Abstract

A hydrocracking catalyst for production of diesel and a jet fuel, and a preparation method therefor. The hydrocracking catalyst comprises a carrier and a metal active component, and the metal active component is loaded on the carrier. The carrier consists of a modified Y-type molecular sieve with the weight percentage of 1wt% to 8wt%, amorphous silicon aluminum of 20wt% to 60wt%, large-pore aluminum oxide of 10wt% to 50wt%, and small-pore aluminum oxide of 10wt% to 40wt%. The weight percentage of the metal active component is 10wt% to 40wt% in the catalyst. The prepared mesoporous NaY-type molecular sieve is a special Y-type molecular sieve in which a mesoporous structure is aggregated by nano-grains, and is provided with a well-developed mesoporous structure having a high specific surface, which can improve the hydrogenation activity, facilitates the diffusion of a reaction product and the selectivity of a target product, also greatly improves the carbon containing capability, reduces the probability of occurrence of excessive cracking and secondary cracking, and improves the activity of the catalyst and the product selectivity.

IPC Classes  ?

• B01J 29/16 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
• C10G 49/08 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves

Abstract

A mesoporous beta zeolite and a preparation method therefor. The mesoporous beta zeolite includes micropores and intracrystalline mesopores, pore diameter of the intracrystalline mesopores being 2.5-9 nm, pore volume of the intracrystalline mesopores is 0.2-0.3 cm3/g, and specific surface area of the intracrystalline mesopores is 142-284m2/g. The mesopore specific surface area and mesopore volume of the present mesoporous beta zeolite are high, and the pore diameter enables carrier pore channels to both ensure a diffusion rate of reactant molecules and realize a relatively high frequency of collision, satisfying a balance between diffusion and collision, and increasing carrier accessibility to large-molecule reactants and guest-molecule diffusion capability. The present preparation method uses cheap and easily obtainable sesbania powder as a mesopore structure-directing agent, and the preparation process is simple and economical, appropriate for industrial production. Crystal grains of the mesoporous beta zeolite prepared by the present method have interconnected mesopores therein, thereby increasing accessibility and molecule diffusion capability of the beta zeolite and broadening the range of applications of the beta zeolite, particularly in relation to reactions between large molecules.

IPC Classes  ?

• C01B 39/48 - Other types characterised by their X-ray diffraction pattern and their defined composition using at least one organic template directing agent
• B01J 29/70 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of types characterised by their specific structure not provided for in groups

Abstract

A method for preparing a mesoporous NaY-type zeolite molecular sieve comprises the following steps: 1) mixing a silicon source, an aluminum source and water in a temperature ranging from 25ºC to 35ºC, adjusting a ph to 9 to 12, dropping an NaY-type molecular sieve directing agent, and then gradually and dropwise adding an organic quaternary ammonium salt serving as a template, so as to obtain aluminosilicate gel; 2) crystallizing the aluminosilicate gel; and 3) roasting a production obtained in step 2) to remove the template. The obtained molecular sieve has a crystallized pore wall structure, the defect of a single pore structure is avoided due to a zeolite molecular sieve of a hierarchical pore structure, is a very valuable catalysis material, and especially has a broad application prospect in reactions that involve in macromolecules and that are limited by diffusion. In the method, the tetradecyl dimethyl benzyl ammonium chloride organic quaternary ammonium salt is used as a mesoporous template, and a new template is provided for the preparation of the mesoporous NaY-type zeolite molecular sieve.

IPC Classes  ?

• C01B 39/24 - Type Y

Abstract

Disclosed are a high-concentration biomass slurry and a preparation method and the use thereof. The high-concentration biomass slurry is mainly obtained by surface modification of biomass powder particles via an emulsified solution; a swelling effect of the biomass powder particles is effectively inhibited, so that the high-concentration biomass slurry is formed. The method for preparing the high-concentration biomass slurry comprises the following steps: 1) blending a non-polar solvent, an emulsifier and optional water into a stable emulsified solution under the conditions of heating and stirring; and 2) homogeneously mixing pulverized biomass powder particles into the emulsified solution, or adding the emulsified solution during biomass breaking and grinding to make the surfaces of the powder particles be modified. Also disclosed is the use of the high-concentration biomass slurry in fields such as biomass power generation and the preparation of synthetic gas using the biomass. The high-concentration biomass slurry is obtained by modifying the biomass powder particles; and the obtained slurry can be conveyed to downstream working procedures requiring a lower energy consumption by using a slurry pump, and high-pressure stable feeding is realized.

IPC Classes  ?

• C10L 5/44 - Solid fuels essentially based on materials of non-mineral origin on vegetable substances
• C10L 9/10 - Treating solid fuels to improve their combustion by using additives
• C10J 3/46 - Gasification of granular or pulverulent fuels in suspension

Abstract

An improved diesel hydrocracking catalyst carrier and a method for preparing same. Raw materials of the carrier comprise the following components in percentage by weight: 3-35% of molecular sieve, 5-75% of γ-Al2O3, 15-75% of amorphous silica-alumina, and 7-40% of binder. The specific surface area of the carrier is 200-450 m2/g, and the total pore volume is 0.35-0.75 cm3/g. During preparation of a composite of molecular sieve and alumina, a molecular sieve without removing a templating agent is added; in a mixed liquid, NH4+ which is generated by means of reaction of an aluminum salt and ammonia water and alkali Na+ which balances negative charges of a molecular sieve framework are exchanged; during roasting, an organic templating agent and NH4+ in the molecular sieve are removed, so that ammonium exchange and templating agent removal of a zeolite molecular sieve are completed during preparation of the composite, without separately performing templating agent removal and ammonium exchange on the molecular sieve. The templating agent has supporting and protecting effects on the pore structure of the molecular sieve. A hydrocracking catalyst prepared using the carrier can remarkably reduce the pour point of a diesel fraction and improve the cetane number of diesel while guaranteeing a high diesel yield.

IPC Classes  ?

• B01J 32/00 - Catalyst carriers in general
• B01J 29/06 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof
• C10G 47/20 - Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof

Abstract

An improved diesel hydrocracking catalyst and a method for preparing same. Raw materials of the catalyst comprise the following components in percentage by weight: 4-25% of molecular sieve, 10-65% of γ-Al2O3, 15-70% of amorphous silica-alumina, 9-40% of binder, and 7-35% of active metal oxide. The specific surface area of the catalyst is 220-450 m2/g, and the total pore volume is 0.30-0.73 cm3/g. During preparation of a composite of molecular sieve and alumina, a molecular sieve without removing a templating agent is added; in a mixed liquid, NH4+ which is generated by means of reaction of an aluminum salt and ammonia water and alkali Na+ which balances negative charges of a molecular sieve framework are exchanged; during roasting, an organic templating agent and NH4+ in the molecular sieve are simultaneously removed, so that ammonium exchange and templating agent removal of a zeolite molecular sieve are completed during preparation of the composite, without separately performing templating agent removal and ammonium exchange on the molecular sieve. The templating agent has supporting and protecting effects on the pore structure of the molecular sieve. The catalyst can remarkably reduce the pour point of a diesel fraction and improve the cetane number of diesel while guaranteeing a high diesel yield.

IPC Classes  ?

• B01J 29/06 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof
• C10G 47/20 - Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof

Abstract

An optimized diesel hydrocracking catalyst carrier and a method for preparing same. Raw materials of the carrier comprise the following components in percentage by weight: 1-35% of modified molecular sieve, 3-75% of γ-Al2O3, 15-75% of amorphous silica-alumina, and 9-40% of binder. The specific surface area of the carrier is 200-450 m2/g, and the total pore volume is 0.35-0.75 cm3/g. A modified molecular sieve is added to an inorganic aluminum salt solution used for preparing γ-Al2O3, and precipitation, drying, and roasting are performed to obtain a composite of molecular sieve and γ-Al2O3; then the remaining materials are mixed with the composite according to the material proportion of the catalyst carrier, and rolling, forming, drying, and activation are performed to obtain the catalyst carrier. The molecular sieve in the carrier has a high silica/alumina ratio and high specific surface area, and is highly dispersed in the carrier; thus, the carrier has more uniform acid sites, and alumina is in closer contact with the molecular sieve. A prepared hydrocracking catalyst can remarkably reduce the pour point of a diesel fraction and improve the cetane number of diesel while guaranteeing a high diesel yield.

IPC Classes  ?

• B01J 32/00 - Catalyst carriers in general
• B01J 29/70 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of types characterised by their specific structure not provided for in groups
• C10G 47/16 - Crystalline alumino-silicate carriers

Abstract

An optimized diesel hydrocracking catalyst and a method for preparing same. Raw materials comprise the following components in percentage by weight: 1-25% of modified molecular sieve, 10-65% of γ-Al2O3, 15-70% of amorphous silica-alumina, 9-40% of binder, and 10-35% of active metal oxide. The specific surface area of the catalyst is 200-450 m2/g, and the total pore volume is 0.30-0.65 cm3/g. To obtain a carrier, a modified molecular sieve is added to an inorganic aluminum salt solution used for preparing γ-Al2O3, and precipitation, drying, and roasting are performed to obtain a composite of molecular sieve and γ-Al2O3; then the remaining materials are mixed with the composite according to the material proportion of the catalyst, and rolling, forming, drying, and activation are performed to obtain the catalyst. The molecular sieve in the catalyst carrier has a high silica/alumina ratio and high specific surface area, and is highly dispersed in the carrier; thus, the carrier has more uniform acid sites, and alumina is in closer contact with the molecular sieve; and therefore, the catalyst can remarkably reduce the pour point of a diesel fraction and improve the cetane number of diesel while guaranteeing a high diesel yield.

IPC Classes  ?

• B01J 29/14 - Iron group metals or copper
• B01J 29/16 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the faujasite type, e.g. type X or Y containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
• B01J 29/46 - Iron group metals or copper
• B01J 29/48 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
• B01J 29/72 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of types characterised by their specific structure not provided for in groups containing iron group metals, noble metals or copper
• B01J 29/76 - Iron group metals or copper
• B01J 29/78 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of types characterised by their specific structure not provided for in groups containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
• C10G 47/20 - Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof

Abstract

Disclosed is a high-nitrogen crude oil hydrorefining catalyst, composed of the following three parts: a carrier, an active component and an adjuvant. The carrier is an alumina carrier, the active component is dualistic, comprising the metal Mo and the metal Ni, and the adjuvant is the non-metal P. In the active component, the load amount of MoO3 is 20%-26% of the mass of the catalyst, and the load amount of NiO is 3.0%-3.8% of the mass of the catalyst. The high-nitrogen crude oil hydrorefining catalyst prepared using the alumina carrier has a relatively high specific surface area and pore volume, and the pore size distribution is centralized, and the mass transfer diffusion effect is good.

IPC Classes  ?

• B01J 27/19 - Molybdenum
• B01J 27/185 - PhosphorusCompounds thereof with iron group metals or platinum group metals
• B01J 21/04 - Alumina
• B01J 32/00 - Catalyst carriers in general
• B01J 35/10 - Solids characterised by their surface properties or porosity
• C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof

Abstract

A hydrotreating catalyst impregnating solution and a preparation method therefor. The impregnating solution is an aqueous solution prepared from a molybdenum-containing compound, a nickel-containing compound, a phosphorus-containing compound, and a carbonate. The preparation method comprises the following steps: 1) adding the molybdenum-containing compound, the nickel-containing compound, and the phosphorus-containing compound to water, and mixing uniformly; 2) heating to raise the temperature by two steps: in the first step, raising the temperature to 35-60°C and reacting for 0-1.5 hours at a constant temperature, and in the second step, further raising the temperature to 90-110°C and performing reflux for 0-3 hours at a constant temperature, to enable the solute added in step 1) to be completely dissolved, thereby obtaining a blackish green clear and transparent solution. In step 2), the carbonate is added to adjust the pH of the impregnating solution to 2-6. The impregnating solution has high metal content and stable properties, is suitable for long-term storage, and has a high and adjustable pH value; a prepared catalyst has high activity.

IPC Classes  ?

• B01J 27/19 - Molybdenum
• B01J 37/02 - Impregnation, coating or precipitation
• C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof

Abstract

A method for preparing a hydrotreating catalyst by an impregnation method, comprising the following steps: 1) preparing an impregnating solution, which contains 10-80 g/100 ml of a molybdenum-containing compound, calculated as MoO3, 1-15 g/100 ml of a nickel-containing compound, calculated as NiO, 0.5-5 g/100 ml of a phosphorus-containing compound, calculated as the P element, a carbonate with a concentration of 0-20 g/100 ml, the pH of the solution being 2-6; 2) preparing an aluminum oxide carrier; and 3) impregnating the aluminum oxide carrier obtained in step 2) by using the impregnating solution obtained in step 1), and then drying and roasting to obtain a final hydrotreating catalyst. The specific surface area and pore volume of the hydrotreating catalyst prepared by this method are improved in different degrees, distribution of active metal on the surface of a carrier is facilitated, and the interaction force between the active metal and the carrier is uniform, so that the hydro-desulfurization and hydro-denitrification performances of the catalyst are both improved.

IPC Classes  ?

• B01J 27/19 - Molybdenum
• B01J 35/10 - Solids characterised by their surface properties or porosity
• B01J 37/02 - Impregnation, coating or precipitation
• C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof

Abstract

Provided are a hydroisomerization dewaxing catalyst and method for preparation thereof; said hydroisomerization dewaxing catalyst is obtained by way of a catalyst carrier loading an active metal component in a soaking liquid, then drying and calcining, said soaking liquid containing Pt metal salt, a second metal ion Sm3+, and a third metal ion cerium Ce3+. The method for preparing the hydroisomerization dewaxing catalyst comprises the following steps: (1) preparing a catalyst carrier; (2) placing the catalyst carrier into a a soaking liquid and soaking, the soaking time being 2-24 h; (3) drying and calcining the soaked catalyst carrier to obtain a catalyst finished product. A second metal ion Sm3+ and third metal ion cerium Ce3+ are introduced into a soaking liquid containing Pt, thus performing a modification, forming a trimetallic complex cluster, greatly improving the dispersity of a noble metal on the surface of a carrier; the Pt load required by a catalyst prepared with the same hydroisomerization catalytic activity is reduced.

IPC Classes  ?

