A temperature-controlling measure for a hydrogenation slurry bed reactor has three control points that are set from low to high: cold hydrogen is injected automatically when the system reaches control point 1; cold oil in injected automatically when the system reaches control point 2; each pressure relief is opened automatically when the system reaches control point 3. The pressure relief point is set before and/or after the circulation pump of the reactor if internal circulation is set in the reactor; the pressure relief point is set at the reactor bottom if the internal circulation is not set; at least one pressure relief valve is set at each pressure relief point.
B01J 8/22 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés les particules étant fluidisées l'agent fluidisant étant un liquide du gaz étant introduit dans le liquide
C10G 1/08 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par hydrogénation destructive avec catalyseurs mobiles
G05D 23/12 - Commande de la température sans source d'énergie auxiliaire avec l'élément sensible répondant aux variations de la pression ou du volume dans un fluide renfermé
2.
WHOLE-PLANT TECHNOLOGICAL PROCESS ADOPTING ALL-ROUND BED HYDROGENATION PROCESS
Provided is a whole-plant technological process adopting an all-round bed hydrogenation process. The whole-plant technological process can be used for residual oil and crude oil refining as well as oil and coal co-refining, and the key of the process is an all-round bed reactor and the oil soluble catalyst, the all-round bed hydrogenation process adopts an empty cylinderical, natural internal circulation or forced internal circulation type reactor for treatment. The process comprises crude oil distillation, residual oil (or oil-coal) all-round bed hydrogen cracking, distillate oil all-round bed hydrogenation, catalytic reforming, isomerization, hydrogen production, light hydrocarbon recovery and sulfur recovery. Whole-plant devices are remarkably decreased, the whole-plant technological process is shortened, the safety risk is low, maintenance work amount is small, economic benefits are increased, and atmospheric pollution is reduced.
C10G 69/00 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion
C10G 45/16 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour éliminer des hétéro-atomes sans modifier le squelette de l'hydrocarbure mis en œuvre et sans craquage en hydrocarbures à point d'ébullition inférieurHydrofinissage avec des particules solides en mouvement dispersés dans l'huile, p. ex. sous forme de bouillie
C10G 47/00 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur
3.
TEMPERATURE AND PRESSURE CONTROL METHOD FOR HYDROGENATION PROCESS, DESIGN METHOD THEREFOR AND USE THEREOF
Disclosed are a temperature and pressure control method for a hydrogenation process, a design method therefor and the use thereof. A pressure relief point is arranged at an outlet of a separation system after a reactor, or at a downstream device or pipeline connected thereto, with the temperature at the pressure relief point being 30-220C. Two control points are arranged, wherein when control point I is exceeded, i.e., temperature 440C /pressure 19 MPa, the pressure reduction rate is 3-10 bar/min; and when control point II is exceeded, i.e., temperature 460C /pressure 21 MPa, the pressure reduction rate is 10-25 bar/min. By using this control method, a high-pressure device can be made more stable during a pressure relief process.
Disclosed are a method for increasing hydrogen partial pressure in a hydrogenation reaction system, a design method therefor and the use thereof. The hydrogenation reaction system comprises at least two reactors, wherein a discharged material from the previous stage of reactor first enters a separation system, which increases the hydrogen partial pressure, for separation, a non-hydrogen component is separated and discharged, and a hydrogen component and liquid and solid phases enter the next stage of reactor. By using this method, the hydrogen partial pressure in the next stage of reactor can be increased, deepening the depth of reaction, improving the rate of conversion of raw materials and the yield of light oils, improving the space velocity, and reducing energy consumption.
An oil-coal co-hydrotreating processing includes the following steps: pulverized coal, vacuum residue and recycle oil are mixed to prepare coal slurry. After mixed with hydrogen, catalyst and additive, oil-coal slurry is preheated into a slurry bed reactor with high reacting pressure for thermal cracking and hydrogenation reaction. After reaction, all the products go into the hot high pressure separator for separation of solid from the bottom and gas from the top. The gas obtained goes into the fixed bed reactor for further hydrocracking or refining, and the distillate obtained enter the fractionating tower. The vacuum gas oil from the bottom of fractionating tower is taken as recycle oil piped to the oil-coal slurry mixing device as solvent.
