WO2015141624A1 - Dispositif pour tester un catalyseur destiné à être utilisé dans le craquage catalytique fluide - Google Patents

Dispositif pour tester un catalyseur destiné à être utilisé dans le craquage catalytique fluide Download PDF

Info

Publication number
WO2015141624A1
WO2015141624A1 PCT/JP2015/057693 JP2015057693W WO2015141624A1 WO 2015141624 A1 WO2015141624 A1 WO 2015141624A1 JP 2015057693 W JP2015057693 W JP 2015057693W WO 2015141624 A1 WO2015141624 A1 WO 2015141624A1
Authority
WO
WIPO (PCT)
Prior art keywords
catalyst
catalytic cracking
reaction
fluid catalytic
oil
Prior art date
Application number
PCT/JP2015/057693
Other languages
English (en)
Japanese (ja)
Inventor
伸吾 酒井
手嶋　勝英
尚夫 迫田
Original Assignee
日揮触媒化成株式会社
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by 日揮触媒化成株式会社 filed Critical 日揮触媒化成株式会社
Priority to SG11201607749YA priority Critical patent/SG11201607749YA/en
Priority to JP2016508716A priority patent/JP6407967B2/ja
Priority to KR1020167025938A priority patent/KR102278260B1/ko
Publication of WO2015141624A1 publication Critical patent/WO2015141624A1/fr

Links

Images

Classifications

    • G—PHYSICS
    • G01—MEASURING; TESTING
    • G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
    • G01N33/00—Investigating or analysing materials by specific methods not covered by groups G01N1/00 - G01N31/00
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G11/00—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G11/14—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts
    • C10G11/18—Catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid catalysts according to the "fluidised-bed" technique
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J29/00—Catalysts comprising molecular sieves
    • B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
    • B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
    • B01J29/061—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof containing metallic elements added to the zeolite
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/30—Catalysts, in general, characterised by their form or physical properties characterised by their physical properties
    • B01J35/31—Density
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J35/00—Catalysts, in general, characterised by their form or physical properties
    • B01J35/40—Catalysts, in general, characterised by their form or physical properties characterised by dimensions, e.g. grain size
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/0009—Use of binding agents; Moulding; Pressing; Powdering; Granulating; Addition of materials ameliorating the mechanical properties of the product catalyst
    • B01J37/0027—Powdering
    • B01J37/0045—Drying a slurry, e.g. spray drying
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/025—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical shaped bed
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1809—Controlling processes
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1818—Feeding of the fluidising gas
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1836—Heating and cooling the reactor
    • G—PHYSICS
    • G01—MEASURING; TESTING
    • G01N—INVESTIGATING OR ANALYSING MATERIALS BY DETERMINING THEIR CHEMICAL OR PHYSICAL PROPERTIES
    • G01N31/00—Investigating or analysing non-biological materials by the use of the chemical methods specified in the subgroup; Apparatus specially adapted for such methods
    • G01N31/10—Investigating or analysing non-biological materials by the use of the chemical methods specified in the subgroup; Apparatus specially adapted for such methods using catalysis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/10—After treatment, characterised by the effect to be obtained
    • B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
    • B01J2229/30—After treatment, characterised by the means used
    • B01J2229/42—Addition of matrix or binder particles
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J38/00—Regeneration or reactivation of catalysts, in general
    • B01J38/04—Gas or vapour treating; Treating by using liquids vaporisable upon contacting spent catalyst
    • B01J38/12—Treating with free oxygen-containing gas
    • B01J38/30—Treating with free oxygen-containing gas in gaseous suspension, e.g. fluidised bed

Definitions

  • the present invention relates to a test apparatus for a catalyst for fluid catalytic cracking of hydrocarbon oil. Specifically, the reaction results are very close to those of a pilot device for fluid catalytic cracking and further to a commercial fluid catalytic cracking device (actual device). In addition to evaluating the catalyst for fluid catalytic cracking, it is extracted from the commercial fluid catalytic cracking device.