• B01J 29/85 - Silicoaluminophosphates [SAPO compounds]
• B01J 29/74 - Noble metals

Abstract

A selective hydrogenation catalyst, a method for preparing same, and a catalytic evaluation method in generation of isobutyraldehyde. The selective hydrogenation catalyst consists of two parts, i.e., a carrier and an active component. The active component comprises a precious metal material and a non-precious metal material. The carrier is one of fumed silica, precipitated silica, aluminum oxide, carbon nitride, and titanium dioxide. The precious metal material is precious metal Ir. The non-precious metal material is any one of non-precious metals Mo, W, Ni, Co, Sm, Ce, and Re. The atomic ratio of the non-precious metal material to the precious metal material is 0.8-5. The catalyst can be used for selectively hydrogenating methacrolein to generate isobutyraldehyde under a mild reaction condition and in water.

IPC Classes  ?

• B01J 23/652 - Chromium, molybdenum or tungsten
• C07C 45/62 - Preparation of compounds having C=O groups bound only to carbon or hydrogen atomsPreparation of chelates of such compounds by reactions not involving the formation of C=O groups by hydrogenation of carbon-to-carbon double or triple bonds
• C07C 47/02 - Saturated compounds having —CHO groups bound to acyclic carbon atoms or to hydrogen
• B01J 23/46 - Ruthenium, rhodium, osmium or iridium
• B01J 21/06 - Silicon, titanium, zirconium or hafniumOxides or hydroxides thereof
• B01J 21/12 - Silica and alumina

Abstract

Provided are a selective hydrogenation catalyst, a preparation method therefor, and an evaluation method for a catalytic preparation of 2-methylallyl alcohol. The selective hydrogenation catalyst consists of two parts, namely, a carrier and an active component, wherein the active component comprises a precious metal material and a non-precious metal material, and the carrier is a mesoporous silicon material, wherein the precious metal material is the precious metal Ir, and the non-precious metal material is any one of the non-precious metals Mo, W, Ni and Co, and the atomic ratio of the non-precious metal material to the precious metal material is 0.1-1. The catalyst can catalytically reduce an unsaturated aldehyde into an unsaturated alcohol under relatively mild reaction conditions and in water.

IPC Classes  ?

• B01J 29/03 - Catalysts comprising molecular sieves not having base-exchange properties
• B01J 23/46 - Ruthenium, rhodium, osmium or iridium
• B01J 23/652 - Chromium, molybdenum or tungsten
• C07C 29/157 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of oxides of carbon exclusively with hydrogen or hydrogen-containing gases characterised by the catalyst used containing iron group metals, platinum group metals, or compounds thereof containing platinum group metals or compounds thereof
• C07C 29/141 - Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen-containing functional group of C=O containing groups, e.g. —COOH of a —CHO group with hydrogen or hydrogen-containing gases

Abstract

2), 10-55 parts of a silicoaluminophosphate (SAPO) molecular sieve, 5-50 parts of modified mesoporous molecular sieve Al-SBA-16, 1-3 parts of sesbania gum powder, and 10-70 parts of alumina A catalyst includes a soluble cobalt salt and the aforesaid carrier. The soluble cobalt salt is loaded on the surface of the carrier.

IPC Classes  ?

• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• B01J 21/00 - Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
• B01J 21/04 - Alumina
• B01J 21/06 - Silicon, titanium, zirconium or hafniumOxides or hydroxides thereof
• B01J 29/04 - Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites, pillared clays
• B01J 29/85 - Silicoaluminophosphates [SAPO compounds]
• B01J 32/00 - Catalyst carriers in general
• B01J 35/02 - Solids
• B01J 35/10 - Solids characterised by their surface properties or porosity
• C01B 39/02 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereofDirect preparation thereofPreparation thereof starting from a reaction mixture containing a crystalline zeolite of another type, or from preformed reactantsAfter-treatment thereof
• C01B 39/54 - Phosphates, e.g. APO or SAPO compounds
• C10G 47/20 - Crystalline alumino-silicate carriers the catalyst containing other metals or compounds thereof
• B01J 27/185 - PhosphorusCompounds thereof with iron group metals or platinum group metals

Abstract

Provided is a process for producing hydrogen by means of the adsorption catalysis of a crude synthetic gas, comprising the following steps: 1) mixing water vapour and a crude synthetic gas in a water-carbon molar ratio of 2 to 6 : 1, adding a reduced reforming catalyst with an adsorption function, and carrying out a reforming hydrogen-producing reaction in a fluidised state; 2) subjecting the reforming catalyst after the reaction to high-temperature combustion so as to oxidise and remove a carbon deposit and sulphur-containing components thereon, and heating the reforming catalyst so as to release CO2 and realise regeneration; and 3) subjecting the regenerated reforming catalyst to in-situ reduction at 400ºC to 900ºC, and recycling the resulting reduced reforming catalyst for hydrogen production to obtain a product, namely, hydrogen. Also provided is a device for producing hydrogen by means of the adsorption catalysis of a crude synthetic gas. By means of the method, the crude synthetic gas containing tar and sulphur can be further converted into hydrogen, so that the steps of the sulphur removal and tar separation of the crude synthetic gas are omitted, and the selection range of hydrogen-producing raw material gases is greatly broadened; the reforming catalyst is reduced in-situ, without a reduction procedure needing to be additionally arranged; and the device saves the use of auxiliary apparatuses such as a degassing tank and a reduction reactor, such that the procedure is greatly simplified.

IPC Classes  ?

• C01B 3/40 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts characterised by the catalyst
• C01B 3/44 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts using moving solid particles using the fluidised bed technique
• B01J 23/78 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with alkali- or alkaline earth metals or beryllium

Abstract

Disclose are a monodispersed iron-based catalyst for the Fischer-Tropsch process, a preparation method therefor and the use thereof. The catalyst comprises a carrier, i.e. silicon dioxide and an active component, i.e. iron. The carrier, i.e. silicon dioxide has a mesoporous spherical particle structure, and the carrier, i.e. silicon dioxide covers the active component, i.e. iron. The active component, i.e. iron is of a nanoparticle shape and is distributed uniformly. The particle size of the carrier, i.e. silicon dioxide particle is 140 - 160 nm. In the preparation method therefor, the pressure of CO2 is adjusted, so that the morphology of the catalyst is changed from a disc-shaped stack into a uniform spherical shape. The iron nanoparticles are thus covered in the interior of the spherical silicon dioxide, sintering of the iron nanoparticles is prevented, and the appearance of an ingredient which is difficult to reduce is also avoided. The iron-based catalyst can be applied to a process route for preparing an α-olefin, wherein the α-olefin is directly synthesized by using a synthetic gas as a raw material under the action of the iron-based catalyst. The iron-based catalyst has a high selectivity for a long chain α-olefin.

IPC Classes  ?

• B01J 23/745 - Iron
• B01J 35/10 - Solids characterised by their surface properties or porosity
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• B01J 37/10 - Heat treatment in the presence of water, e.g. steam

Abstract

A comprehensive utilization process for selective catalytic oxidative conversion of a tail gas from Fischer-Tropsch synthesis. The process comprises: conditioning a raw gas for Fischer-Tropsch synthesis, feeding the raw gas into a Fischer-Tropsch synthesis reactor, then performing a Fischer-Tropsch synthesis reaction to obtain a liquid hydrocarbon product and a tail gas; feeding the tail gas into a gas separation device to separate and to extract hydrogen from the tail gas, collecting a portion of a separated tail gas obtained after hydrogen extraction for use as a recycled tail gas, transporting the recycled tail gas into a selective catalytic oxidative conversion reactor, allowing, under the effect of a catalyst, a light hydrocarbon in the recycled tail gas to undergo selective catalytic oxidation with an oxidizing agent, and be converted into hydrogen and carbon monoxide; and returning the hydrogen and carbon monoxide to mix with the raw gas for Fischer-Tropsch synthesis, and to enter the Fischer-Tropsch synthesis reactor again to produce a liquid hydrocarbon product. The process lowers the depth of raw gas conversion and the scale of conversion equipment, increases the utilization rate and carbon efficiency of Fischer-Tropsch synthesis raw material, and improves the economics of a Fischer-Tropsch system.

IPC Classes  ?

• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts

Abstract

A boron-modified hydrofining catalyst having a high loading amount and a preparation method therefor. The catalyst consists of an active metal component and a carrier. The active metal component is carried by the carrier. The active metal component consists of oxides containing group VIB and group VIII metals. The group VIB metal is Mo and/or W, and the group VIII metal is Ni and/or Co. The carrier is a boron-modified aluminium oxide carrier. The boron-modified hydrofining catalyst and B2O3 are uniformly distributed and concentrated on the surface of the aluminium oxide carrier, so as to prevent the active component from entering an aluminium oxide lattice, help to improve the dispersity and utilization of the metal component, and further improve the hydrogenation activity of the catalyst. In addition, a boracic hydrofining catalyst having a high loading amount can be obtained, and the catalyst has high denitrification activity.

IPC Classes  ?

• B01J 23/83 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with rare earths or actinides
• C10G 45/08 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing nickel or cobalt metal, or compounds thereof in combination with chromium, molybdenum, or tungsten metals, or compounds thereof

Abstract

An apparatus for producing diesel fuel and jet fuel using Fischer-Tropsch synthetic oil, the apparatus including a hydrofining reactor, a hot separator, a first rectifying column, a hydrocracking reactor, a hydroisomerization reactor, a second rectifying column, a first mixing chamber and a second mixing chamber. The hydrofining reactor includes a raw material inlet and a hydrofining product outlet. The hot separator includes a separated oil outlet and a hydrofining product inlet which is connected to the hydrofining product outlet. The first rectifying column includes a tail oil fraction outlet, a diesel fraction outlet and a separated oil inlet which is connected to the separated oil outlet. The first mixing chamber includes a circulating hydrogen inlet, a first mixture outlet and a tail oil fraction inlet which is connected to the tail oil fraction outlet.

IPC Classes  ?

• B01J 19/24 - Stationary reactors without moving elements inside
• C10G 65/12 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only including cracking steps and other hydrotreatment steps
• C10G 67/02 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
• C10G 45/02 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing
• C10G 47/00 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions
• C10G 65/14 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural parallel stages only

Abstract

An integral iron cobalt bimetallic Fischer-Tropsch synthesis catalyst and a preparation method therefor. The catalyst comprises a porous metal iron carrier, a molecular sieve membrane coated on the surface of the porous metal iron carrier, and a metal active component loaded on the molecular sieve membrane. The porous metal iron carrier is an integral three-dimensional network structural carrier which is formed by: dividing a polyurethane foam into pieces to use as a template, immersing the same in a binder solution containing active powder alumina, potassium carbonate, calcium carbonate, magnetite and iron powder, drying and sintering so as to form the carrier. The weights of the major components in the integral three-dimensional network structural carrier satisfy the following mathematical relationship: Fe∶Al2O3:K2O∶CaO＝100∶(1.5-6.0)∶(0.2-2.8)∶(0.2-3.2); the molecular sieve membrane is a cluster aggregate having uniformly dispersed ZSM-5 nanoparticles; and the load of the metal active component cobalt accounts 10-30% of the weight of the finished catalyst product. The catalyst has the advantages of having a large carrier surface area and strong catalyst adhesion performances. The catalyst preparation method is simple and the product performance is stable.

IPC Classes  ?

• B01J 29/46 - Iron group metals or copper
• B01J 35/10 - Solids characterised by their surface properties or porosity
• C07C 1/04 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon monoxide with hydrogen

Abstract

Provided is a method for preparing boron-modified aluminium oxide. The method comprises the following steps: 1) preparing an aqueous boric acid solution having a mass concentration of 0.5%-6.0% at room temperature; 2) taking an aluminium oxide precursor and placing same in a hydro-thermal treatment furnace, and introducing the aqueous boric acid solution into the furnace, wherein the amounts of the aluminium oxide precursor and the aqueous boric acid solution are as follows: the content in percentage by weight of B2O3 therein is 1.0%-10.0%, based on the mass of the boron-modified aluminium oxide carrier; and 3) heating the hydro-thermal treatment furnace for hydro-thermal treatment of the aluminium oxide precursor so as to give the boron-modified aluminium oxide, wherein the hydro-thermal treatment temperature is 450℃-700℃ and the reaction pressure inside the hydro-thermal treatment furnace is 0-0.3 MPa. The method not only can make the auxiliary boron better distributed on the surface of the aluminium oxide carrier, and improve the dispersity of active components, but also can adjust the ratio of a B acid and an L acid of the aluminium oxide carrier and improve the pore structure of the aluminium oxide carrier.

IPC Classes  ?

• B01J 32/00 - Catalyst carriers in general
• B01J 21/02 - Boron or aluminiumOxides or hydroxides thereof
• C10G 45/04 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used

Abstract

Provided are a multi-level channel-type cobalt-based Fischer-Tropsch synthetic catalyst with a core-shell structure and a preparation method therefor. The catalyst comprises a catalyst carrier S, a metal active component Co loaded on the catalyst carrier S and a shell layer molecular sieve membrane M which wraps the surface of the catalyst carrier S, wherein the catalyst carrier S is one of or a mixture of two of SiO2 and Al2O3 in any proportion, the microstructure morphology of SiO2 and Al2O3 is spherical, the specific surface area thereof is 160-290 m2/g, and the average particle size ranges between 10 and 50 meshes; the shell layer molecular sieve membrane M is a cluster aggregate of uniformly dispersed H-ZSM-5 nanoparticles, the particle size of the H-ZSM-5 nanoparticles ranges between 10-30 nm, the micropore aperture thereof is less than or equal to 2.0 nm, and the gap between adjacent H-ZSM-5 nanoparticles is less than or equal to 100 nm; and the loading amount of the metal active component Co accounts for 10-30% of the sum of the weights of the catalyst carrier S and the metal active component Co. The shell layer of the Fischer-Tropsch synthetic catalyst has a multi-level channel and a high catalytic efficiency. Meanwhile, the preparation method is simple in process and low in energy consumption.

IPC Classes  ?

• B01J 29/46 - Iron group metals or copper
• B01J 35/08 - Spheres
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon

Abstract

A selective hydrogenation catalyst for producing biodiesel and a preparation method and an application therefor. The selective hydrogenation catalyst comprises a carrier and a main metal active component, the main metal active component being loaded onto the carrier; the weight percentage of the catalyst product occupied by the main metal active component is 5-30%, the main metal active component being one or a combination of more than one oxide containing Co, Mo, Ni, or W, and the carrier being composed of 1-8% molecular sieves, 25-65% amorphous silicon aluminium, 30-65% aluminium oxide, and 2-10% graphene adjuvant calculated by weight percentage of the raw ingredient. The method for preparing the catalyst comprises immersing the carrier in a metal salt solution containing Co, Mo, Ni, and/or W for 4-20 h to obtain an immersed carrier; and, after freeze-drying, calcining the immersed carrier to obtain the selective hydrogenation catalyst. Under the same load, the carrier has a larger active surface area and has more active sites, reducing reaction temperature and improving hydrogenation performance.