C10G 1/06 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par hydrogénation destructive
C10G 1/08 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par hydrogénation destructive avec catalyseurs mobiles
C10G 67/00 - Traitement des huiles d'hydrocarbures, uniquement par au moins un procédé d'hydrotraitement et au moins un procédé de raffinage en l'absence d'hydrogène
C10L 9/04 - Traitement des combustibles solides en vue d'améliorer leur combustion par des moyens chimiques par hydrogénation
C10L 9/06 - Traitement des combustibles solides en vue d'améliorer leur combustion par des moyens chimiques par oxydation
C10G 45/02 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour éliminer des hétéro-atomes sans modifier le squelette de l'hydrocarbure mis en œuvre et sans craquage en hydrocarbures à point d'ébullition inférieurHydrofinissage
C10G 45/16 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour éliminer des hétéro-atomes sans modifier le squelette de l'hydrocarbure mis en œuvre et sans craquage en hydrocarbures à point d'ébullition inférieurHydrofinissage avec des particules solides en mouvement dispersés dans l'huile, p. ex. sous forme de bouillie
C07C 1/04 - Préparation d'hydrocarbures à partir d'un ou plusieurs composés, aucun d'eux n'étant un hydrocarbure à partir d'oxydes de carbone à partir de monoxyde de carbone avec de l'hydrogène
6.
METHOD FOR STAGE-BY-STAGE PRESSURE REDUCTION OF THREE-PHASE FLUID AND DESIGN METHOD THEREFOR AND USE THEREOF
Disclosed is a method for the stage-by-stage pressure reduction of a three-phase fluid, wherein the three-phase fluid flows through pressure-reducing valves of at least two stages for the completion of pressure reduction in order to separate light components, the pressure of the three-phase fluid before the first pressure reduction is ≥ 15 MPa, the pressure of the three-phase fluid after the last pressure reduction is ≤ 5 Mpa, the content of each of a gas phase, a liquid phase and a solid phase in the three-phase fluid is ≥ 1 wt％. In the method for the stage-by-stage pressure reduction of the three-phase fluid, the fluid flows through pressure-reducing valves of at least two stages in order to separate light components, and this stage-by-stage pressure reduction reduces the pressure drop magnitude of each stage and can directly substantially decrease the degrees of expansion-type wearing and cavitation-type wearing on equipment and valves. Further disclosed are a use of the above-mentioned method for the stage-by-stage pressure reduction of a three-phase fluid and a design method therefor.
C10G 31/00 - Raffinage des huiles d'hydrocarbures, en l'absence d'hydrogène, par des méthodes non prévues ailleurs
C10G 67/02 - Traitement des huiles d'hydrocarbures, uniquement par au moins un procédé d'hydrotraitement et au moins un procédé de raffinage en l'absence d'hydrogène uniquement par plusieurs étapes en série
C10G 1/00 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon
7.
OIL-SOLUBLE HYDROGENATION CATALYST, AND PREPARATION METHOD THEREFOR AND USE THEREOF
An oil-soluble hydrogenation catalyst, and a preparation method therefor and the use thereof. The catalyst comprises the following ingredients: one or several of VIII group and VIB group metal compounds, one or several of carboxylic acid organic matter and alcohol organic matter, and a vulcanizing agent, wherein the mass content of the metal elements in the catalyst is 0.5-15% by weight; the vulcanizing agent is liquid sulfur or an unstable sulfide which can be decomposed into H2S under vulcanization conditions; and the mass of the sulfur element in the vulcanizing agent is 0.8-4 times the mass of the metal elements in the catalyst.