  • the present invention relates to a test apparatus for fluid catalytic cracking catalysts applicable to the evaluation and research and development of new catalysts.
  • the fluid catalytic cracking process is a process for producing gasoline mainly from hydrocarbon oil.
  • a catalyst used in the fluid catalytic cracking process for example, a catalyst containing a zeolite, a binder, a filler such as kaolin or alumina, and an additive as required is known.
  • Patent Document 1 discloses (1) alumina particles having a particle size of 2 to 60 ⁇ m containing a metal component and a phosphorus component selected from one or more of alkaline earth metals and rare earth metals, and (2) crystalline aluminosilicate.
  • a catalyst for catalytic cracking of hydrocarbons in which (3) zeolite is uniformly dispersed in a porous inorganic oxide matrix is described. It is described that this catalyst has metal resistance, high activity, and selectivity and can suppress generation of hydrogen and coke.
  • Patent Document 2 discloses a catalyst composition for fluid catalytic cracking of hydrocarbons containing an inorganic oxide matrix other than alumina, crystalline aluminosilicate zeolite and alumina, and each component containing a phosphorus atom. It is described that when this catalyst is used for the catalytic cracking of heavy oil hydrocarbons, the bottom (bottom oil) resolution is excellent, the amount of hydrogen and coke produced is low, and the gasoline and kerosene oil fractions increase.
  • Patent Document 3 discloses (1) a molecular sieve having a —Si—OH—Al— skeleton whose surface pores are modified with a specific phosphate, (2) a water-insoluble metal salt, (3) a phosphate compound, A hydrothermally stable porous molecular sieve catalyst obtained by evaporating water from a raw material mixture containing is described. This catalyst is described as having high hydrothermal resistance and improving gas olefin yield and selectivity.
  • Patent Document 4 discloses fine spherical particles obtained by spray-drying an aqueous slurry of a mixture of air-flow calcined alumina, clay containing silica and alumina as a main component, a precursor of a silica-based inorganic oxide and crystalline aluminosilicate, and an alkali metal. It describes a method for producing a catalytic cracking catalyst in which a rare earth is introduced after washing so that the oxide content is 1.0% by mass or less as an oxide. It is described that when this catalyst is used for catalytic cracking of heavy hydrocarbon oils containing a large amount of metal, it exhibits high cracking activity, high gasoline selectivity, low production of coke and gas, and high hydrothermal resistance. ing.
  • Patent Document 5 discloses a catalyst for fluid catalytic cracking of hydrocarbon oil obtained by mixing two or more catalyst compositions containing zeolite and an inorganic oxide matrix composed of an active matrix component and an inert matrix component, Each catalyst composition has a different zeolite content (however, one catalyst composition includes a case where the zeolite content is 0), and a catalyst for fluid catalytic cracking of hydrocarbon oil, Is described.
  • gasoline and middle distillate can be obtained in high yield
  • coke can be produced in low yield
  • bottom resolution can be increased, that is, the yield of heavy fraction can be lowered. It is stated that you can.
  • Patent Document 6 discloses a catalyst composition A containing 10 to 30% by mass of a silica-based binder as zeolite and a binder, and a catalyst composition B containing 10 to 30% by mass of an aluminum compound binder as a binder and binder.
  • the weight of the catalyst composition a and W a, the weight of the catalyst composition B as W B, the mass ratio (W a: W B) is 10: 90-90: it was mixed in any proportion in 1:10
  • a catalyst for fluid catalytic cracking of hydrocarbon oils is described. According to this catalyst, gasoline and light oil fractions can be obtained in high yield, coke can be produced in low yield, and bottom resolution can be increased, that is, production of heavy fractions can be suppressed. It is described.
  • FIG. 3 A schematic diagram of such a microactivity test method is shown in FIG.