IPC Classes  ?

• B01J 29/76 - Iron group metals or copper
• B01J 29/78 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of types characterised by their specific structure not provided for in groups containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
• B01J 29/14 - Iron group metals or copper
• B01J 29/80 - Mixtures of different zeolites
• B01J 29/85 - Silicoaluminophosphates [SAPO compounds]
• C10G 45/12 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves

Abstract

Provided is a selective hydrogenation catalyst used for producing aviation biofuel, comprising a carrier and a main metal active ingredient, said main metal active ingredient being loaded on said carrier; the weight percentage of the main metal active ingredient with respect to the catalyst finished product is 0.05-1.15%; the main metal active ingredient is Pt or Pd; the weight percentages of the raw materials of the carrier are 2-10% molecular sieve, 25-65% amorphous silica-alumina, 30-65% aluminum oxide, and 2-10% graphene additive. The method for preparing the catalyst comprises: placing the carrier into a metal saline solution containing Pt or Pd and soaking for 4-20 h to obtain a carrier after soaking; after drying said carrier, processing in a reduction atmosphere to obtain a selective hydrogenation catalyst. At the same capacity, the active surface area of the catalyst is larger and has more active sites, reducing reaction temperature and improving hydrogenation performance.

IPC Classes  ?

• B01J 29/74 - Noble metals
• B01J 29/12 - Noble metals
• B01J 29/80 - Mixtures of different zeolites
• B01J 29/85 - Silicoaluminophosphates [SAPO compounds]
• C10G 45/12 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves

Abstract

Provided is a combined solar-powered seawater desalination and air-conditioned cooling method and system having high efficiency. The method comprises: a solar energy collection step, a seawater desalination step, and an air-conditioned cooling step. The seawater desalination step uses a heat conducting medium used in the solar energy collection step as a heat source. The air-conditioned cooling step uses steam from a distillation process as a heat source. An air conditioning coolant is cooled by means of heat exchange with seawater. A device of the invention comprises: a solar energy collecting system (I), a seawater desalination system (II), and an absorption air conditioning system (III). The seawater desalination system (II) comprises a distillation system (27) and a heat exchange system (28). The distillation system (27) implements heating by means of the solar energy collection system (I). A heated steam inlet (1.1) of the absorption air conditioning system (III) communicates with a steam outlet (27.3) of the distillation system (I). A coolant inlet (8.1) and coolant outlet (3.1) of the absorption air conditioning system (III) respectively communicate with an air conditioning coolant outlet (30.2) and air conditioning coolant inlet (30.1) of the heat exchange system (28). The invention uses solar power as a heat source to implement seawater desalination and air-conditioned cooling at the same time, thereby improving energy use efficiency.

IPC Classes  ?

• C02F 1/14 - Treatment of water, waste water, or sewage by heating by distillation or evaporation using solar energy
• F25B 15/02 - Sorption machines, plants or systems, operating continuously, e.g. absorption type without inert gas

Abstract

A method and equipment thereof for producing high quality diesel using low-temperature Fischer-Tropsch synthetic oil and low-grade oil feedstock. The method comprises the following steps: 1) mixing a Fischer-Tropsch diesel with hydrogen, and after saturation with the dissolved hydrogen, using a liquid-phase hydrogenation process for refining hydrogenation; 2) mixing a hydrogenated and refined reactant obtained from Step 1) with a low-grade oil feedstock and Fischer-Tropsch paraffin to obtain an oil mixture, then subjecting the oil mixture to a gas-liquid countercurrent hydrogenation method for refining hydrogenation; 3) using a gas-liquid countercurrent hydrogenation method to hydrogenate, crack, and isomerize a hydrogenated and refined reactant obtained from Step 2); and 4) performing fractional distillation on a liquid-phase oil produced in Step 3) to obtain the high-quality diesel. The method combines liquid-phase hydrogenation and gas-liquid countercurrent hydrogenation for processing a Fischer-Tropsch synthetic oil and low-grade diesel to obtain a diesel with qualified density and high cetane number.

IPC Classes  ?

• C10G 65/02 - Treatment of hydrocarbon oils by two or more hydrotreatment processes only plural serial stages only

Abstract

A supported iron-based catalyst for Fischer-Tropsch synthesis and manufacturing method thereof. The catalyst comprising: a support, an active component of Fe, and an adjuvant of Cu and K, wherein the mass percentage of the Fe is 20-60% relative to the carrier, and the mass ratio of Fe to Cu to K is 100:5-10:4-12. The Cu and K adjuvants are uniformly distributed across the surface of the catalyst. The manufacturing process introduces one or more non-ionic surfactant. The surfactant is then mixed with an inorganic salt of the active component Fe. The method introduces ultrasounds or microwaves during the impregnation process, improving the drying and roasting conditions, thereby improving catalyst activity and stability.

IPC Classes  ?

• B01J 23/78 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with alkali- or alkaline earth metals or beryllium
• B01J 29/46 - Iron group metals or copper
• B01J 37/02 - Impregnation, coating or precipitation
• B01J 37/34 - Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves

Abstract

A separation device for a catalyst and heavy hydrocarbon in a slurry bed reactor. The separation device comprises a filter tank (1), a sieve plate (2), an electromagnet (3) and a filtrate tank (4). A catalyst outlet of the filter tank (1) is connected to an input end of the filtrate tank (4). An output end of the filtrate tank (4) is connected to a filtrate circulation return inlet of the filter tank (1). A pipeline between the output end of the filtrate tank (4) and the filtrate circulation return inlet of the filter tank (1) is communication with a product conveying pipe of a product storage tank (5). The catalyst outlet of the filter tank (1) is further connected to a catalyst discharging pipe. A lower portion inside the filter tank (1) is provided with the sieve plate (2), on which a magnetic filter medium layer (6) is provided. The filter tank (1) is provided with the electromagnet (3), which generates a uniform magnetic field at the sieve plate (2). The separation device provides highly efficient solid-liquid separation without blocking a filter medium, and a separated solid catalyst can be recycled and reused, enabling a slurry bed reactor to operate continuously in industrial applications.

IPC Classes  ?

• B01J 8/22 - Chemical or physical processes in general, conducted in the presence of fluids and solid particlesApparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• B01D 35/06 - Filters making use of electricity or magnetism

Abstract

A system and method for producing low-condensation-point middle distillate using Fischer-Tropsch synthesized whole distillate. In the system, a Fischer-Tropsch heavy oil transport pipe (5) is connected to a middle input end of a first hydrogenation reactor (1); a Fischer-Tropsch light oil transport pipe (6) is connected to a bottom input end of the first hydrogenation reactor (1); a first hydrogen transport pipe (7) is in communication with the Fischer-Tropsch heavy oil transport pipe (5); a second hydrogen transport pipe (8) is in communication with the Fischer-Tropsch light oil transport pipe (6); an output pipe of the first hydrogenation reactor (1) is connected to a bottom input end of a second hydrogenation reactor (2); a top output end of the second hydrogenation reactor (2) is connected to an input end of a gas-liquid separator (3); a liquid-phase output end of the gas-liquid separator (3) is connected to an input end of a fractionating column (4); the fractionating column (4) has a naphtha product output port (9) and a low-condensation-point diesel output port (10). In the method, a lower feeding approach is used in all the hydrogenation reactors, thereby achieving more appropriate distribution of hydrogen concentration along the axial directions of the reactors and minimum temperature gradient in the reactors, and overcoming the defect of large pressure drop in the upper part of a catalyst bed layer.

IPC Classes  ?

• C10G 67/02 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only

Abstract

Provided are an ultra-dispersed cobalt/platinum-based catalyst for Fischer-Tropsch synthesis and a manufacturing method thereof. The catalyst comprises an alumina carrier, an active cobalt species, and an active platinum additive in amounts of 53-84.5%, 15-45%, and 0.5-2.0% by weight, respectively. The alumina carrier has a size of 0.6-2.4 mm and a specific surface area of 140-300 m2/g. The active cobalt species and the active platinum additive have a particle size of 3-20 nm and are loaded on the alumina carrier in uniformly dispersed nanoclusters. The process parameters for the catalyst manufacturing method of the present invention are easy to apply. High dispersion of the cobalt species is achieved in the final catalyst product.

IPC Classes  ?

• B01J 23/89 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with noble metals
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon

Abstract

Provided is an apparatus and method for producing an environmentally-friendly solvent oil using a Fischer-Tropsch synthetic oil. The device comprises a hydrorefining reactor (A), a hydrogenation reactor (B), a hot high-pressure separator (C), an alkaline tower (D), a rectification tower (E), and a condenser (F). The method comprises feeding a mixture of the Fischer-Tropsch synthetic oil and hydrogen into the hydrorefining reactor (A), then feeding a mixture of the resultant product and hydrogen into the hydrogenation reactor (B), and the final product entering the hot high-pressure separator (C) to be separated into a gas-phase fraction and a liquid-phase fraction. The gas-phase fraction flows through the alkaline tower (D), and enters the condenser (F) for separation. A mixture of the separated gas portion and fresh hydrogen flows back to the hydrorefining reactor (A) and the hydrogenation reactor (B). The liquid-phase fraction obtained from the hot high-pressure separator (C) enters the rectification tower (E), and is fractionated to produce a naphtha fraction, an environmentally-friendly solvent oil and an unconverted oil.

IPC Classes  ?

• C10G 67/00 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only

Abstract

A catalyst for preparing aviation fuel from synthetic oil obtained by Fischer-Tropsch process, including: between 20 and 50 percent by weight of an amorphous aluminum silicate, between 5 and 20 percent by weight of alumina, between 20 and 60 percent by weight of a hydrothermally modified zeolite, between 0.5 and 1.0 percent by weight of a Sesbania powder, between 0.5 and 5 percent by weight of nickel oxide, and between 5 and 15 percent by weight of molybdenum oxide. The invention also provides a method for preparing the catalyst.

IPC Classes  ?

• B01J 21/04 - Alumina
• B01J 23/28 - Molybdenum
• B01J 23/755 - Nickel
• B01J 23/883 - Molybdenum and nickel
• B01J 29/48 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
• B01J 29/78 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of types characterised by their specific structure not provided for in groups containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
• B01J 35/02 - Solids
• B01J 37/00 - Processes, in general, for preparing catalystsProcesses, in general, for activation of catalysts
• B01J 37/02 - Impregnation, coating or precipitation
• B01J 37/04 - Mixing
• B01J 37/06 - Washing
• B01J 37/08 - Heat treatment
• C10G 49/04 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or characterised by the catalyst used containing nickel, cobalt, chromium, molybdenum, or tungsten metals, or compounds thereof
• C10G 49/08 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves

Abstract

A method for gasifying biomass using a gasifier, the gasifier including a furnace body and a fuel pretreatment system. The method includes 1) crushing and sieving a biomass fuel to yield particle size-qualified fuel particles, 2) exciting working gas to yield plasma, and spraying the plasma into the gasifier, 3) spraying the particle size-qualified fuel particles into the gasifier via nozzles, synchronously spraying an oxidizer via an oxygen/vapor inlet into the gasifier, and 4) monitoring the temperature and components of the syngas, regulating an oxygen flow rate, a vapor flow rate, and microwave power to maintain the process parameters within a preset range and to control a temperature of the syngas to be between 900 and 1200° C., collecting the syngas from the syngas outlet at the top of the furnace body, and discharging liquid slag from the slag outlet.

IPC Classes  ?

• C10J 3/72 - Other features
• C10J 3/18 - Continuous processes using electricity
• C10J 3/48 - ApparatusPlants
• C10J 3/50 - Fuel charging devices
• C10J 3/46 - Gasification of granular or pulverulent fuels in suspension

Abstract

A catalyst including between 50.0 and 99.8 percent by weight of iron, between 0 and 5.0 percent by weight of a first additive, between 0 and 10 percent by weight of a second additive, and a carrier. The first additive is ruthenium, platinum, copper, cobalt, zinc, or a metal oxide thereof. The second additive is lanthanum oxide, cerium oxide, magnesium oxide, aluminum oxide, silicon dioxide, potassium oxide, manganese oxide, or zirconium oxide.

IPC Classes  ?

• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• B01J 23/889 - Manganese, technetium or rhenium
• B01J 23/745 - Iron
• B01J 23/75 - Cobalt
• B01J 23/78 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with alkali- or alkaline earth metals or beryllium
• B01J 23/72 - Copper
• B01J 23/80 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with zinc, cadmium or mercury
• B01J 21/08 - Silica
• B01J 23/83 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with rare earths or actinides
• B01J 23/86 - Chromium
• B01J 23/89 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with noble metals
• B01J 35/00 - Catalysts, in general, characterised by their form or physical properties
• B01J 35/08 - Spheres
• B01J 37/00 - Processes, in general, for preparing catalystsProcesses, in general, for activation of catalysts
• B01J 37/02 - Impregnation, coating or precipitation
• B01J 37/04 - Mixing
• B01J 37/08 - Heat treatment

Abstract

A catalyst including cobalt, a carrier including silica, and a selective promoter including zirconium. The cobalt and the selective promoter are disposed on the surface of the carrier, and the outer surfaces of the active component cobalt and the selective promoter zirconium are coated with a shell layer including a mesoporous material. A method for preparing the catalyst, including: 1) soaking the carrier including silica into an aqueous solution including a zirconium salt, aging, drying, and calcining a resulting mixture to yield a zirconium-loaded carrier including silica; 2) soaking the zirconium-loaded carrier including silica into an aqueous solution including a cobalt salt, aging, drying, calcining a resulting mixture to yield a primary cobalt-based catalyst; 3) preparing a precursor solution of a mesoporous material; and 4) soaking the primary cobalt-based catalyst into the precursor solution of the mesoporous material; and crystalizing, washing, drying, and calcining a resulting mixture.

IPC Classes  ?