B01J 31/28 - Catalyseurs contenant des hydrures, des complexes de coordination ou des composés organiques contenant en outre des composés métalliques inorganiques non prévus dans les groupes du groupe du platine, du cuivre ou du groupe du fer
B01J 31/34 - Catalyseurs contenant des hydrures, des complexes de coordination ou des composés organiques contenant en outre des composés métalliques inorganiques non prévus dans les groupes du chrome, du molybdène ou du tungstène
B01J 31/04 - Catalyseurs contenant des hydrures, des complexes de coordination ou des composés organiques contenant des composés organiques ou des hydrures métalliques contenant des acides carboxyliques ou leurs sels
C10G 1/06 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par hydrogénation destructive
C10G 49/02 - Traitement des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, non prévu dans un seul des groupes , , , ou caractérisé par le catalyseur utilisé
C10G 49/04 - Traitement des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, non prévu dans un seul des groupes , , , ou caractérisé par le catalyseur utilisé contenant du nickel, du cobalt, du chrome, du molybdène ou du tungstène, ou leurs composés
C10G 49/06 - Traitement des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, non prévu dans un seul des groupes , , , ou caractérisé par le catalyseur utilisé contenant des métaux du groupe du platine ou leurs composés
A temperature control measure for a slurry bed hydrogenation reactor and a design method and use thereof. Three control points are set: when the temperature reaches the first control point, cold hydrogen is injected; when the temperature reaches the second control point, a cold oil is injected; and when the temperature reaches the third control point, various depressurization points are started. The temperature of the first control point is larger than or equal to 425°C and smaller than 440°C, and/or the pressure of the first control point is larger than or equal to 19 MPa; the temperature of the second control point is larger than or equal to 440°C and smaller than 455°C, and/or the pressure of the second control point is larger than or equal to 19 MPa; and the temperature of the third control point is larger than or equal to 455°C, and/or the pressure of the third control point is larger than or equal to 20 MPa. If internal circulation is set for the reactor (1), the depressurization points are set in front and/or rear of a reactor circulation pump (5); if no internal circulation is set for the reactor, the depressurization points are set at the bottom of the reactor; the number of reducing valves (7) set at each depressurization point is larger than or equal to 1. The measure is easy to operate and high in automation degree and improves safety of the reactor and production.
C10G 1/08 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par hydrogénation destructive avec catalyseurs mobiles
B01J 8/22 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés les particules étant fluidisées l'agent fluidisant étant un liquide du gaz étant introduit dans le liquide
A method and device for inline detection and control of the degree of swelling of coal: transporting a portion of an oil-coal slurry completely swollen in an oil-coil slurry swelling tank (1) into a detection tank (4), calculating the liquid level height h1 = m/ρ·s·(a + 1) of unswollen pulverized coal in the detection tank (4) on the basis of the oil-to-coal mass ratio a, the density ρ of pulverized coal, the bottom area s of the detection tank (4), and the measured total mass m of the oil-coal slurry in the detection tank (4), then turning on a centrifuge (5) at the lower part of the detection tank (4) to rotate the oil-coal slurry until the oil and coal are stratified, and then measuring the liquid level height h2 of the coal stratum, thus determining the degree of swelling of coal Q = h2/h1, and operating normally the swelling tank (1) when Q is in an acceptable range, otherwise, turning on a steam pneumatic valve (7) controlling the swelling conditions of the oil-coal slurry swelling tank (1) to optimize operating conditions. The detection and control of the degree of swelling of coal per the present method ensure the conversion rate of coal and the yield and quality of a hydrogenated oil, and provide great effects and value for industrial promotion.
C10G 1/00 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon
G01N 15/08 - Recherche de la perméabilité, du volume des pores ou de l'aire superficielle des matériaux poreux
A method for processing oil and coal using a mixed refining process: pre-treating raw oil and coal according to a ratio of 97-30:3-70, adding hydrogen and a catalyst, and placing into a slurry bed hydrogenation unit, the gas components produced by the slurry bed becoming gas products after being treated through a gas treatment process; and the liquid components becoming liquid products after being treated successively through a single-stage or multi-stage hydrogenation treatment process, a catalytic reforming process, and an aromatics extraction process. The present method has an improved total yield of light oil, a short process flow, high apparatus utilisation rate, and reduced investment costs, is environmentally friendly, and the process line thereof is easy to adjust.
C10G 1/06 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par hydrogénation destructive
C10G 69/08 - Traitement des huiles d'hydrocarbures par au moins un procédé d'hydrotraitement et au moins un autre procédé de conversion uniquement par plusieurs étapes en série comprenant au moins une étape de réformage d'essence "naphta"
11.
METHOD FOR REMOVING CRYSTALLINE SALT, AND DESIGN METHOD AND APPLICATION THEREOF
A method for removing crystalline salt: arranging at least one concentration detector in a waste water outlet pipeline of a final stage separator; detecting the concentration of obstructive matter in the waste water gathered after water filling and flushing at a water filling site, and determining the type of obstructive matter; then, on the basis of the concentration and type of the obstructive matter, controlling the water filling amount at each water filling site to be 50-1000 times greater than the water required for saturation concentration of the obstructive matter, the water filling site being located in a pipeline between a reactor and a separator and/or a separator and/or a pipeline between separators. The present removal method is used in devices and pipelines in a slurry bed hydrogenation process, solving the problem of the large amount of by-products such as crystalline matter in the hydrogenated product, and reducing the content of nitrogen and heavy metals in the hydrogenated product and the separated liquid oil intermediate product.