  • 31 is a fixed bed catalyst layer, and the raw material oil is inserted into the reactor together with the purge gas led out from the purge supply line 33 via the raw material oil supply nozzle 32 and the raw material oil supply pump.
  • the Reference numeral 35 denotes a heating furnace, and 36 denotes a thermocouple.
  • the contact time in a commercial catalytic cracking apparatus varies depending on the type of raw material hydrocarbon oil used, it is approximately several seconds, whereas in MAT, it is approximately 50 to 120 seconds.
  • the amount of catalyst used is very small at several grams.
  • FIG. 4 shows a schematic diagram of a pilot plant apparatus.
  • 41 is the bottom of the reaction tower
  • 42 is the top of the reaction tower
  • 43 is the feed oil supply line
  • 44 is the separator
  • 45 is the stripper
  • 46 is the lift line
  • 47 is the regeneration tower
  • 48 is the catalyst transport line
  • 49 is the catalyst.
  • a trap, 50 is a generated oil recovery tank
  • 51 is a fractionator
  • 52 is a generated gas.
  • the feedstock oil is introduced from the line 43 and the catalyst is introduced from the line 48 to the reaction tower bottom 41, and after catalytic cracking reaction, the product is distilled through 50 to 52.
  • Patent Document 7 discloses a test apparatus employing a small fluidized bed shown in FIG.
  • the catalyst is packed into the catalyst fluidized bed reactor 21
  • feedstock oil and the like are supplied from the feedstock 22 for the feedstock oil and dispersed gas, and from the feed gas supply nozzles and lines for the catalyst flow 23 and 23 ′, Flowing gas is supplied.
  • Reference numeral 24 denotes a discharge line for product gas and fluid gas.
  • it is a test apparatus which performs catalytic cracking reaction, detecting temperature with the thermocouple 26 in the heating furnace 25 provided in the reactor exterior.
  • the present applicant obtained the small test apparatus of Patent Document 7 and conducted various tests.
  • this apparatus has a catalyst filling amount of several grams and a contact time with the raw material hydrocarbon oil of about 60 to 120 seconds, and the test efficiency is good, but the deviation from the test result of the pilot plant is not necessarily small. In terms of the performance evaluation of the catalyst used in the actual apparatus, it was not necessarily sufficient.
  • the present inventors have provided a catalyst flow cell (1) isolated inside the reaction vessel (6) in a small test apparatus, and the catalyst is placed in this cell. Filling and supplying the catalyst flow gas from the upper part to make the catalyst in a fluid state, and supplying the reaction raw material hydrocarbon oil from the upper part to the flow catalyst area, the test result approximate to the test result in the pilot plant is obtained. As a result, the present invention has been completed.
  • a catalyst test apparatus for fluid catalytic cracking comprises a catalyst flow cell (1) inside, a catalyst flow cell (1), a reaction raw material supply nozzle (2) from above, and a catalyst flow gas. It is characterized by comprising a reaction vessel (6) provided with a supply nozzle (3) and provided with a product recovery line (5) at the bottom.
  • the catalyst flow cell (1) is cylindrical, the inner diameter (D I ) is in the range of 1 to 4 cm, the height (T) is in the range of 2 to 14 cm, and the height (T) and the inner diameter ( D is in the range ratio (T) / (D I) is 1.1 to 7.0 and I), it is preferable the bottom of the cell is conical structure concave down.
  • the inner volume of the catalyst flow cell (1) is preferably in the range of 5 to 40 ml.
  • the catalyst filling amount of the catalyst flow cell (1) during the test is preferably in the range of 1 to 20 g.
  • the average particle diameter of the catalyst is preferably in the range of 40 to 100 ⁇ m, and the bulk specific gravity is preferably in the range of 0.5 to 1.1 g / ml.
  • a reaction result very close to that of a pilot device for fluid catalytic cracking or a commercial catalytic cracking device can be obtained even if it is small, and the catalyst for fluid catalytic cracking is evaluated and extracted from the commercial catalytic cracking device. It is possible to provide a test apparatus for a catalyst for fluid catalytic cracking of hydrocarbon oil, which can be suitably used for catalyst evaluation and research and development.