• B01J 21/08 - Silica
• B01J 23/75 - Cobalt
• B01J 21/06 - Silicon, titanium, zirconium or hafniumOxides or hydroxides thereof
• B01J 31/02 - Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
• B01J 33/00 - Protection of catalysts, e.g. by coating
• B01J 35/10 - Solids characterised by their surface properties or porosity
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• B01J 35/00 - Catalysts, in general, characterised by their form or physical properties
• B01J 35/02 - Solids
• B01J 37/00 - Processes, in general, for preparing catalystsProcesses, in general, for activation of catalysts
• B01J 37/02 - Impregnation, coating or precipitation
• B01J 37/08 - Heat treatment

Abstract

A hybrid power generation system using solar energy and bioenergy, including a solar thermal boiler system, a biomass boiler system, and a turbogenerator system. The solar thermal boiler system includes a trough solar collector, a heat collector, an oil circulating pump, a storage tank for storing heat transfer oil, a solar thermal heater, a solar thermal evaporator, a main pipe transporting saturated steam, and an auxiliary boiler. Heat transfer oil output from a solar light field of the solar thermal boiler system is transmitted through and transfers heat to the solar thermal evaporator and the solar thermal heater, and the heat transfer oil returns to the storage tank for storing heat transfer oil. The heat transfer oil in the storage tank is pumped to the solar light field via the oil circulating pump.

IPC Classes  ?

• F02C 6/00 - Plural gas-turbine plantsCombinations of gas-turbine plants with other apparatusAdaptations of gas-turbine plants for special use
• F01D 15/10 - Adaptations for driving, or combinations with, electric generators
• F01K 3/18 - Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters
• F03G 6/06 - Devices for producing mechanical power from solar energy with solar energy concentrating means
• F03G 7/00 - Mechanical-power-producing mechanisms, not otherwise provided for or using energy sources not otherwise provided for
• F01K 11/02 - Steam engine plants characterised by the engines being structurally combined with boilers or condensers the engines being turbines
• H02K 7/18 - Structural association of electric generators with mechanical driving motors, e.g.with turbines

Abstract

A power generation system, including: a solar energy concentration system, a biomass gasification device, a gas-powered generator, a steam turbine, a steam-powered generator. The solar energy concentration system is connected to a solar energy heat exchange system. The biomass gasification device is connected to the gas-powered generator. The gas outlet of the gas turbine is connected to the gas exhaust heat system. The second steam outlet of the gas exhaust heat system is connected to the second and the third cylinders of the steam turbine. The first steam outlet of the gas exhaust heat system and the steam outlet of the solar energy heat exchange system are connected to a steam mixing regulating system. The mixed steam outlet of the steam mixing regulating system is connected to the first cylinder of the steam turbine.

IPC Classes  ?

• F01D 15/10 - Adaptations for driving, or combinations with, electric generators
• F02C 6/00 - Plural gas-turbine plantsCombinations of gas-turbine plants with other apparatusAdaptations of gas-turbine plants for special use
• H02K 7/18 - Structural association of electric generators with mechanical driving motors, e.g.with turbines
• H02P 9/04 - Control effected upon non-electric prime mover and dependent upon electric output value of the generator
• F02C 3/28 - Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension using a separate gas producer for gasifying the fuel before combustion
• F03G 6/02 - Devices for producing mechanical power from solar energy using a single state working fluid
• F01K 27/00 - Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for
• F01K 3/18 - Plants characterised by the use of steam or heat accumulators, or intermediate steam heaters, therein having heaters
• F02C 3/04 - Gas-turbine plants characterised by the use of combustion products as the working fluid having a turbine driving a compressor
• F02G 1/00 - Hot gas positive-displacement engine plants
• B60K 16/00 - Arrangements in connection with power supply of propulsion units in vehicles from forces of nature, e.g. sun or wind
• B60L 8/00 - Electric propulsion with power supply from forces of nature, e.g. sun or wind

Abstract

2 outlets of the first decarburizing tower and the second decarburizing tower are both connected to a cold medium inlet of the waste heat exchanger; and a cold medium outlet of the waste heat exchanger is connected to a gasifying agent entrance of the gasifier.

IPC Classes  ?

• C10J 3/48 - ApparatusPlants
• C10J 3/72 - Other features
• C10J 3/82 - Gas withdrawal means
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• C10K 1/00 - Purifying combustible gases containing carbon monoxide
• C10K 1/02 - Dust removal
• C10K 1/08 - Purifying combustible gases containing carbon monoxide by washing with liquidsReviving the used wash liquors
• C10K 3/04 - Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by catalytic treatment reducing the carbon monoxide content

Abstract

An ultra high pressure cooling and purification process and apparatus for an oil production biomass syngas, the process comprising: (1) performing two-stage waste heat recovery and cyclone dust removal processing, with by-products of high pressure and low pressure steam, (2) removing a portion of heavy tar precipitated out from the biomass syngas by cooling in a second stage indirect heat exchange process, (3) further removing dust and lowering a temperature using a washing solution, (4) conducting deep removal of dust and coke using a moist air flow, and purging to remove remaining small amounts of dust and tar fog in the biomass syngas, and causing the pressure thereof to drop to 0.3-1 Mpa, so as to obtain a biomass syngas having respective dust and tar fog contents of less then 10 mg/Nm3, and a temperature of < 45°C. The apparatus is mainly comprised of an integrated heat exchange and dust removal device, a packed tower scrubber and a wet electrostatic precipitator. By optimizing process plan design and controlling appropriate process parameters, the invention realizes stepped cooling of a biomass syngas, stepped recovery of waste heat, and stepped dust removal, and achieves the object of tar removal and cooling and purification.

IPC Classes  ?

• C10J 3/84 - Gas withdrawal means with means for removing dust or tar from the gas
• C10K 1/10 - Purifying combustible gases containing carbon monoxide by washing with liquidsReviving the used wash liquors with aqueous liquids
• C10K 1/04 - Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
• C10K 1/02 - Dust removal

Abstract

Disclosed are a support for selective synthesis of a high-quality kerosene fraction from a synthesis gas, a catalyst thereof, and a preparation method therefor. The support consists of the following raw materials in parts by weight: 5-50 parts of mesoporous zirconia, 10-55 parts of a silicoaluminophosphate molecular sieve, 5-50 parts of modified Al-SBA-16, 1-3 parts of sesbania powder, and 10-70 parts of alumina. The catalyst consists of a soluble cobalt salt and the support, the soluble cobalt salt being loaded on the surface of the support. In the catalyst, cobalt oxide accounts for 5-20% by weight of the catalyst. The catalyst support provided in the present invention has moderate acidity and has a three-dimensional pore channel structure with large and uniform mesoporous pore channels and good mass transfer and diffusion effects, so that the generation of methane in the reaction process can be effectively reduced while improving the selectivity of kerosene fraction oil. In the present invention, a high-quality kerosene fraction is directly obtained from a synthesis gas with high selectivity by means of a Fischer-Tropsch synthesis reaction, thereby effectively resolving the prior-art problem of complex subsequent treatment processes after Fischer-Tropsch synthesis.

IPC Classes  ?

• B01J 32/00 - Catalyst carriers in general
• B01J 35/10 - Solids characterised by their surface properties or porosity
• B01J 29/85 - Silicoaluminophosphates [SAPO compounds]
• B01J 21/04 - Alumina
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• B01J 21/00 - Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium

Abstract

Provided are a chloralkali method and Fischer-Tropsch synthesis integrated utilization adjustment process and an equipment therefor. The process includes: 1) gasifying a gasification feedstock for the Fischer-Tropsch synthesis to obtain a crude synthesis gas with the main components being H2, CO and CO2; 2) electrolyzing a saturated NaCl solution by using a conventional industrial chloralkali method to obtain a NaOH solution, Cl2 and H2; and 3) using the NaOH solution and H2 prepared by the chloralkali method for removing CO2 in the crude synthesis gas to obtain a pure synthesis gas and adjusting the molar ratio of carbon to hydrogen in the pure synthesis gas, respectively, so that the pure synthesis gas reaches the requirements for a feeding gas of the Fischer-Tropsch synthesis. The equipment includes a gasification apparatus, a chloralkali method electrolyzer, a gas-washing apparatus and a Fischer-Tropsch synthesis reactor. By organically combining the chloralkali method and the Fischer-Tropsch synthesis process, and using the hydrogen gas produced by the chloralkali method to adjust the composition of the pure synthesis gas, the treating amount of the water-gas shift process is reduced and the working procedure is simplified.

IPC Classes  ?

• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• C01B 3/52 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquidsRegeneration of used liquids
• C01B 3/04 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of inorganic compounds, e.g. ammonia
• C10J 3/00 - Production of gases containing carbon monoxide and hydrogen, e.g. synthesis gas or town gas, from solid carbonaceous materials by partial oxidation processes involving oxygen or steam
• C10J 3/84 - Gas withdrawal means with means for removing dust or tar from the gas
• C10J 3/48 - ApparatusPlants

Abstract

Disclosed is a method for preparing a negative electrode material of a lithium-ion battery by using a biomass gasification furnace filter residue. The method comprises: 1) mixing a biomass gasification furnace filter residue with a surface active agent and grinding the mixture, grinding the mixture adequately, removing the surface active agent in a water washing manner, carrying out the suction filtration, and obtaining the filter residue for standby use; 2) placing hydrochloric acid into the filter residue obtained in step 1), adequately removing impurities, and filtering and washing the filter residue to be neutral for standby use; 3) placing the filter residue obtained in step 2) into a mixed solution of polyethyleneimine and ethanol, carrying out the oscillation, washing the polyethyleneimine and the ethanol after the adequate oscillation, performing the filtering, and obtaining the filter residue for standby use; and 4) placing nitric acid having a mass fraction of 55% to 70% into the filter residue obtained in step 3), adequately stirring at the temperature of 35 to 45 degrees centigrade, carrying out the modification, washing the nitric acid, and filtering and drying to obtain a negative electrode material of a lithium-ion battery. The negative electrode material of the lithium-ion battery, which has a high capacity, a high primary efficiency and good cycling performance and is safe and pollution-free, is obtained; the process is simple in process flow, low in cost and applicable to the expanded production.

IPC Classes  ?

• H01M 4/139 - Processes of manufacture
• H01M 4/1393 - Processes of manufacture of electrodes based on carbonaceous material, e.g. graphite-intercalation compounds or CFx
• H01M 4/1391 - Processes of manufacture of electrodes based on mixed oxides or hydroxides, or on mixtures of oxides or hydroxides, e.g. LiCoOx

Abstract

A catalyst for methanation of carbon dioxide, a method of preparing the catalyst, and a method of hydrogenating carbon dioxide in the presence of the catalyst in a fixed bed reactor are disclosed. The catalyst is formed by mixing ash from a biomass power plant with a nickel compound and calcining the resulting mixture. The catalyst formed by calcination includes between 2 and 20 wt. % of nickel supported on ash from combusting biomass.

IPC Classes  ?

• B01J 21/08 - Silica
• C07C 27/00 - Processes involving the simultaneous production of more than one class of oxygen-containing compounds
• C07C 1/12 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon dioxide with hydrogen
• B01J 21/18 - Carbon
• B01J 23/755 - Nickel
• B01J 37/08 - Heat treatment
• B01J 37/04 - Mixing

Abstract

Disclosed is a high-pressure pulverizer, which comprises a pulverizer body (1) and an electric motor (2). A high-pressure container (3) is arranged outside the pulverizer body (1). A sealed space is formed between the high-pressure container (3) and the pulverizer body (1). A feeding port (3a) is formed in an outer wall of an upper portion of the high-pressure container (3). The feeding port (3a) is in sealed communication with a feeding pipe of the pulverizer body (1) through a soft feeding joint (4). A discharging port (3b) is formed in an outer wall of a lower portion of the high-pressure container (3). The discharging port (3b) is in sealed communication with a discharging pipe of the pulverizer body (1) through a soft discharging joint (5). A bearing base (6) is arranged at the bottom of the high-pressure container (3). The pulverizer body (1) is mounted on the bearing base (6) through a shock pad (7). A connecting shaft (8) is movably inserted into the top of the high-pressure container (3) in a sealed manner. The upper end of the connecting shaft (8) is in transmission connection with an output shaft of the electric motor (2). The lower end of the connecting shaft is connected to a main shaft of the pulverizer body (1). When the pulverizer is operating, high-pressure inert media is provided in a sealed space between the pulverizer body (1) and the high-pressure container (3). The pressure of the inert media is greater than or equal to the pressure in the pulverizer body (1). The pulverizer is suitable for pulverizing materials such as coal and non-metallic ore.

IPC Classes  ?

• B02C 7/08 - Crushing or disintegrating by disc mills with coaxial discs with vertical axis

Abstract

A monolithic catalyst, including cobalt, a metal matrix, a molecular sieve membrane, and an additive. The metal matrix is silver, gold, copper, platinum, titanium, molybdenum, iron, tin, or an alloy thereof. The molecular sieve membrane is mesoporous silica SBA-16 which is disposed on the surface of the metal matrix and is a carrier of the active component and the additive. The thickness of the carrier is between 26 and 67 μm. The additive is lanthanum, zirconium, cerium, rhodium, platinum, rhenium, ruthenium, titanium, magnesium, calcium, strontium, or a mixture thereof. A method for preparing the monolithic catalyst is also provided.

IPC Classes  ?

• B01J 23/00 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group
• B01J 23/89 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with noble metals
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• B01J 37/02 - Impregnation, coating or precipitation
• B01J 29/03 - Catalysts comprising molecular sieves not having base-exchange properties
• B01J 35/04 - Foraminous structures, sieves, grids, honeycombs
• B01J 29/70 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of types characterised by their specific structure not provided for in groups
• B01J 37/06 - Washing
• B01J 37/34 - Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves
• B01J 35/02 - Solids

Abstract

Disclosed is an online furnace drying method for a heat-insulation natural gas catalytic oxidizing furnace, comprising: (1) simultaneously introducing oxygen, natural gas and temperature-control gas capable of decreasing a reaction heating rate into a natural gas catalytic oxidizing furnace, controlling a molar ratio of the oxygen to the natural gas at (0.3-0.6): 1, and meanwhile, controlling a molar ratio of the temperature-control gas to raw material gas consisting of the oxygen and the natural gas at (0.1-7):(1.3-1.6); (2) preheating the mixed gas so as to gradually increase the temperature, and stopping the preheating until the temperature reaches an oxidation triggering temperature; and (3) gradually decreasing the molar ratio of the temperature-control gas to the raw material gas, allowing the reaction temperature to increase at a heating rate meeting the requirement of a designed furnace drying curve, and stopping the introduction of the temperature-control gas until the reaction temperature reaches a working temperature. The present invention solves the problem that the temperature rises excessively fast during the furnace heating process, prevents a heat-insulation fire-resisting material from being cracked due to shock heating, and protects the natural gas catalytic oxidizing furnace, so that the natural gas catalytic oxidizing furnace can be stably transitioned to a normal operation state.

IPC Classes  ?