A method for preprocessing raw materials of a slurry bed hydrogenation process: a heavy oil, pulverized coal, and a catalyst attached having pulverized coal attached thereto are jointly mixed, kneaded in a kneading machine, and circulatively stirred in at least one level of swelling tank to produce a catalyst/oil-coal slurry; or, the heavy oil is mixed respectively with pulverized coal and the catalyst having pulverized coal attached thereto, kneaded in different kneading machines, converged to the one level of swelling tank, and circulatively stirred for at least one level to produce the catalyst/oil-coal slurry, where the particle size of the pulverized coal is less than 470 μm, and the mass ratio of the heavy oil to the pulverized coal is 97-30 : 3-70. The method increases the conversion rate of coal and total yield of a light oil, reduces wearing by the raw materials on equipment, pumps, valves, and piping at the same time, and is simple to operate, accurate, and practical.
C10G 45/16 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour éliminer des hétéro-atomes sans modifier le squelette de l'hydrocarbure mis en œuvre et sans craquage en hydrocarbures à point d'ébullition inférieurHydrofinissage avec des particules solides en mouvement dispersés dans l'huile, p. ex. sous forme de bouillie
C10G 1/08 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par hydrogénation destructive avec catalyseurs mobiles
13.
CATALYST SUPPORT, LOADING METHOD THEREOF, AND USES THEREOF
A catalyst support, a loading method thereof, and uses thereof. The active component of the catalyst is either one of or a combination of several group VIII and group VIB metal compounds. The support is a powdered substance having adsorptive capability, where the bulk density of the support is 0.8-3.0 g/cm3, the specific surface area is 100-1000 m2/g, the average pore diameter is 6-300 nm, the pore volume is 0.2-1.5 cm3/g, and the support accounts for 12 wt% to 95 wt% of the total mass of the catalyst. The support having the parameters of the present invention has reduced density and hardness, greatly enhances the dispersibility of the catalyst, thus allowing the catalyst to maximize the catalytic activity thereof, reduces wearing to equipment, pumps, valves, and piping, provides great delivery conditions, and is inexpensive.
A method of matching and selecting source materials for a coal and oil mixture refining process. The oil is characterized by: a saturated component content exceeding or equal to 8%, a linear alkane content less than or equal to 6%, and an aromatic hydrocarbon content exceeding or equal to 15%. The coal is characterized by: a hydrogen/carbon ratio exceeding or equal to 0.55, a volatile component exceeding or equal to 20%, and an air dried moisture content less than or equal to 26%, an air dried ash content less than or equal to 27%, and a particle diameter less than or equal to 470 μm. The method can precisely control properties of oil and coal added into a hydrogen reactor, providing a favorable match between a source oil and coal, resulting in effective synergy, increasing a conversion rate of coal and oil, and delivering an increased liquid product yield.
C10G 1/06 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par hydrogénation destructive
15.
SPIRAL THREE-DIMENSIONAL TYPE APPARATUS FOR CONVEYING AND COOLING OIL COKE OR PITCH, DESIGN METHOD THEREFOR, AND USE THEREOF
A spiral three-dimensional type apparatus for conveying and cooling oil coke or pitch, a design method therefor, and a use thereof. An existing plane-type oil coke or pitch conveying mode is changed to a spiral three-dimensional type conveying mode. One end of a conveying belt (1) is connected to a discharging pipeline (3) for oil coke (100 to 350°C) after being cooled, and the other end of the conveying belt (1) is connected to a discharging hopper (5). The conveying belt (1) is arranged in a spiral descending mode, and the spiral descending angle (α) of the conveying belt (1) ranges from 5 to 30°. A cooling water pipeline is arranged inside the conveying belt (1) to accelerate cooling molding of oil coke and pitch. The apparatus can reduce the occupied space of a molding area for oil coke or pitch, and improves the usage rate of factory unit area.