  • mode of the catalyst test apparatus for fluid catalytic cracking concerning this invention is shown.
  • the schematic diagram of the small test apparatus of the fluidized bed disclosed by patent document 7 is shown.
  • 1 shows a schematic diagram of an ASTM-D3907 microactivity test apparatus defined by the American Society for Testing and Materials (ASTM).
  • ASTM-D3907 microactivity test apparatus defined by the American Society for Testing and Materials (ASTM).
  • ASTM-D3907 microactivity test apparatus defined by the American Society for Testing and Materials (ASTM).
  • ASTM-D3907 microactivity test apparatus defined by the American Society for Testing and Materials (ASTM).
  • the schematic diagram of the pilot plant of the fluidized bed which imitated the commercial catalytic cracking apparatus is shown.
  • a catalytic test apparatus for fluid catalytic cracking according to the present invention includes a catalyst flow cell (1) inside the catalyst flow cell (1), and a reaction raw material supply nozzle from above ( 2) and a gas supply nozzle (3) for catalyst flow, and a reaction vessel (6) provided with a product recovery line (5) at the bottom.
  • FIG. 1 shows a schematic diagram of one embodiment of a fluid catalytic cracking catalyst test apparatus according to the present invention.
  • FIG. 1 shows a catalyst flow cell 1, a reaction raw material supply nozzle 2, a raw material oil supply pump 2 ', a catalyst flow gas supply nozzle 3, a catalyst flow gas supply source 3', a nozzle support 4, and a product recovery line. 5, a reaction vessel 6, a heating furnace 7, and a thermocouple 8 are provided.
  • Catalyst flow cell (1) A predetermined catalytic cracking catalyst is inserted into the catalyst flow cell (1), and the catalyst is flowed to perform catalytic cracking of the introduced hydrocarbon oil.
  • the catalyst flow cell (1) is cylindrical and has a bottom at the bottom.
  • the bottom is preferably a concave conical or hemispherical structure.
  • Such a structure improves the reproducibility of the catalytic cracking test results for hydrocarbon oils, because the catalyst during the reaction is in a more uniform flow state than when the catalyst flow cell is prismatic or has a flat bottom.
  • a reaction result very close to that of the pilot device can be obtained.
  • the catalyst flow cell (1) is placed so that the inside of the cell can be isolated from the inside of the reaction vessel.
  • a jig or stopper for holding the catalyst flow cell may be provided on the outer surface or bottom of the cell, whereby the catalyst flow cell (1) is installed at a predetermined position in the reaction vessel.
  • the upper part of the cell for catalyst flow may be suspended from the nozzles (2) and (3) or the support (4) described later.
  • the inner diameter (D I ) of the cylindrical cell is preferably in the range of 1 to 4 cm, more preferably 1 to 3 cm.
  • the inner diameter (D I ) of the cylindrical cell is small, the flow state of the catalyst is deteriorated, and the measurement accuracy and reproducibility may be insufficient. Even if the inner diameter (D I ) of the cylindrical cell is too large, the mixing accuracy of the catalyst and hydrocarbon oil deteriorates due to insufficient lateral diffusion of the raw hydrocarbon oil. It tends to decrease or the decomposition becomes insufficient.
  • the height (T) of the cylindrical cell is preferably in the range of 2 to 14 cm, more preferably 3 to 12 cm.
  • the height (T) of the cylindrical cell means from the bottom of the cell to the top of the cell.
  • the ratio (T) / (D I ) between the height (T) and the inner diameter (D I ) is in the range of 1.1 to 7.0, more preferably 1.5 to 6.5. preferable.
  • the internal volume of the catalyst flow cell (1) is preferably in the range of 5 to 40 ml, more preferably 6 to 30 ml.