• C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts
• C01B 31/18 - Carbon monoxide

Abstract

A method of hydrofining a low-temperature Fischer-Tropsch distillate having a high-yield of middle distillates, the method comprising: dividing a low-temperature Fischer-Tropsch distillate having a high-yield of middle distillates into a light distillate, heavy distillate and middle distillate, and sequentially feeding the same into a first, second and third feed inlet of a hydrogenation reactor from an upper portion to a middle portion to perform a hydrofining process; respectively mixing a recycling hydrogen fed into a hydrogen inlet with three components in the hydrogenation reactor; and subsequently separating reaction products. The method maintains and controls a stable temperature of a refining reactor bed, reducing a feeding temperature of a heavy component, shortening a waiting time of a middle component, and reducing secondary cracking.

IPC Classes  ?

• C10G 45/72 - Controlling or regulating
• C10G 45/02 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing

Abstract

A diesel oil and jet fuel production system and method utilizing Fischer-Tropsch synthetic oil. The method comprises two parts, hydrofining and hydro-upgrading, and comprises the following steps: mixing a Fischer-Tropsch synthetic oil with hydrogen and introducing the same into a hydrofining reactor (A), and introducing a product thereof into a first fractionating tower (C); taking a cut naphtha fraction as an ethylene cracking raw material, and introducing a diesel fraction into a hydroisomerization reactor (E); introducing an unconverted oil into a hydrocracking reactor (D), mixing the products of the two reactors and then introducing the mixed products into a second fractionating tower (F) to obtain a jet fuel and diesel oil product, and circulating the unconverted oil to the hydrocracking reactor (D). The method can produce diesel oil, jet fuel and a hydrotreating wax oil product, has a simple technique, a stable process, low equipment investment, low costs, a long running period, and a high yield of diesel oil and jet fuel which can directly serve as fuel or blending components.

IPC Classes  ?

• C10G 67/00 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
• C10G 45/02 - Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbonsHydrofinishing
• C10G 47/00 - Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, to obtain lower boiling fractions

Abstract

The hydrotreatment method for a low-temperature Fischer-Tropsch synthesis product of the present invention comprises the following steps of: (1) firstly, mixing a Fischer-Tropsch wax with a sulfur-containing liquid catalyst in a certain proportion, then putting same into contact with hydrogen gas, then firstly feeding same into a first reaction region of a hydrogenation pretreatment catalyst, and then feeding the effluent of the first reaction region into a second reaction region filled with a hydrocracking catalyst and carrying out a hydrocracking reaction; (2) feeding a hydrocracking product of the second reaction region, together with a Fischer-Tropsch naphtha and diesel oil, into a third reaction region so as to come into contact with a hydrofining catalyst, and carrying out a hydrofining reaction; then feeding the effluent of the hydrofining reaction into a fourth reaction region so as to come into contact with a hydroisomerizing pour point depression catalyst, and carrying out a isomerizing pour point depression reaction; and (3) feeding the effluent of the fourth reaction region into a gas-liquid separation system C, wherein a hydrogen-rich gas is separated therefrom and recycled, and a liquid product is fed into a fractionation system D and separated so as to obtain naphtha, diesel oil and a tail oil, wherein the tail oil is circulated back to the second reaction region. By means of the present invention, the density of the synthesized diesel oil can be increased, the condensation point can be decreased, and the indexes for an automotive diesel oil can be achieved.

IPC Classes  ?

• C10G 67/02 - Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only

Abstract

A monodisperse transition metal nano-catalyst for Fischer-Tropsch synthesis and a preparation method therefor and an application thereof. The catalyst comprises transition metal. The transition metal is stably dispersed in an organic solvent in the form of monodisperse metal nanoparticles. The particle size of the transition metal is 1-100 nm. The specific surface area of the catalyst is 5-300 m2/g. The dispersity of the metal nanoparticles of the catalyst is high, and the catalyst can be directly applied to a Fischer-Tropsch synthesis reaction without filtering, cleaning, high-temperature roasting, and activated reduction.

IPC Classes  ?

• B01J 23/745 - Iron
• B01J 23/75 - Cobalt
• B01J 23/889 - Manganese, technetium or rhenium
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon

Abstract

Disclosed is a biomass pretreatment system suitable for entrained-flow bed gasification, comprising a coarse crusher, a dryer and a baking reactor, wherein the discharge port of the coarse crusher is connected to the charge port of the dryer, and the discharge port of the dryer is connected to the charge port of the baking reactor; the baking reactor comprises a reactor body, a rotary shaft, a driving component, at least one tower plate, a scraping plate and a baking medium input tube; the input end of the baking medium input tube respectively penetrates through and extends out of the reactor body; a bubbling hole is respectively provided on the disk surface of each tower plate; a tray with a fan-shaped notch is respectively provided between each tower plate and the corresponding baking medium input tube; the size and arranged position of the notch on the tray are matched with those of the notch on the corresponding tower plate; at least one wind cap in communication with the output end of the corresponding baking medium input tube is installed on the tray; and the wind outlet of the wind cap faces towards the corresponding tower plate. The system is suitable for biomass pretreatment.

IPC Classes  ?

• C10J 3/46 - Gasification of granular or pulverulent fuels in suspension
• C10J 3/72 - Other features
• F26B 9/06 - Machines or apparatus for drying solid materials or objects at rest or with only local agitationDomestic airing cupboards in stationary drums or chambers
• C10L 9/08 - Treating solid fuels to improve their combustion by heat treatment, e.g. calcining

Abstract

A blend combustion method of fuel coal fly ash for a biomass circulating fluidized bed boiler (9) and a device thereof. In the method, the fuel coal fly ash is jetted onto the bottom of a dense phase combustion zone (13) bed layer inside the biomass circulating fluidized bed boiler (9) so that the fuel coal fly ash is mixed with incandescent biomass bed materials in a bubble state or a turbulent fluidized state to generate intensive heat and mass transfer and temperature increase with violent rolling and friction, thereby abrading away ash shells on the external layer of the fuel coal fly ash to expose unburned residual carbon black core therein, and finally the fuel coal fly ash is completely combusted in the dense phase combustion zone (13) and a dilute phase combustion zone (14). The device is mainly composed of a fuel coal fly ash storage bin (1), a rotary material feeding device (2), an ejector (3), an air blower (5), a transporting pipeline (6), a bottom feeding abrasion resistant spray nozzle (8) and so on, which are used with the biomass circulating fluidized bed boiler (9). By means of the device, the fuel coal fly ash can be recycled into the biomass circulating fluidized bed boiler (9) for fully combustion again to perform secondary power generation, thereby effectively reducing the amount of a biomass fuel, increasing the power generation capacity of unit fuel, and can reduce emission of coal combustion pollutant.

IPC Classes  ?

• F23C 10/00 - Apparatus in which combustion takes place in a fluidised bed of fuel or other particles
• F23C 10/22 - Fuel feeders specially adapted for fluidised bed combustion apparatus

Abstract

Disclosed are a cobalt-based Fischer-Tropsch synthesis catalyst and a preparation method and the use thereof. The catalyst is comprised of an active component Co and a carrier Al2O3-SiO2 composite aerogel, wherein on the basis of the total amount of the catalyst, the content of Co is 2%-10 wt%, and the content of Al2O3-SiO2 composite aerogel is 90%-98%; the specific surface area of the catalyst is 250-750m2/g; the average pore size is 9-28.6 nm; and the pore volume is 2.75-4.23 mL/g. The preparation method for the catalyst comprises: (1) preparing a Al2O3 sol; (2) preparing a SiO2 sol; and (3) preparing a Co/Al2O3-SiO2 composite aerogel. The catalyst has a high specific surface area and a large pore size due to a three-dimensional pore system; the active components are homogeneously dispersed into the pores, which not only prevents the agglomeration of metal particles but also facilitates the diffusion of the reactants and products, such that the catalyst can be applied to Fischer-Tropsch synthesis very well.

IPC Classes  ?

• B01J 21/12 - Silica and alumina
• B01J 23/75 - Cobalt
• B01J 35/10 - Solids characterised by their surface properties or porosity
• B01J 37/00 - Processes, in general, for preparing catalystsProcesses, in general, for activation of catalysts
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon

Abstract

A gasification system for producing synthetic gas from biomass, including: a biomass material pre-processing part; a pyrolysis part; a condensing part; and a gasification part. The pyrolysis part includes a pyrolysis bed and a combustion bed. The condensate tank of the condensing part is connected to a non-condensable pyrolysis gas compressor via a pipeline; an output of the non-condensable pyrolysis gas compressor is connected to the pyrolysis bed and the combustion bed. The non-condensable pyrolysis gas acts as a fuel of the combustion bed and a fluidizing medium of the pyrolysis bed.

IPC Classes  ?

• C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
• C10B 49/22 - Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique
• C10K 1/02 - Dust removal
• C10K 1/04 - Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
• C10K 1/06 - Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials combined with spraying with water
• C10C 5/00 - Production of pyroligneous acid
• C01B 3/22 - Production of hydrogen or of gaseous mixtures containing hydrogen by decomposition of gaseous or liquid organic compounds

Abstract

−1, a temperature of between 380 and 700° C., and a pressure between 0.1 and 0.8 megapascal.

IPC Classes  ?

• C10G 33/04 - De-watering or demulsification of hydrocarbon oils with chemical means
• C10G 3/00 - Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
• C10G 11/18 - Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised bed" technique
• B01D 17/04 - Breaking emulsions
• B01J 29/08 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the faujasite type, e.g. type X or Y
• C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
• C10L 1/02 - Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
• B01J 29/40 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11

Abstract

Disclosed are a catalyst suitable for production of aviation kerosene from biomass Fischer-Tropsch synthesis oil and a preparation method therefor. Various components by weight in percentage in the catalyst are: 20-50% of an amorphous aluminium-silicon, 5-20% of an aluminium oxide binder, 20-60% of a hydrothermally modified ZSM-22 molecular sieve, 0.5-5% of nickel oxide, and 5-15% of molybdenum oxide. The preparation method is as follows: firstly performing an NH4+ exchange treatment on the K-ZSM-22 molecular sieve to obtain an H-ZSM-22 molecular sieve, then performing a hydrothermal treatment to obtain a modified H-ZSM-22 molecular sieve, and then after uniform mixing with the amorphous aluminium-silicon, adding the aluminium oxide binder and a sesbania powder, mixing and kneading same, grinding into clusters, forming same by band extrusion, then drying and calcinating same, and finally loading active metals Ni and Mo. The catalyst obtained from the present invention has a high activity and a high selectivity, increases the isomerization degree of long-chain alkanes, reduces the freezing points of the fractions of aviation kerosene, and improves the yield of the aviation kerosene.

IPC Classes  ?

• B01J 29/48 - Crystalline aluminosilicate zeolitesIsomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11 containing arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
• B01J 37/02 - Impregnation, coating or precipitation
• C10G 49/04 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or characterised by the catalyst used containing nickel, cobalt, chromium, molybdenum, or tungsten metals, or compounds thereof
• C10G 49/08 - Treatment of hydrocarbon oils, in the presence of hydrogen or hydrogen-generating compounds, not provided for in a single one of groups , , , , or characterised by the catalyst used containing crystalline alumino-silicates, e.g. molecular sieves

Abstract

A structured iron-based catalyst for producing an α-olefin from a synthesis gas and a preparation method and use. The catalyst comprises an active component iron, auxiliary agents and a carrier, wherein the auxiliary agents comprise a first auxiliary agent which is a transition metal or a transition metal oxide and a second auxiliary agent which is a metal oxide. The content of the active component iron is 50.0%-99.8%, the content of the first auxiliary agent is 0-5.0%, the content of the second auxiliary agent is 0-10% and the balance is the carrier which is silicon dioxide. A precursor of the active component iron, a precursor of the first auxiliary agent and the carrier silicon dioxide are made into mono-dispersed particles using a heat dispersing method, and then impregnated with a solution of a precursor of the second auxiliary agent to obtain the structured iron-based catalyst. The above-mentioned structured iron-based catalyst is used for producing an α-olefin from a synthesis gas. Since the mono-dispersed structured iron-based catalyst can generate an active centre suitable for the generation of the α-olefin, it thus has good selectivity.

IPC Classes  ?

• B01J 23/745 - Iron
• B01J 23/83 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with rare earths or actinides
• B01J 23/889 - Manganese, technetium or rhenium
• B01J 23/75 - Cobalt
• B01J 23/86 - Chromium
• B01J 23/80 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with zinc, cadmium or mercury
• B01J 23/89 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with noble metals
• B01J 23/78 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with alkali- or alkaline earth metals or beryllium
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon

Abstract

A cobalt-based Fischer-Tropsch synthesis catalyst coated with mesoporous materials and preparation method therefor are disclosed. The catalyst comprises a silica carrier surface-loaded with an active component of cobalt and a selective promoter of zirconium; the outside of the active component of cobalt and the selective promoter of zirconium is coated with a mesoporous material shell layer. The preparation method comprises preparing silica carrier loaded with zirconium, preparing an initial cobalt-based Fischer-Tropsch synthesis catalyst on the silica carrier base, formulating a precursor solution of mesoporous materials, then dipping, crystallizing, washing, drying and calcining to obtain the cobalt-based Fischer-Tropsch synthesis catalyst coated with mesoporous materials. The active component is coated and protected by the mesoporous material shell layer, the thickness of the shell layer is controllable, the catalyst has long service life, high reactivity and good stability. The pore structure of mesoporous materials provides a channel for diffusing CO and H2, the selectivity of C5+ is high and the selectivity of methane is low. The catalyst is specially applicable to slurry bubble column reactors or continuously stirred tank reactors.

IPC Classes  ?

• B01J 23/75 - Cobalt
• B01J 35/10 - Solids characterised by their surface properties or porosity
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon

Abstract

A solar thermal and BIGCC-integrated hybrid power generation system comprising a solar energy concentrating collector system (9), biomass gasification equipment (1), a gas-fired electric generator (7), a steam turbine (13), and a steam electric generator (14). The solar energy concentrating collector system (9) is connected to a solar energy heat exchange system (11). The biomass gasification equipment (1) is connected to the gas-fired electric generator (7) via a gas compressor (3), a combustion chamber (5), and a gas turbine (6). An output of the gas turbine (6) is simultaneously connected to a gas residual heat system (8). A low-pressure steam output of the gas residual system (8) is connected to a medium/low-pressure cylinder of the steam turbine (13). A high-pressure steam output of the gas residual system (8) and high-pressure steam produced by the solar energy heat exchange system (11) are both connected to a steam mixture regulating system (12). An output of the steam mixture regulating system (12) is connected to a high-pressure cylinder of the steam turbine (13). By means of the steam mixture regulating system, mixture of steams of different temperatures is implemented, and the temperature of the mixed steam is regulated and controlled, thus satisfying steam requirements of a variable parameter steam turbine.