B65G 15/22 - Transporteurs comportant des surfaces porteuses de charges sans fin, c.-à-d. des tapis roulants ou autres systèmes équivalents, auxquelles l'effort de traction est transmis par des moyens différents des éléments d'entraînement sans fin de même configuration comportant une série d'éléments travaillant ensemble
16.
WAX OIL CIRCULATING HYDROGENATION METHOD, DESIGN METHOD THEREFOR, AND USE THEREOF
A wax oil circulating hydrogenation method, a design method therefor, and a use thereof. The hydrogenation method comprises: mixing the wax oil produced by a slurry bed hydrogenation reactor with some or all raw materials to be hydrogenated or one or two catalysts to obtain raw material slurry having reduced viscosity, the raw material slurry entering the slurry bed hydrogenation reactor for circulating hydrogenation. The mass fraction of wax oil for circulating hydrogenation accounts for 4-30wt% of the raw materials to be hydrogenated, such that the kinematic viscosity of the raw material slurry is less than or equal to 750 cSt at the temperature being less than or equal to 60°C. The method is simple and convenient to operate, facilitates automated control, improves the light oil yield, improves the stability of apparatus operation, and prolongs the repair cycle of a hydrogenation-series apparatus.
C10G 1/08 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par hydrogénation destructive avec catalyseurs mobiles
C10G 47/26 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur avec des particules solides en mouvement en suspension dans de l'huile, p. ex. sous forme de bouillie
C10G 47/34 - Composés organiques, p. ex. hydrocarbures hydrogénés
17.
BACKWASHING METHOD, DESIGN METHOD THEREFOR, AND USE THEREOF
A backwashing method, a design method therefor, and a use thereof. The backwashing method comprises: enabling some or all self-produced wax oil to flow into a device or a pipeline or a port blocked due to coking or discontinuous flowing for backwashing. A device for backwashing comprises a hydrogenation reactor, a pressure reduction furnace, and a separator. The used backwashing method is simple and convenient to operate, facilitates automated control, improves the light oil yield, improves the stability of apparatus operation, and prolongs the maintenance cycle of a hydrogenation-series apparatus.
B01J 8/22 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés les particules étant fluidisées l'agent fluidisant étant un liquide du gaz étant introduit dans le liquide
C10G 45/16 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour éliminer des hétéro-atomes sans modifier le squelette de l'hydrocarbure mis en œuvre et sans craquage en hydrocarbures à point d'ébullition inférieurHydrofinissage avec des particules solides en mouvement dispersés dans l'huile, p. ex. sous forme de bouillie
C10G 47/26 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur avec des particules solides en mouvement en suspension dans de l'huile, p. ex. sous forme de bouillie
C10G 49/12 - Traitement des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, non prévu dans un seul des groupes , , , ou avec des particules solides en mouvement en suspension dans de l'huile, p. ex. sous forme de bouillie
C10G 1/08 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par hydrogénation destructive avec catalyseurs mobiles
18.
MULTI-OPTIMIZED HIGH PRESSURE SEPARATOR AND CONFIGURATION METHOD AND USE THEREOF
A multi-optimized high pressure separator and configuration method and use thereof. The separator has a length-diameter ratio of 2.5-5.5:1. A feed port is located on one side of a cylinder and above the liquid surface. The height of the liquid surface is 10%-50% of the length of the tangent of the cylinder. The distance from the centerline of the feeding port to the central line of the cylinder is 15%-40% of the length of the tangent line of the cylinder. A heavy component outlet opening (5) is directly below the cylinder of the high pressure separator, and a light component outlet (4) is provided at the top of the cylinder. The bottom part of the cylinder approaching the heavy component outlet (5) is conical in structure having a cone angle of 40-120°.
C10G 31/06 - Raffinage des huiles d'hydrocarbures, en l'absence d'hydrogène, par des méthodes non prévues ailleurs par chauffage, refroidissement ou traitement par la pression
19.