  • the internal volume of the catalyst flow cell (1) is in the above range, a suitable flow state can be obtained even with a small amount of catalyst charge, so the reproducibility of the catalytic cracking test result of hydrocarbon oil is improved. In addition, a reaction result very close to that of the pilot device can be obtained.
  • the amount of catalyst packed in the catalyst flow cell (1) during the test varies depending on the internal volume of the catalyst flow cell (1), the particle size distribution of the catalyst, the bulk density of the catalyst, etc. It is preferably in the range of 2 to 15 g.
  • the size of the catalyst flow cell (1) can be increased in proportion to the catalyst amount.
  • the test apparatus of the present invention is designed for the purpose of testing and developing a catalyst used in a commercial catalytic cracking apparatus.
  • the catalyst has an average particle diameter of 40 to 100 ⁇ m, preferably 50 to 80 ⁇ m. It is preferable.
  • the average particle diameter of the catalyst is not within the above range, a suitable catalyst flow state cannot be obtained, and the test accuracy may be insufficient.
  • the average particle diameter of the above catalyst was sieved at 20, 30, 45, 60, 75, 90, 105, and 150 ⁇ m by a dry micromesh sieve method, and the weight percent of each classified sample was determined, and the cumulative weight percent was plotted.
  • the 50% by weight value is defined as the average particle size.
  • the bulk specific gravity of the catalyst is preferably in the range of 0.5 to 1.1 g / ml, more preferably 0.6 to 1.0.
  • test accuracy may be insufficient because a suitable flow state cannot be obtained.
  • the bulk specific gravity of the catalyst is measured based on UOP Method 254-65.
  • the catalyst is calcined at 600 ° C. for 2 hours, cooled, poured into a 25 ml cylinder until the catalyst overflows, the overflowed catalyst is horizontally ground from the cylinder upper surface, and the weight of the catalyst is measured.
  • a filter can be provided at the uppermost part of the catalyst flow cell (1) to prevent the catalyst from scattering, and it can be used in combination with glass wool or the like.
  • Reaction raw material supply nozzle (2) A nozzle (2) for supplying the reaction raw material to the catalyst flow cell (1) is provided inside the cell.
  • the reaction raw material supply nozzle (2) is installed so that the tip thereof can flow in the catalyst flow cell (1) and the catalyst.
  • the nozzle is provided so that the tip of the nozzle is positioned at the center of the structure. It is preferable.
  • the tip of the reaction raw material supply nozzle (2) is at the center of the conical or hemispherical structure, the contact between the catalyst and the raw material hydrocarbon oil becomes more uniform, and the test accuracy is high.
  • the cross-sectional area of the tip of the reaction raw material supply nozzle (2) is preferably in the range of 0.1 to 4 mm 2 , more preferably 0.2 to 2 mm 2 .
  • the reaction raw material supply nozzle (2) When the cross-sectional area of the tip of the reaction raw material supply nozzle (2) is within the above range, the reaction raw material can be stably supplied and good test accuracy can be obtained.
  • reaction raw material supply (2) For the reaction raw material supply (2), the reaction raw material is introduced into the catalyst flow cell (2) by a pump or the like from an external reaction raw material supply source.
  • Gas supply nozzle for catalyst flow (3) A catalyst flow gas supply nozzle (3) from above is provided in the catalyst flow cell (1) together with the reaction raw material supply nozzle (2). In the catalytic reaction, a gas for catalyst flow is usually supplied to flow the catalyst.
  • the catalyst flow gas supply nozzle (3) is provided so that the tip of the nozzle is located at the center of the lower conical region or hemispherical region in order to increase the contact efficiency with the catalyst and the raw material oil. It is preferable.
  • the reaction raw material supply nozzle (2) and the catalyst flow gas supply nozzle (3) are preferably provided close to each other. When both are provided close to each other, the catalyst that has been in a suitable fluidized state by the fluidizing gas uniformly contacts the raw material hydrocarbon oil, so that good test accuracy can be obtained.