IPC Classes  ?

• F02C 6/00 - Plural gas-turbine plantsCombinations of gas-turbine plants with other apparatusAdaptations of gas-turbine plants for special use
• F03G 6/02 - Devices for producing mechanical power from solar energy using a single state working fluid
• F01K 27/00 - Plants for converting heat or fluid energy into mechanical energy, not otherwise provided for

Abstract

An optimized integrated system for solar-biomass hybrid electricity generation. A heat transfer oil outputted from a solar farm (1 and 2) of a solar thermal boiler system flows sequentially through a solar thermal evaporator (6) and a solar thermal heater (5) then back to a heat transfer oil storage tank (4) and is then delivered via a circulation oil pump (3) to the solar farm to complete a heat transfer oil circulation. Solar thermal steam produced by the solar thermal evaporator is delivered to a biomass boiler system (9) via a steam header (7). Auxiliary steam produced by a coal-fired or gas-fired or oil-fired auxiliary boiler (8) also is mixed with the solar thermal steam and delivered to the biomass boiler system via the steam header. The solar thermal mixed steam and steam produced by a biomass boiler itself are delivered to a turbo generator (10) to drive an electric generator (11) into generating electricity. The system simplifies solar thermal power generation system and equipment configurations, provides stable electricity generation, high thermal efficiency, and extended service life.

IPC Classes  ?

• F01K 11/02 - Steam engine plants characterised by the engines being structurally combined with boilers or condensers the engines being turbines
• F03G 7/00 - Mechanical-power-producing mechanisms, not otherwise provided for or using energy sources not otherwise provided for
• F03G 6/06 - Devices for producing mechanical power from solar energy with solar energy concentrating means
• F01D 15/10 - Adaptations for driving, or combinations with, electric generators

Abstract

Provided is a device for high-density continuous culture of microalgae, the device comprising a photobioreactor circulating unit, a nutrient solution feeding unit, a ventilated carbon supplementing unit and a microalgae harvesting unit. Also provided is a method for conducting high-density continuous culture of microalgae using the device.

IPC Classes  ?

• C12M 1/00 - Apparatus for enzymology or microbiology
• C12N 1/12 - Unicellular algaeCulture media therefor

Abstract

Provided are a metal-matrix integrated membrane catalyst for Fischer-Tropsch (F-T) synthesis, and preparation method thereof. The catalyst consists of a metallic integrated matrix, a molecular sieve membrane carrier, an active component Co and other adjuvants. The method comprises: pre-treating the metallic integrated matrix, and conducting in-situ growth of an SBA-16 molecular sieve membrane carrier, the thickness of the molecular sieve membrane carrier being 26-67 μm; and then loading the active component Co and other adjuvants on the molecular sieve membrane carrier via an impregnation method. The method of preparing the metal-matrix integrated membrane catalyst for the F-T synthesis comprises the following steps: pre-treating the metal-matrix; 2) pre-establishing well-chosen seed; 3) placing the pre-treated metallic integrated matrix in the SBA-16 molecular sieve synthesized solution, and conducting in-situ growth of the molecular sieve membrane carrier on the metallic integrated matrix; 4) impregnating, aging and calcinating the active component and adjuvant element; impregnating the metallic integrated matrix having the in-situ grown SBA-16 molecular sieve into the saline solution of the active component Co and other adjuvants, drying, aging, calcinating, and cooling to room temperature. The formed molecular sieve membrane has mechanical pressure resistance, and better firmness.

IPC Classes  ?

• B01J 29/03 - Catalysts comprising molecular sieves not having base-exchange properties
• B01J 35/10 - Solids characterised by their surface properties or porosity
• B01J 23/75 - Cobalt
• B01J 23/02 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the alkali- or alkaline earth metals or beryllium
• B01J 23/10 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of rare earths
• B01J 23/42 - Platinum
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon

Abstract

Provided is a process for the coupling pressurized pyrolysis of biomasses, which pyrolyses the biomasses using microwaves coupled with plasmas, and treats the carbon residues after the pyrolysis using plasmas. The method has a high efficiency, and a high carbon conversion. The synthetic gas has a good quality and the volume of the effective gas reaches above 90%. Also provided is a pyrolyzing furnace for the above-mentioned pyrolysis process, which includes a pyrolysis furnace (2), a feeding system, a cyclone separator (4). The lower part of the pyrolyzing furnace is provided with multiple microwave inlets (12) and a plasma torch (13) interface, and the bottom thereof is provided with a slag storage pool. Both the microwave inlets (12) and the plasma torch (13) interface of the pyrolyzing furnace are distributed in multiple layers with each layer being placed at a uniform distance. The plasma torch (13) interface is placed below the microwave inlets (12) and above the level of the liquid in the slag storage pool and the jet direction of the plasma at the plasma torch (13) interface is in the range of a microwave field at the microwave inlets. The thus resultant synthetic gas is free of tar, and the subsequent purification process is simple, without environmental pollution.

IPC Classes  ?

• C10B 23/00 - Other methods of heating coke ovens
• C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material

Abstract

2 catalyst, cooling the calcined material to room temperature, and grinding it to yield a powder; 2) heating the powder in a fluidized bed reactor; 3) adding the heated powder into excess dilute nitric acid solution and filtering to obtain a cobalt nitrate solution; 4) adjusting the pH value of the cobalt nitrate solution to 1.5, adding a preheated oxalic acid solution, adjusting a pH value of the resulting solution to 1.5, immediately filtering the resulting solution to yield a precipitate of cobalt oxalate, washing the precipitate of cobalt oxalate to yield a neutral filtrate; 5) drying the precipitate and calcining to yield cobalt oxide; 6) dissolving the cobalt oxide in nitric acid to yield a second cobalt nitrate solution; and 7) evaporating the second cobalt nitrate solution to obtain crystalline cobalt nitrate.

IPC Classes  ?

• C22B 3/00 - Extraction of metal compounds from ores or concentrates by wet processes
• C22B 3/32 - Carboxylic acids

Abstract

A high-temperature high-pressure biomass syngas cooling and purification process comprises: 1) subsection cooling; 2) collecting and eliminating empyreumatic oil; 3) washing and purification; and 4) wet-type electrostatic precipitation processing. Also provided is a high-temperature high-pressure biomass syngas cooling and purification device, mainly comprising a shell-and-tube heat recovery boiler (2), a dry-gas filter (3), a vertical smoke-tube heat recovery boiler (4), a venture washing tower (5), and a wet-type electrostatic precipitator (6). The device of the present invention is simple, safe and stable; has low power consumption and high efficiency, and achieves good economic benefits.

IPC Classes  ?

• C10K 1/00 - Purifying combustible gases containing carbon monoxide
• C10K 1/02 - Dust removal
• C10K 1/04 - Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials

Abstract

Provided is a method for modifying a biomass pyrolysis oil, which specifically comprises the following steps: a first step of demulsification, layering, and dehydration: adding an inorganic salt ion and an organic demulsifier into the biomass pyrolysis oil, wherein the mass ratio of the inorganic salt to the biomass pyrolysis oil is 1:2000-1:800, the mass ratio of the organic demulsifier to the biomass pyrolysis oil is 1:4000-1:1000, after mixing sufficiently, standing and taking the upper layer of biomass pyrolysis oil; a second step of performing a catalytic cracking modification on the biomass pyrolysis oil: using a modified catalyst: 1) modifying a catalyst: performing an ageing treatment on a carclazyte catalyst supported on a zeolite molecular sieve for 2-8 h with 100% water vapour under the condition of 500-800°C; and 2) placing the aged catalyst into a reactor, injecting the biomass pyrolysis oil into the reactor filled with the catalyst, with a catalyst-to-oil ratio of 1:3-16, and performing a catalytic cracking modification on the biomass pyrolysis oil under the conditions of a mass airspeed of 6-15 h-1, a reaction temperature of 380-700°C and a reaction pressure of 0.1-0.8 Mpa.

IPC Classes  ?

• C10G 55/06 - Treatment of hydrocarbon oils, in the absence of hydrogen, by at least one refining process and at least one cracking process plural serial stages only including at least one catalytic cracking step

Abstract

A Fischer-Tropsch synthesis catalyst for syngas to low carbon olefins, the modified molecular sieve carrier and preparation method thereof. The Fischer-Tropsch catalyst components are molecular sieve carrier and active components, the molecular sieve is Ce salt and/or Pr salt modified Si-Al molecular sieve and/or high-Si molecular sieve carrier. The active component comprises main component of Fe, further Mn and Cu as well as alkaline assistants. The content of modified molecular sieve is 40%-80 wt%. The weight content of Ce salt and/or Pr salt is 1%-20% of that of the molecular sieve. The Ce salt and/or Pr salt modified molecular sieve is prepared by treating Si-Al molecular sieve and/or high-Si molecular sieve with acid solution to obtain H-type molecular sieve, impregnating the H-type molecular sieve in Ce salt solution and/or Pr salt solution, then drying and calcining. The Fischer-Tropsch synthesis catalyst for syngas to low carbon olefins is obtained by impregnating the Ce salt and/or Pr salt modified molecular sieve in the salt solution of active components, then drying and calcining.

IPC Classes  ?

• B01J 23/10 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of rare earths
• B01J 29/00 - Catalysts comprising molecular sieves
• B01J 23/02 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the alkali- or alkaline earth metals or beryllium
• B01J 23/16 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of arsenic, antimony, bismuth, vanadium, niobium, tantalum, polonium, chromium, molybdenum, tungsten, manganese, technetium or rhenium
• B01J 23/72 - Copper
• B01J 23/745 - Iron

Abstract

Solar and steam hybrid power generation system including a solar steam generator, an external steam regulator, a turboset, and a power generator. A steam outlet end of the solar steam generator is connected to a steam inlet of the turboset. A steam outlet end of the external steam regulator is connected to the steam inlet of the turboset. A steam outlet of the turboset is connected to the input end of a condenser, and the output end of the condenser is connected to the input end of a deaerator. The output end of the deaerator is connected to the input end of a water feed pump. The output end of the water feed pump is connected to a circulating water input end of the solar steam generator. The output end of the water feed pump is connected to a water-return bypass of the external steam.

IPC Classes  ?

• F01D 21/00 - Shutting-down of machines or engines, e.g. in emergencyRegulating, controlling, or safety means not otherwise provided for
• F01D 19/00 - Starting of machines or enginesRegulating, controlling, or safety means in connection therewith
• F01D 17/00 - Regulating or controlling by varying flow
• F03G 6/00 - Devices for producing mechanical power from solar energy
• F01D 17/04 - Arrangement of sensing elements responsive to load
• F01D 17/02 - Arrangement of sensing elements
• F01D 17/08 - Arrangement of sensing elements responsive to condition of working fluid, e.g. pressure
• F01K 11/02 - Steam engine plants characterised by the engines being structurally combined with boilers or condensers the engines being turbines
• F24J 2/07 - Receivers working at high temperature, e.g. for solar power plants
• F22B 1/00 - Methods of steam generation characterised by form of heating method
• F01D 19/02 - Starting of machines or enginesRegulating, controlling, or safety means in connection therewith dependent on temperature of component parts, e.g. of turbine casing
• F01D 17/06 - Arrangement of sensing elements responsive to speed
• F03G 6/06 - Devices for producing mechanical power from solar energy with solar energy concentrating means

Abstract

A comprehensive treatment process and apparatus for solid fuel power station wastes; conditioned seawater containing metal ions of Na+, K+, Ca2+ and Mg2+ is electrolyzed to generate alkaline substances and acid gas, the alkaline substances are used to absorb carbon dioxide in the emitted flue gas of the power station, and the carbon dioxide is treated to be harmless and then discharged into the sea for storage; the acid gas is used to synthesize hydrochloric acid, and the hydrochloric acid is used for a dissolution replacement reaction with the coal ash, biomass ash or cheap silicate mineral powder discharged by the power station; the isolated dissolved solution containing the ions of Na+, K+, Ca2+, Mg2+ and Cl- is recycled and returned to the conditioned seawater for further electrolysis; and the isolated SiO2 is utilized as an industrial raw material, thus forming a beneficial cycle of the comprehensive treatment of the power station waste. The apparatus mainly comprises an electrolysis device (2), a carbon dioxide absorption column (5), a hydrogen chloride synthesis column (20), a silicate reactor (10), a cyclone separator (14), and a vacuum belt conveyer (13).

IPC Classes  ?

• B01D 53/62 - Carbon oxides
• B01D 53/78 - Liquid phase processes with gas-liquid contact
• C01B 33/143 - Preparation of hydrosols or aqueous dispersions by acidic treatment of silicates of aqueous solutions of silicates
• B09B 3/00 - Destroying solid waste or transforming solid waste into something useful or harmless

Abstract

Provided is a high-capacity macromolecular polymer hydrogen storage material, comprising a linear macromolecular polymer as a main chain, and a borane ammonia derivative grafted on the side chain and/or end of the linear macromolecular polymer after a side-chain group and/or end group of the linear macromolecular polymer is aminated by a polyamine compound and reacts with a borohydride. Also provided is a preparation method for the high-capacity macromolecular polymer hydrogen storage material.

IPC Classes  ?

• C01B 3/02 - Production of hydrogen or of gaseous mixtures containing hydrogen

Abstract

Disclosed are a method and a device for biomass gasification by cycling of carbon dioxide without oxygen. Concretely the method and the device are integrated, wherein carbon dioxide is used as the only gasifying agent for gasifying biomass and other solid fuels into high-quality synthesis gas, the carbon dioxide in the synthetic gases is recovered, and the carbon dioxide produced in the succeeding process using the synthetic gases is recycled for gasification. The purpose of zero emission of carbon dioxide of the whole system is achieved. The advantages of no oxygen consumption, the production of high-quality synthesis gas, high cold gas efficiency and simple operation are achieved. Zero emission of carbon dioxide of the whole system is achieved.

IPC Classes  ?