NOVEL HEATING FURNACE HAVING MULTI-HEARTH STRUCTURE, AND DESIGN METHOD AND USE THEREOF
Provided are a novel heating furnace having a multi-hearth structure, and method and use thereof. The heating furnace comprises a feed channel (1), a combustor (2), a furnace body and a collection outlet channel (7). The number of the combustor (2) is one. The furnace body comprises at least two hearths (3, 4) therein. An inlet of each hearth (3, 4) comprises a heat-insulated switch-board (10, 11) capable of being opened and closed. Remote differential pressure gauges (8, 0) are respectively provided between an inlet and an outlet of each hearth (3, 4). A feed space (13) is formed between the combustor (2) and the hearths (3, 4). The feed channel (1) communicates with the feed space (13). Each hearth (3, 4) comprises an outlet channel (5, 6). A heat-insulating filler is filled between the adjacent hearths (3, 4). Without changing a furnace tube configuration, a furnace tube material and the number of the combustor, when a hearth has a problem, a heating operation can be timely switched to another hearth without suspending normal operation for a heating furnace overhaul, thereby extending an operation suspension interval of a device required by the heating furnace overhaul, improving operation stability of the device, and eliminating a need of installing a spare furnace and accordingly reducing the cost.
A multiple optimized separator combined system, a use method for same, and a design method therefor. The separator combined system has a high-temperature, high-pressure separator, a medium-temperature, high-pressure separator, a room-temperature, high-pressure separator, a low-pressure, high-temperature, a low-pressure, medium-temperature separator, and a low-pressure, room-temperature separator. Three different temperatures, namely high temperature, medium temperature, and low temperature and two different pressures, namely high pressure and low pressure, are permutated to form a six-separator combined system, which forms graded temperatures and pressures and individually separate different gaseous-phase products and liquid-phase products. This achieves with respect to separation of a gaseous phase the goal of reducing the operating pressure for downstream equipment while ensuring the purity of recycled hydrogen and the goal with respect to the separation of a liquid phase the goal of S and N removal.
The present invention is a multiple optimized separator combined system, a design method for same, and uses thereof. The combined system comprises at least two separators. The at least two separators respectively are a high-temperature, high-pressure separator and a room-temperature, low-pressure separator. The operating temperature of the high-temperature, high-pressure separator is 350-470 °C, the operating pressure of same is 17-22 MPa, and an inlet thereof is connected to an outlet of a hydrogenation reactor. The operating temperature of the room-temperature, low-pressure separator is 30-80 °C, the operating pressure of same is 1-5 MPa, a room temperature gas flows from an upper-part outlet of the separator into a recycled hydrogen treatment facility to produce recycled hydrogen and an exhaust, a liquid-phase isolated product flows from a lower-part outlet of the separator into a fractionation system to isolate a room temperature oil. The separator combined system of the present invention achieves with respect to separation of a gaseous phase the goal of reducing the operating pressure for downstream equipment while ensuring the purity of the recycled hydrogen, and achieves with respect to isolation of a liquid phase the goal of S and N removal.
An iron-based catalyst, and a preparation method therefor and a use thereof. The raw materials of the catalyst comprise the following components: an iron-based main catalyst: FeOOH; an active additive: ammonium molybdate; a carrier: a dry coal powder or an active carbon powder. The mass ratio of the metal centre Mo and the metal centre Fe is 1:350 - 1:175, and the mass ratio of the metal centre Fe and the carrier is 1:30 - 1:3. The preparation method comprises the following steps: dissolving the iron oxide-hydroxide in distilled water, stirring evenly, and obtaining an iron oxide-hydroxide slurry; adding an ammonium molybdate aqueous solution to the iron oxide-hydroxide slurry, stirring evenly, and obtaining an iron oxide-hydroxide slurry dispersed with molybdenum; adding the carrier to the iron oxide-hydroxide slurry dispersed with molybdenum, stirring evenly, filtering, and obtaining a filter cake; drying the filter cake in an N2 environment, grinding to 10-200μm, and obtaining an iron-based catalyst for slurry bed hydrogenation. The iron-based catalyst for slurry bed hydrogenation implements a high conversion rate and liquid yield in residue hydrogenation, direct coal liquefaction and oil-coal mixing, and significantly improves efficiency.
B01J 37/02 - Imprégnation, revêtement ou précipitation
C10G 49/04 - Traitement des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, non prévu dans un seul des groupes , , , ou caractérisé par le catalyseur utilisé contenant du nickel, du cobalt, du chrome, du molybdène ou du tungstène, ou leurs composés
23.