  • a double pipe is used, and an inner inner nozzle is used as a reaction raw material supply nozzle (2), and an outer outer pipe is used as a catalyst flow gas supply nozzle (3). It is preferable.
  • FIG. 1 shows an example of such a double pipe.
  • the reaction raw material supply nozzle (2) and the gas flow nozzle for catalyst flow (3) it is possible to supply the raw material hydrocarbon oil to the catalyst in a suitable flow state, which is good. Test accuracy can be obtained. Further, the fluidizing gas also has a role of uniformly dispersing and diffusing the raw material hydrocarbon oil, so that good test accuracy can be obtained.
  • the outer pipe of the double pipe can be used as the reaction raw material supply nozzle (2), and the inner pipe can be used as the gas flow supply nozzle for catalyst flow (3), but in this case, the mixed state of the catalyst and the raw material hydrocarbon oil is The test accuracy may be insufficient.
  • the reaction raw material supply nozzle (2) and the catalyst flow gas supply nozzle (3) can be appropriately designed and used so that a predetermined range of reaction raw material can be supplied and the catalyst can be in a uniform flow state. .
  • the cross-sectional area of the tip of the gas flow supply nozzle (3) for catalyst flow is preferably in the range of 0.2 to 8 mm 2 , more preferably 0.4 to 4 mm 2 .
  • the catalyst can be in a uniform flow state, and good test accuracy can be obtained.
  • Support (4) A support (4) is provided so that the reaction raw material supply nozzle (2) and the catalyst flow gas supply nozzle (3) can be fixed at predetermined positions.
  • the flow state of the catalyst can be kept constant, and the feed position of the raw hydrocarbon oil can be kept constant, so that excellent test accuracy can be obtained.
  • the support body of the cell (1) for catalyst flow is not shown in figure, it can be provided suitably.
  • a support in the form of hanging the catalyst flow cell (1) on the nozzles (2) and (3) can be provided.
  • Product recovery line (5) A product recovery line (5) is provided at the lower part of the reaction vessel (6).
  • the product (gaseous product, liquid product) and catalyst flow gas that are distilled at the start of the reaction in the catalyst flow cell are recovered from the product recovery line (5) and used for composition analysis and the like.
  • the reaction vessel (6) mainly contains the above-described catalyst flow cell (1), reaction raw material supply nozzle (2), catalyst flow gas supply nozzle (3) and support (4), and a product at the bottom. It has a recovery line (5).
  • the size, shape, and the like of the reaction vessel (6) are preferably such that the catalyst flow cell (1) can be contained and heated uniformly by a heating furnace (7) provided outside.
  • Heating furnace (7), temperature detector (8) An annular heating furnace (7) is provided so that the reaction vessel (6) can be inserted therein.
  • the heating furnace (7) is appropriately adjusted so as to maintain a predetermined reaction temperature.
  • the heating method is not particularly limited, and a well-known one can be adopted.
  • As the temperature detector a well-known one such as a thermocouple is usually used.
  • the catalyst catalyst can be tested without particular limitation as long as it is a catalyst for fluid catalytic cracking of hydrocarbon oil. At this time, it is preferable that an average particle diameter and bulk specific gravity exist in the above-mentioned range.
  • the catalyst is obtained by spray-drying a mixed slurry of crystalline aluminosilicate zeolite, inorganic oxide matrix component, binder, clay mineral and the like disclosed in Patent Documents 5 and 6 (sometimes referred to as a fresh catalyst).
  • a catalyst extracted from a commercial catalytic cracking apparatus (sometimes referred to as an equilibrium catalyst) or the like can also be used.
  • a fresh catalyst it is preferable to measure in advance by hydrothermal treatment at about 650 to 850 ° C. to make it quasi-equilibrium. It is also possible to carry out measurement by supporting a metal component such as Ni, V, Fe, etc. contained in the equilibrium catalyst on a fresh catalyst and then quasi-equilibrium. In the case of an equilibrium catalyst, although it depends on the purpose of the test, it is usually tested by heating and baking to remove carbon.