• C10J 3/00 - Production of gases containing carbon monoxide and hydrogen, e.g. synthesis gas or town gas, from solid carbonaceous materials by partial oxidation processes involving oxygen or steam
• C10K 3/00 - Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide

Abstract

Disclosed is a process for comprehensively utilizing low carbon emission Fischer-Tropsch synthesis tail gas. In the process, a non-cycling tail gas generated after a Fischer-Tropsch synthesis reaction is steam reformed and converted into a hydrogen-rich synthesis gas, and then highly purified hydrogen is separated and extracted from the hydrogen-rich synthesis gas for use. The process comprises the following steps: 1) conducting a steam conversion reaction to obtain converted gas; 2) conducting a Fischer-Tropsch synthesis reaction to obtain a hydrocarbon fuel; 3) after a pre-reforming reaction, converting a hydrocarbon compound containing two or more carbon atoms into methane; 4) conducting a reforming reaction to convert the methane and steam into hydrogen and carbon monoxide; 5) separating the hydrogen and carbon monoxide from the gas; and 6) providing heat for a reforming reactor. The present invention effectively utilizes the Fischer-Tropsch synthesis tail gas, especially a tail gas containing a large amount of inert constituents, and converts the tail gas into the hydrogen for use. Furthermore, the present invention effectively utilizes the residual combustible constituents in the reformed gas after the hydrogen is separated, thus improving energy utilization efficiency.

IPC Classes  ?

• C01B 3/38 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using catalysts

Abstract

Provided in the present invention is a method for a Fischer-Tropsch synthesis and for utilizing an exhaust with the steps of: after transformation and purification, introducing a Fischer-Tropsch synthesis raw material gas into a Fischer-Tropsch synthesis reactor, where the operating conditions for the Fischer-Tropsch synthesis are a temperature between 150°C and 300°C and a pressure between 2 and 4 MPa(A), using an iron-based or cobalt-based catalyst in a Fischer-Tropsch reaction to produce a liquid hydrocarbon product; 2) introducing a Fischer-Tropsch synthesis exhaust produced in step 1) into a pressure swing adsorption hydrogen-separation apparatus, extracting hydrogen gas from the Fischer-Tropsch synthesis exhaust, where the purity of the hydrogen gas is controlled between 80% and 99%; 3) using the pressure swing adsorption apparatus to extract methane from the exhaust in step 2), where the purity of the methane is controlled between 80% and 95%; step 4) sending a portion of the hydrogen extracted by pressure swing adsorption in step 2) to be mixed with the Fischer-Tropsch synthesis raw material gas, and, after transformation and purification, to be used for adjusting the hydrogen-carbon ratio of the Fischer-Tropsch synthesis raw material gas; 5) introducing the methane produced in step 3) into a methane reforming process for a reforming reaction, producing a synthetic gas of a high hydrogen-to-carbon ratio, then sending to step 1) to be mixed with the Fischer-Tropsch raw material gas and be used to adjust the hydrogen-carbon ratio of the Fischer-Tropsch raw material gas.

IPC Classes  ?

• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• B01D 53/047 - Pressure swing adsorption
• C07C 9/04 - Methane
• C07C 7/12 - Purification, separation or stabilisation of hydrocarbonsUse of additives by adsorption, i.e. purification or separation of hydrocarbons with the aid of solids, e.g. with ion-exchangers
• C01B 3/50 - Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification

Abstract

Provided in a method for preparing a liquid hydrocarbon product from a biomass-produced synthetic gas, specific steps are as follows: 1) mixing a crude synthetic gas produced by a reaction in a biomass gasifier with a hydrogen-rich gas, where the volume ratio of the hydrogen-rich gas to the crude synthetic gas is between 0.7 and 2.1; 2) feeding the gaseous mixture acquired in step 1) into a dehydration apparatus to remove the moisture, carbon dioxide, and other hazardous impurities contained in the gas, acquiring a synthetic gas meeting the requirement of a Fischer-Tropsch synthesis reaction; 3) reacting the synthetic gas acquired in step 2) into a Fischer-Tropsch synthesis reactor, where the Fischer-Tropsch synthesis is a process catalyzed with a high efficieny Fischer-Tropsch synthesis catalyst to produce the liquid hydrocarbon product, where the temperature is between 150°C and 300°C, and where the pressure is usually between 2 and 4 MPa(A), producing the liquid hydrocarbon product, and discharging water generated from the apparatus, where the volume ratio of H2/CO of the Fischer-Tropsch synthesis raw material gas introduced into the Fischer-Tropsch synthesis reactor is between 1.8 and 3.0, and where the H2+CO of the effective synthetic gas accounts for 50% to 99% of the total gaseous volume; and, 4) returning 70% to 95% of a discharged exhaust produced in step 3) to step 3) to be mixed with the synthetic gas and then be reacted in the Fischer-Tropsch synthesis reactor.

IPC Classes  ?

• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• C07C 1/04 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon monoxide with hydrogen

Abstract

A liquid phase CO2 methanation catalyst comprises amphipathic ionic liquid and metal active components dispersed in the amphipathic ionic liquid. The metal active components are in the state of stable colloid in the amphipathic ionic liquid, particle size is 0.5 to 20nm, and are in the shape of spherical. The metal active components include a first metal active component and a second metal active component. The first metal active component is nickel, the second metal active component is one or more of lanthanum, cerium, molybdenum, ruthenium, ytterbium, rhodium, palladium, platinum, potassium and magnesium, and the molar ratio of the first metal active component to the second metal active component is 10:0.1-2. Also provided are a preparation method of the liquid phase CO2 methanation catalyst and a use for CO2 methanation thereof.

IPC Classes  ?

• B01J 31/02 - Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
• B01J 31/06 - Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing polymers
• C07C 9/04 - Methane
• C07C 1/12 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon dioxide with hydrogen

Abstract

Disclosed is a method for preparing nanosilicon dioxide with a modified surface from rice hull, comprising the steps of: pre-treating rice hull with a treating gas containing CO2 to remove metal ions, impurities and dirt, drying and grinding; soaking for 4-8 hours in a diluted solution of phosphoric acid, boric acid, hydrochloric acid, formic acid, acetic acid, propionic acid, butyric acid, or a salt of a strong acid and a weak base with a concentration of 0.05-0.5 mol/L,the soaking temperature being no higher than 10°C, filtering by suction, removing the filtrate, and drying; and baking under anaerobic conditions at 300°C-450°C, so as to obtain the nanosilicon dioxide with a modified surface. The product has a particle size of 60-200 nm, an oil absorption value of 1.00-2.50 mL/g, a surface contact angle to water > 128°, and a BET specific surface area of 60-120 m2/g.

IPC Classes  ?

• C01B 33/18 - Preparation of finely divided silica neither in sol nor in gel formAfter-treatment thereof
• B82Y 30/00 - Nanotechnology for materials or surface science, e.g. nanocomposites

Abstract

A process for converting carbon dioxide in flue gas into natural gas by using dump power energy. The process uses the dump power energy to electrolyze water to generate hydrogen gas; the hydrogen gas and carbon dioxide captured from industrial flue gas are subjected to a methanation reaction; heat generated from the methanation reaction is used to heat water to generate superheated water vapor for driving a steam turbogenerator to generate power for supplementing power energy for electrolyzing water, and thus natural gas is obtained by synthesizing. Equipment used in synthesized natural gas is further provided. The equipment is mainly formed by combining a transforming and rectifying device (1), an electrolytic bath (2), a steam turbogenerator (4), a carbon dioxide heater (21), at least two-stage of fixed bed reactors (11, 13), various indirect heat exchangers, a steam drum (12), a natural gas condenser (8), and a process water pipeline (3).

IPC Classes  ?

• C10L 3/06 - Natural gasSynthetic natural gas obtained by processes not covered by , or
• C10L 3/08 - Production of synthetic natural gas
• C07C 1/12 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon dioxide with hydrogen
• C07C 9/04 - Methane

Abstract

A method for preparing high-temperature, active particle-containing steam. The method includes: 1) preparing steam; selecting one or several non-oxidizing gases as a working gas; ionizing the working gas into a plasma working medium by using a plasma generator; and 2) injecting the plasma working medium into a high-temperature steam generator to form high-temperature ionized environment while introducing the steam into the high-temperature steam generator for allowing the steam to contact with the plasma working medium so that the steam is heated and activated to form active particle-containing steam. A device for preparing the high-temperature, active particle-containing steam is also provided.

IPC Classes  ?

• B01J 12/00 - Chemical processes in general for reacting gaseous media with gaseous mediaApparatus specially adapted therefor
• C10J 3/00 - Production of gases containing carbon monoxide and hydrogen, e.g. synthesis gas or town gas, from solid carbonaceous materials by partial oxidation processes involving oxygen or steam
• B01J 19/08 - Processes employing the direct application of electric or wave energy, or particle radiationApparatus therefor

Abstract

A method for recovering ruthenium from waste catalyst of aluminum oxide loaded with ruthenium comprises the following steps: drying, roasting and cooling the waste catalyst of aluminum oxide loaded with ruthenium; grinding into black powder containing ruthenium oxide; placing the black powder into a fluid bed reactor, introducing hydrogen and performing reduction reaction, thereby obtaining metal Ru; introducing a mixed gas of oxygen and ozone into the fluid bed reactor and oxidizing the waste catalyst, thereby obtaining RuO4 gas; introducing the RuO4 gas into sufficient hydrochloric solution to dissolve the RuO4 gas, thereby obtaining an H3RuC16 solution; adding excessive oxidant into the H3RuC16 solution and promoting the H3RuC16 to be fully oxidized, thereby generating hexachloro (IV) ruthenium acid; adding excessive NH4Cl, reacting, filtering and cleaning filter cake, thereby obtaining an ammonium hexachloro (IV) ruthenium solid; and finally, performing hydrogen reduction treatment on the ammonium hexachloro (IV) ruthenium solid, thereby obtaining the metal ruthenium. The method is simple in operation, low in cost, short in recovering period and high in recovery ratio.

IPC Classes  ?

• C22B 7/00 - Working-up raw materials other than ores, e.g. scrap, to produce non-ferrous metals or compounds thereof
• C22B 11/00 - Obtaining noble metals

Abstract

Provided is a method for preparing high-purity cobalt nitrate crystals from Co/SiO2 waste catalysts. The method sequentially comprises the following steps: 1) calcining Co/SiO2 waste catalysts to be treated at 350 to 500 ℃ under the existence of air for 3 to 6 hours, grinding the Co/SiO2 waste catalysts into powder after cooling to the room temperature; 2) transferring the waste catalyst powder into a fluidized bed reactor and taking reduction reaction for 8 to 12 hours in mixed gas of H2 and N2; 3) adding the waste catalysts after the reduction reaction into excessive dilute nitric acid solution to be fully dissolved and filtering; 4) using alkali liquid for regulating the pH value of the obtained cobalt nitrate solution to 1.5, adding oxalic acid solution for reaction in the water bath of 25 to 80 ℃, regulating the pH value of the reacted solution to 1.5 by diluted alkali solution and filtering the hot solution to obtain cobalt oxalate precipitates; 5) after drying the cobalt oxalate precipitates, roasting the dried cobalt oxalate precipitates at the temperature of 550 to 650 ℃ for 4 to 8 hours; 6) dissolving the obtained cobalt oxide by dilute nitric acid solution and 7) evaporating and crystallizing the cobalt nitrate solution to obtain Co(NO3)2·6H2O crystals. The recovery rate and the purity of the Co(NO3)2·6H2O in the method are high.

IPC Classes  ?

• C01G 51/00 - Compounds of cobalt
• B09B 3/00 - Destroying solid waste or transforming solid waste into something useful or harmless

Abstract

A solar energy and methane energy complementary power generation apparatus comprises solar energy heat collection devices (13, 14), a methane storage tank (19), a methane boiler (10), a turboset (2) and a generator (1). A methane combustor (16), a steam superheater (11) and a feed-water preheater (12) are arranged in the methane boiler; the solar energy heat collection devices (13, 14) and the methane combustor (16) can heat steam in the steam superheater (11) simultaneously or separately; an output end of the steam superheater (11) is connected to a high-pressure steam inlet (3) of the turboset (2); a lower-pressure steam outlet (4) of the turboset (2) is connected to the feed-water preheater (12) through a condenser (5), a deaerator (6) and a water feed pump (7) in turn; circulating water output from the feed-water preheater (12) is returned to the steam superheater (11) after being heated by the solar energy heat collection devices (13, 14). This apparatus does not discharge sulfur dioxide or carbon dioxide, can stabilize impact of weather fluctuation on the solar energy and can conveniently change the operating mode of the turboset; therefore, the generator can generate power 24 hours all the day from daytime to nighttime, no matter the weather is sunny or overcast.

IPC Classes  ?

• F03G 6/06 - Devices for producing mechanical power from solar energy with solar energy concentrating means

Abstract

A solar energy and external source steam complementary power generation apparatus comprising a solar steam generation device, an external source steam regulator (15), a turboset (2) and a generator (1). A steam output end of the solar steam generation device is connected to a high-pressure steam inlet (3) of the turboset (2) through a first regulating valve (15); a steam output end of the external source steam regulator (15) is connected to the high-pressure steam inlet (3) of the turboset (2) through a second regulating valve (20) and a second switching valve (19). A low-pressure steam outlet (4) of the turboset (2) is connected to a circulating water input end of the solar steam generation device through a condenser (5), a deaerator (6), a water feed pump (7) and a first switching valve (16) in turn. An output end of the water feed pump (7) is connected to an external source steam water return bypass (11) through a fourth switching valve (23).

IPC Classes  ?

• F03G 6/06 - Devices for producing mechanical power from solar energy with solar energy concentrating means
• F01K 11/02 - Steam engine plants characterised by the engines being structurally combined with boilers or condensers the engines being turbines

Abstract

The present invention provides a Fischer-Tropsch synthesis cobalt nano-catalyst based on porous material confinement, and a preparation method therefor. The catalyst of the present invention uses organogel as a template and is prepared by means of a sol-gel method; metal components are used as the core and the porous material is used as the shell. The metal components comprise a first metal component Co; a second metal component, being one of Ce, La, and Zr, and a third metal component, being one of Pt, Ru, Rh, and Re. In a finished catalyst, the first metal component accounts for 10%-35% by weight, the second metal component accounts for 0.5% to 10% by weight, the third metal component accounts for 0.02% to 2% by weight, and the rest is a carrier. The carrier is the porous material and is spherical, and the component thereof is nano-silica or alumina. The pore diameter of the porous material is 1-20 nm, the surface area is 300-500 m2/g, and the particle size of the active component is 0.5-20 nm. The core-shell structure cobalt porous catalyst of the present invention has the advantages of low methane selectivity, high catalysis reactivity, and good C5+ selectivity, and the main products of the present invention are diesel oil and paraffin.

IPC Classes  ?