MULTI-OPTIMISED SLURRY BED HYDROGENATION REACTOR, AND DESIGN METHOD THEREFOR AND USE THEREOF
A multi-optimised slurry bed hydrogenation reactor, and a design method therefor and a use thereof. The hydrogenation reactor is provided with an inner circulation structure and a feed distributor, a feed opening being located at a bottom portion of a tower body of the reactor, a discharge opening being located at a top portion of the tower body. The inner circulation structure comprises a circulation bubble cap, a circulation tube and a circulation pump, the circulation bubble cap being located at an inner upper portion of the tower body and being a frustoconical hollow cup, a lower end being connected to the circulation tube which leads to the bottom portion of the tower body of the reactor and is connected to the circulation pump located outside the tower body. The feed distributor comprises an inlet feed distributor and a circulation feed distributor, and is located between a tower body inner wall of an inner lower portion of the tower body and the circulation tube. The feed opening comprises an inlet feed opening and a circulation feed opening. A reaction material passes through the inlet feed opening and the inlet feed distributor to enter the tower body, and circulation material recovered by the inner circulation structure passes through the circulation pump to enter the circulation feed opening, and passes through the circulation feed distributor to enter the tower body. The present invention increases the degree of back-mixing of a reactant, and increases the raw material conversion rate and the light oil yield.
B01J 8/22 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés les particules étant fluidisées l'agent fluidisant étant un liquide du gaz étant introduit dans le liquide
C10G 45/00 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène
24.
HYDROGENATION PROCESS TEMPERATURE CONTROL METHOD, AND DESIGN METHOD THEREFOR AND USE THEREOF
A hydrogenation process temperature control method, and a design method therefor and a use thereof. The hydrogenation process temperature control method comprises injecting a coolant into a hydrogenation device in order to control the temperature, injection positions being respectively located at a pipe in front of a certain stage or multi-stage reactor, in a pipe in front of a certain stage or multi-stage separator, and/or on the certain stage or multi-stage separator. The coolant is conveyed via at least one cooling pipe, and the flow may be controlled. The temperature control method effectively prevents reactor temperature runaway and the formation of vortex flows, and also prevents the occurrence of coking within the separator, thereby improving the operational stability of the hydrogenation device.
B01J 8/22 - Procédés chimiques ou physiques en général, conduits en présence de fluides et de particules solidesAppareillage pour de tels procédés les particules étant fluidisées l'agent fluidisant étant un liquide du gaz étant introduit dans le liquide
G05D 23/19 - Commande de la température caractérisée par l'utilisation de moyens électriques
25.
MULTI-OPTIMISED HYDROGENATION SERIES METHOD, AND DESIGN METHOD THEREFOR AND USE THEREOF
A multi-optimised hydrogenation series method, and a design method therefor and a use thereof. The hydrogenation method comprises the following steps: heat exchanging is performed at a heat exchanger between hydrogen and gas of an outlet of a high-temperature high-pressure separator, i.e. a high-temperature high-pressure separator at a heat exchanger to raise the temperature of the hydrogen to 300-420oC, the hydrogen being divided into two paths and heated; one path is mixed with a raw material and enters a raw material heating furnace to be heated to 330-420oC to form a mixture flow, one path enters a hydrogen heating furnace to be heated to become high temperature hydrogen having a temperature of 450-580oC, one path of the high temperature hydrogen is mixed with the mixture flow of an outlet of the raw material heating furnace and enters a primary hydrogenation reactor, one path is mixed with a material flow of an outlet of the primary hydrogenation reactor and enters a secondary hydrogenation reactor, one path enters the high-temperature high-pressure separator from a bottom portion, and if three or more reactors are provided, the high temperature hydrogen enters said reactors in a sequential manner. The method is simple in operation and facilitates automated control. The heating forms and entry positions of the hydrogen solve the problems that the temperature of an inlet of the primary reactor is unstable, the hydrogen partial pressure of the second reactor is insufficient, and asphaltenes undergo condensation reactions within the separator.
C10G 47/26 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur avec des particules solides en mouvement en suspension dans de l'huile, p. ex. sous forme de bouillie
C10G 45/16 - Raffinage des huiles d'hydrocarbures au moyen d'hydrogène ou de composés donneurs d'hydrogène pour éliminer des hétéro-atomes sans modifier le squelette de l'hydrocarbure mis en œuvre et sans craquage en hydrocarbures à point d'ébullition inférieurHydrofinissage avec des particules solides en mouvement dispersés dans l'huile, p. ex. sous forme de bouillie
26.