  • Hydrocarbon oil (raw oil)
  • raw material oil vacuum distillation light oil, atmospheric distillation residual oil, vacuum distillation residual oil, deasphalted oil, light cycle oil (LCO), heavy cycle oil (HCO), or a mixed oil thereof can be used.
  • LCO light cycle oil
  • HCO heavy cycle oil
  • the catalyst flow cell (1) in the reaction vessel (6) is filled with a predetermined amount of catalyst, then the reaction vessel (6) is placed in the heating furnace (7), and then the flow gas Is supplied at a predetermined speed to fluidize the catalyst in the catalyst flow cell (1), and the temperature of the catalyst layer is raised to a predetermined reaction temperature.
  • the raw material oil is supplied from the reaction raw material supply nozzle (2) at a predetermined speed for a predetermined time to react.
  • the product While reacting, the product is recovered from the product recovery line (5) provided at the bottom of the reaction vessel (6), and the product gas and product oil are separated and quantified with a cooler cooled to -10 ° C. , Separating and quantifying each component contained in the product gas and product oil.
  • gas and hydrocarbons having 1 to 6 carbon atoms are separated and quantified by gas chromatography (manufactured by Shimadzu Corporation: GC-20B-3S).
  • GC-2014 gas chromatography
  • Example 1 Catalyst test apparatus for fluid catalytic cracking
  • the catalyst test apparatus for fluid catalytic cracking has the structure shown in FIG. 1, with the reaction vessel 6 having a height of 26 cm, an inner diameter of 2.2 cm, and the cell 1 having a height of 7.7 cm.
  • the inner diameter was 1.6 cm
  • the bottom was on a cone
  • the cone angle was 45 ° from the perpendicular.
  • the nozzle has a double tube structure, the cross-sectional area of the tip of the reaction raw material supply nozzle 2 is 1.1 mm 2 , and the cross-sectional area of the tip of the catalyst flow gas supply nozzle 3 is 2.4 mm 2 . there were.
  • the nozzle tip used was the one installed so as to be the central part of the cone bottom of the cell 1.
  • the catalyst flow cell has a cylindrical shape, an inner diameter (D 1 ) of 1.6 cm, a height (T) of 7.7 cm, and an internal volume of 14.4 ml.
  • the catalyst flow cell (1) of the fluid catalytic cracking catalyst test apparatus is filled with 4.8 g of the pseudo-equilibrium catalyst, and N 2 gas is supplied as a fluidizing gas at a rate of 30 ml (STP) / min. The temperature was raised to 550 ° C. while fluidizing. Then, the reaction (NO. 1) was performed under the following conditions.
  • the product is recovered from the product recovery line (5). Then, after the supply of the raw material hydrocarbon oil is completed, the reaction raw material supply nozzle (2) is 30 ml / min and the catalyst flow gas supply nozzle (3 The product remaining on the catalyst was recovered while supplying N 2 gas at a rate of 30 ml / min. Thereafter, the product gas and the produced oil were separated and quantified with a cooler cooled to ⁇ 10 ° C., and then each component contained in the produced gas and the produced oil was separated and quantified.
  • the catalyst was taken out from the catalyst flow cell (1), and the coke remaining on the catalyst was quantified with a carbon analyzer (EMIA-321V manufactured by Horiba, Ltd.). Based on the separation / quantification results, the conversion rate and the yield of each component were determined based on the following rules.
  • EMIA-321V manufactured by Horiba, Ltd.