• B01J 21/04 - Alumina
• B01J 21/08 - Silica
• B01J 37/00 - Processes, in general, for preparing catalystsProcesses, in general, for activation of catalysts
• C10G 2/00 - Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon

Abstract

A methanation catalyst of carbon dioxide, a preparation method and a usage of the same. The catalyst is prepared by high-temperature calcination of ash of a biomass power plant mixed with a metal nickel compound, the component of the metal nickel being 2-20% by weight. The preparation method comprises: 1) preparing the metal nickel compound as a water solution with a mass concentration being 5-30%; 2) calcinating the ash of the biomass power plant in the temperature of 300-400°C for 20-40min; 3) converting raw material proportions according to the weight percentage of the nickel component in the catalyst, mixing the water solution of the metal nickel compound prepared in the step 1) and the calcinated ash of the biomass power plant in the step 2), stirring and turning over for 5-10h for uniform impregnation; 4) drying the impregnated ash of the biomass power plant in the temperature of 110-150°C for 0.5-1.5h; and 5) calcinating the dried ash of the biomass power plant in the temperature of 400-500°C for 3-6h. The catalyst can not only make waste profitable, but also has excellent catalytic activity, which can be used to catalyze a carbon dioxide hydrogenation reaction to impel the carbon dioxide to be converted into methane, and is especially applicable in resource recycling of the ash of the biomass power plant.

IPC Classes  ?

• B01J 23/78 - Catalysts comprising metals or metal oxides or hydroxides, not provided for in group of the iron group metals or copper combined with metals, oxides or hydroxides provided for in groups with alkali- or alkaline earth metals or beryllium
• C07C 1/12 - Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon from oxides of carbon from carbon dioxide with hydrogen
• C07C 9/04 - Methane

Abstract

A disc-type solar Stirling engine power generation device capable of operating continuously day and night comprises a solar disc-type Stirling engine power generation unit (1). A burner (2) and a burner position adjustment mechanism (3) capable of adjusting a burning opening of the burner to aim at a heat receiver of the disc-type solar Stirling engine unit or leave the heat receiver are disposed on each disc-type solar Stirling engine unit. The position adjustment mechanism is installed on a support (1a) of the disc-type solar Stirling engine. The burner (2) is installed on the position adjustment mechanism. A fuel supply system (4) of the burner is connected to the burner through a main switching valve (4c), a branch switching valve (5), a regulation valve (6), and a flexible fuel pipe (7). The Stirling power generation device is capable of stably generating power during nights and cloudy days.

IPC Classes  ?

• F03G 6/00 - Devices for producing mechanical power from solar energy
• F02G 1/043 - Hot gas positive-displacement engine plants of closed-cycle type the engine being operated by expansion and contraction of a mass of working gas which is heated and cooled in one of a plurality of constantly communicating expansible chambers, e.g. Stirling cycle type engines

Abstract

Disclosed is a method and device for preparing a high temperature water vapour rich in active particles using plasma, the device comprising a plasma generator (1) and a high temperature vapour generator (2), wherein the middle of one end of the high temperature vapour generator (2) is provided with a high temperature plasma inlet (4) in communication with an outlet (1b) of the plasma generator (1); the plasma generator (1) has an inlet (1a) for non-oxidizing gases; the high temperature plasma inlet (4) is surrounded by an annular vapour inlet (3d), which annular vapour inlet (3d) has rotary guide blades (7) mounted therein. The casing of the high temperature vapour generator (2) has a shape of stepped increasing stages divided into 1-4 stage(s), and an annular narrow orifice (3a, 3b, 3c) for vapour entrance is provided between two adjacent casing parts at each stage, with the annular narrow orifice (3a, 3b, 3c) connected to a vapour pressure feeding device (3). The method comprises the steps of: spraying the prepared vapour and the high temperature plasma working materials ionized by the plasma generator (1) into the high temperature vapour generator (2) through their respective inlets, intensively mixing the high temperature vapour and the high temperature plasma, and heating and activating the vapour so as to form the vapour with active particles.

IPC Classes  ?

• B01J 19/08 - Processes employing the direct application of electric or wave energy, or particle radiationApparatus therefor
• B01F 5/04 - Injector mixers
• C10J 3/00 - Production of gases containing carbon monoxide and hydrogen, e.g. synthesis gas or town gas, from solid carbonaceous materials by partial oxidation processes involving oxygen or steam

Abstract

Disclosed is a solar energy generation system using a biomass boiler (6) as an auxiliary heat source, comprising a solar energy light gathering and heat collecting device, a biomass boiler (6), a turbine generator system, wherein the solar energy light gathering and heat collecting device uses water as a working medium, and adopts medium pressure solar energy vacuum heat-collecting pipes (13) in a serial/parallel matrix combination, an outlet of the solar energy light gathering and heat collecting device is in communication with a bottom of a drum (6a) of the biomass boiler (6) via a second control valve (22), and a steam outlet of the biomass boiler drum (6a) is connected with a cylinder (3) of a turbine generator (1). The generation system uses the solar heat source and the biomass heat source alternatively according to weather variations, so the system operates stably, thereby improving the device utilization. Further disclosed is a generation method using the generation system.

IPC Classes  ?

• F03G 6/06 - Devices for producing mechanical power from solar energy with solar energy concentrating means
• F01K 11/02 - Steam engine plants characterised by the engines being structurally combined with boilers or condensers the engines being turbines

Abstract

3 by adjusting the amount of pyrolysis gas for transportation. The temperature of the carbonization furnace is controlled at between 400° C. and 600° C. by adjusting the amount of oxygen.

IPC Classes  ?

• C01B 6/24 - Hydrides containing at least two metals, e.g. Li(AlH4)Addition complexes thereof
• C10J 3/00 - Production of gases containing carbon monoxide and hydrogen, e.g. synthesis gas or town gas, from solid carbonaceous materials by partial oxidation processes involving oxygen or steam
• C10J 3/46 - Gasification of granular or pulverulent fuels in suspension

Abstract

A process and system for producing synthesis gas from biomass by pyrolysis are provided. The process comprises the following steps: 1) pre-treating biomass raw material (1); 2) performing pyrolysis on the biomass raw material (1) by fast biomass pyrolysis technology to obtain a pyrolysis gas and carbon powders in a pyrolysis bed (5); 3) separating the pyrolysis gas from the carbon powders and a solid heat carrier by a cyclone separator (6); 4) separating the carbon powders from the solid heat carrier by a solid-solid separator (7), with the carbon powders being collected via a carbon powder hopper (8) and the solid heat carrier being recycled in the pyrolysis bed (5) after being heated in a carrier heating fluidized bed (9-2); 5) delivering the generated pyrolysis gas to a condensation tank (12) for spray-condensing with the condensable part in the pyrolysis gas being condensed to generate biofuel oil which are compressed by a high-pressure oil pump (17) and then introduced into a gasification furnace (20) to be gasified; and 6) delivering a part of the uncondensed pyrolysis gas to a combustion bed (9-1) to combust with air, and delivering the other part to the pyrolysis bed (5) as a fluidizing medium. The raw material is directly dried by using hot flue gas produced by the carrier heating fluidized bed (9-2). The heat generated by combusting the uncondensed pyrolysis gas produced by the pyrolysis bed (5) with air in the combustion bed (9-1) is supplied to the pyrolysis bed (5).

IPC Classes  ?

• C10J 3/66 - Processes with decomposition of the distillation products by introducing them into the gasification zone
• C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
• C10B 57/10 - Drying
• C10B 49/22 - Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with moving solid heat-carriers in divided form in dispersed form according to the "fluidised bed" technique
• C01B 3/36 - Production of hydrogen or of gaseous mixtures containing hydrogen by reaction of gaseous or liquid organic compounds with gasifying agents, e.g. water, carbon dioxide, air by reaction of hydrocarbons with gasifying agents using oxygen or mixtures containing oxygen as gasifying agents

Abstract

A process and system for producing synthesis gas from biomass by carbonization are provided. The system comprises a pre-treatment part for biomass raw material, a carbonization furnace (4), a gasification furnace (20) and a pipeline connection and gas delivery system thereof. The top of the carbonization furnace (4) is connected with a cyclone separator (5), and the output end of the cyclone separator (5) is connected with a combustion bed (7) and a charcoal hopper (12) respectively. The output end of the combustion bed (7) is connected to a heat exchanger (9) for heating cycling pyrolysis gas. An outlet of the heated pyrolysis gas is connected with the carbonization furnace (4), and an outlet of the heat-exchanged waste heat flue gas is connected with a drying system (2). The pipeline from a charcoal outlet of the carbonization furnace (4) to the charcoal hopper (12) is provided with a water-cooling screw conveyer (11) which cools the charcoal from the outlet of the carbonization furnace (4) to 60-280℃ and then conveys it to the charcoal hopper (12). The pipeline from the outlet of the charcoal hopper (12) to the gasification furnace (20) is provided with a mill (13), a charcoal slurry tank (16) and a high-pressure charcoal slurry pump (17) in turn. A gas supply pipe of the burning bed (7) is connected with an air pipeline (6), thereby supplying air as combustion-supporting gas.

IPC Classes  ?

• C10J 3/66 - Processes with decomposition of the distillation products by introducing them into the gasification zone
• C10J 3/54 - Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
• C10J 3/56 - ApparatusPlants
• C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
• C10B 57/10 - Drying
• C10B 49/02 - Destructive distillation of solid carbonaceous materials by direct heating with heat-carrying agents including the partial combustion of the solid material to be treated with hot gases or vapours, e.g. hot gases obtained by partial combustion of the charge

Abstract

High temperature gasifying process with biomass includes feeding, carbonization, powder making of charcoal, transportation of powdery charcoal and gasifying in gasifier, wherein the high temperature charcoal discharged from the carbonization furnace is condensed to 60-200℃ through condenser, then is reduced to normal pressure by feeding apparatus for reducing pressure. The charcoal is turned into powder through powder making machine, and then the powdery charcoal is sent to feeding apparatus for increasing pressure, the powdery charcoal with increased pressure is ejected to gasifier by ejector. In the process, the pyrolysis gas produced from carbonization furnace is used as carrier gas, and the ratio of solid to gas in the transportation pipe for powdery charcoal is controlled to 0.03-0.45m3/m3 by adjusting the amount of pyrolysis gas for transportation. Carbonization goes on through direct combustion of additionally provided combustible gas and oxygen in carbonization furnace, the temperature of carbonization furnace is controlled at 400-600℃ through adjusting the amount of oxygen. The system for performing the process is characterized in that the pipeline from the outlet of charcoal at carbonization furnace to gasifier is sequently positioned with condenser of charcoal, feeding apparatus for reducing pressure of charcoal, powder making machine, feeding apparatus for increasing pressure of charcoal and powdery charcoal ejector.

IPC Classes  ?

• C10J 3/00 - Production of gases containing carbon monoxide and hydrogen, e.g. synthesis gas or town gas, from solid carbonaceous materials by partial oxidation processes involving oxygen or steam
• C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
• B09B 3/00 - Destroying solid waste or transforming solid waste into something useful or harmless

Abstract

High temperature gasifying process with biomass includes feeding, carbonization, powder making of charcoal, transportation of powdery charcoal and gasifying in gasifier, wherein carbonization is carried out in the carbonization furnace for pyrolysis of biomass with the heat released by direct combustion of additionally provided combustible gas and oxygen, the product of carbonization is pyrolysis gas and charcoal. The temperature in the carbonization furnace is controlled at 400~600℃through adjusting the amount of oxygen,  the molar number of added combustible gas is greater than 1 and less than 5 based on that the molar number of combustible gas is 1 when it is completely combusted with oxygen. The temperature of the flame at the nozzle of the carbonization furnace is controlled at 1800~1200℃ through adjusting the amount of additionally provided combustible gas entering into the carbonization furnace. Powdery charcoal is formed through reducing the temperature of charcoal, reducing pressure, powder making, increasing pressure and fluidization, and the powdery charcoal is sent to gasifier through adjusting the transportation amount of the pyrolysis gas and/or additionally provided combustible gas. The system for performing the process includes a filter, the filter is positioned at the outlet of the pyrolysis gas of the carbonization furnace, wherein the pipe of the reverse purging gas of the filter is in fluid communication with the pipe of additionally provided combustible gas.

IPC Classes  ?

• C10J 3/00 - Production of gases containing carbon monoxide and hydrogen, e.g. synthesis gas or town gas, from solid carbonaceous materials by partial oxidation processes involving oxygen or steam
• C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
• B09B 3/00 - Destroying solid waste or transforming solid waste into something useful or harmless

Abstract

High temperature gasifying process with biomass includes feeding, carbonization, powder making of charcoal, transporting of powdery charcoal and gasifying in gasifier, wherein carbonization is carried out in the carbonization furnace for pyrolysis of biomass with the heat released by the direct combustion of additionally provided combustible gas and oxygen, the product of carbonization is pyrolysis gas and charcoal. The temperature in the carbonization furnace is controlled at 400~600℃through adjusting the amount of oxygen, the molar number of combustible gas is greater than 1 and less than 5 based on that the molar number of combustible gas is 1 when it is completely combusted with oxygen. The temperature of the flame at the nozzle of the carbonization furnace is controlled at 1800~1200℃ through adjusting the amount of additionally provided combustible gas entering into the carbonization furnace. Powdery charcoal is formed through reducing the temperature of charcoal, reducing pressure, powder making, increasing pressure and fluidization, and the powdery charcoal is sent to gasifier through adjusting the transportation amount of the pyrolysis gas. The system for performing the process includes a carbonizing furnace, a powder-making system and so on.

IPC Classes  ?

• C10J 3/00 - Production of gases containing carbon monoxide and hydrogen, e.g. synthesis gas or town gas, from solid carbonaceous materials by partial oxidation processes involving oxygen or steam
• C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material
• B09B 3/00 - Destroying solid waste or transforming solid waste into something useful or harmless

Abstract

A high-temperature gasification process using biomass to produce synthetic gas involves gasifying a powdered charcoal through transporting the powdered charcoal to a gasification furnace. An externally supplied combustible gas is directly combusted and reacted with the oxygen in a carbonization furnace, and the heat discharged from the reaction is directly supplied for a thermolysis of biomass. The thermolysis gas and the charcoal are produced from the carbonization furnace. Temperature of the carbonization furnace is controlled within 400 to 600℃. Flame temperature at a burner of the carbonization furnace is controlled within 1800 to 1200℃. A system for the process is also disclosed.

IPC Classes  ?

• C10B 53/02 - Destructive distillation, specially adapted for particular solid raw materials or solid raw materials in special form of cellulose-containing material