METHOD AND EQUIPMENT FOR SLURRY BED HYDROGENATION MIXED REFINEMENT OF OIL AND COAL
A method and equipment for slurry bed hydrogenation mixed refinement of oil and coal. The method comprises the following steps: first, coal powder, residue oil, and recycled wax are prepared into an oil-coal slurry; the oil-coal slurry, a catalyst, an additive, and hydrogen are mixed, passed through a preheater, and introduced into a slurry bed reactor for thermal cracking and hydrogenation reactions, and then all products are introduced into a hot high-pressure separator, where solids are separated at the bottom, and gases are separated at the top and then introduced into a fixed-bed reactor for further hydrocracking or refinement, a distillate oil produced is introduced into a fractionator tower, where wax at the tower bottom serves as recycled wax and recirculated to an oil-coal slurry preparation tank. The wax produced is reused as a coal-dissolving solvent, the viscosity of the oil-coal slurry is greatly reduced, the fluidity of the oil-coal slurry is improved, and the hydrogen donating capability of a liquid phase is increased. Only a media distributor is found within the slurry bed hydrogenation reactor, and no bed-level support plate is provided, thus greatly reducing medium pressure drop. The reactor has a moderate reaction pressure, the catalyst is inexpensive and easy to manufacture, for which only common domestic raw materials are used, thus greatly reducing costs.
C10G 67/00 - Traitement des huiles d'hydrocarbures, uniquement par au moins un procédé d'hydrotraitement et au moins un procédé de raffinage en l'absence d'hydrogène
C10G 1/06 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par hydrogénation destructive
27.
COAL AND OIL HYBRID HYDROGENATION REFINING TECHNIQUE AND DEVICE
A coal and oil hybrid hydrogenation refining technique and device: preparing coal dust, residual oil, and recycled wax oil into a coal-oil slurry; mixing same with a catalyst, an additive, and hydrogen; implementing a thermal cracking and hydrogenation reaction in a slurry-bed reactor; placing all the products thereof into a thermal high-pressure separator; after separating the solids from the bottom and the gases from the top, implementing further hydrocracking or refining in a fixed-bed reactor; and placing the obtained distillate oil into a fractionation column, the wax oil at the bottom of the column being recycled wax oil. Re-using the produced wax oil as a coal-oil solvent oil reduces the viscosity of the coal-oil slurry, improves the fluidity of the coal-oil slurry, and increases the hydrogen production capacity of the liquid phase. The inside of the slurry-bed hydrogenation reactor is only provided with a medium distributor, and no bed layer support plate is arranged therein, reducing the medium pressure drop.
C10G 1/06 - Production de mélanges liquides d'hydrocarbures à partir de schiste bitumineux, de sable pétrolifère ou de matières carbonées solides non fusibles ou similaires, p. ex. bois, charbon par hydrogénation destructive
C10G 65/02 - Traitement des huiles d'hydrocarbures, uniquement par plusieurs procédés d'hydrotraitement uniquement par plusieurs étapes en série
28.
RESIDUAL OIL SLURRY BED HYDROCRACKING METHOD AND DEVICE
A residual oil slurry bed hydrocracking method and device. A procedure of a "slurry bed + fixed bed" reactor is adopted, and raw materials, additives, catalysts and hydrogen gas are mixed, heated, pressurized and then fed into a slurry bed reactor for thermal cracking reaction and catalysis reaction. In the reaction process, coke, catalysts and additives are subsequently separated at the bottom of a thermal high pressure separator. A light oil product is produced through further hydrocracking and hydrogen refining in an ordinary fixed bed reactor. A ferro-molybdenum catalyst is adopted to improve the reaction activity, inhibit coke generation, reduce the pressure of the system to 17 to 20 MPa, and greatly lower the cost of equipment. By means of the method, the conversion rate of residual oil can be 90% to 95%, and the light oil yield can be 80% to 83%.
C10G 47/02 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur caractérisé par le catalyseur utilisé
C10G 47/26 - Craquage des huiles d'hydrocarbures, en présence d'hydrogène ou de composés donneurs d'hydrogène, pour obtenir des fractions à point d'ébullition inférieur avec des particules solides en mouvement en suspension dans de l'huile, p. ex. sous forme de bouillie
brevets