  • Boiling range of gasoline 36 to 204 ° C
  • Boiling range of light cycle oil (LCO) 204 to 343 ° C
  • Reaction (NO.2) In the reaction (NO.1), 5.76 g of the catalyst was charged, and the raw material hydrocarbon oil was supplied at an oil passing rate of 0.096 g / sec for 10 seconds, and the catalyst / raw material hydrocarbon oil ratio (C / O): 6 , Space velocity (WHSV): 57 hr ⁇ 1 , reaction (NO. 2) was carried out in the same manner except that the reaction time was 10 sec, and the conversion rate and the yield of each component were determined.
  • reaction (NO.3) In the reaction (NO. 1), 6.72 g of catalyst was charged, and raw material hydrocarbon oil was supplied at an oil passing rate of 0.096 g / sec for 10 seconds, and the catalyst / raw material hydrocarbon oil ratio (C / O): 7 , Space velocity (WHSV): 49 hr ⁇ 1 , reaction (NO. 3) was carried out in the same manner except that the reaction time was 10 sec, and the conversion rate and the yield of each component were determined.
  • the diameter of the bottom of the reaction tower (41) is 1.28 cm
  • the diameter of the top of the reaction tower (42) is 0.94 cm at the bottom detail and 2.14 cm at the top thickest part
  • the total height of the reaction tower is 81.cm. It was 7 cm.
  • Fluid catalytic cracking catalyst A catalyst equilibrated in the same manner as in Example 1 was used.
  • Reaction test catalyst circulation type catalyst test equipment for fluid catalytic cracking manufactured by JGC Catalysts & Chemicals Co., Ltd .: Midget-2
  • the oil which mixed residual oil (DSAR) and desulfurization vacuum distillation light oil (DSVGO) by 1: 1 was supplied at the speed
  • the temperature was adjusted with an electric heater so that the temperature at the top of the reaction tower was 520 ° C. and the temperature at the bottom of the reaction tower was 550 ° C.
  • the catalyst passes through the stripper (45) and the lift line (46) and is transferred to the regeneration tower (47). While supplying air at a temperature of 680 ° C., the amount of coke on the regenerated catalyst is 0.05% by mass. Played back to be as follows. The regenerated catalyst was circulated through the reaction tower. *
  • the obtained product was recovered by separating it into product oil and product gas with a fractionator cooled to ⁇ 20 ° C., and then each component was separated and quantified.
  • reaction (NO.2) was performed under the conditions of a catalyst circulation rate of 70 g / min and a catalyst / raw material hydrocarbon oil ratio (C / O): 7.
  • the obtained product was separated and quantified in the same manner as in the reaction (NO. 1).
  • reaction (NO.3) was performed under the conditions of a catalyst circulation rate of 80 g / min and a catalyst / raw material hydrocarbon oil ratio (C / O): 8.
  • the obtained product was separated and quantified in the same manner as in the reaction (NO. 1).
  • Fluid catalytic cracking catalyst A catalyst equilibrated in the same manner as in Example 1 was used.
  • the temperature in the reactor was set to 550 ° C., and an oil obtained by mixing desulfurized atmospheric residual oil (DSAR) and desulfurized vacuum distilled gas oil (DSVGO) at 1: 1 as a raw material hydrocarbon oil at an oil feed rate of 0.0177 g / sec. Feeded for 75 seconds.
  • DSAR desulfurized atmospheric residual oil
  • DSVGO desulfurized vacuum distilled gas oil
  • the space velocity (WHSV) 16 hr ⁇ 1
  • the reaction time is 75 sec.
  • the product was recovered from the product recovery line, and then after the feed of the raw material hydrocarbon oil was completed, N 2 gas was supplied to the reaction raw material feed nozzle (32) under the condition of 30 ml and remained on the catalyst. The product was recovered. Thereafter, the product gas and the produced oil were separated and quantified with a cooler cooled to ⁇ 10 ° C., and then each component contained in the produced gas and the produced oil was separated and quantified.
  • the catalyst was taken out from the catalyst flow cell (1), and the coke remaining on the catalyst was quantified with a carbon analyzer (EMIA-321V manufactured by Horiba, Ltd.).
  • EMIA-321V manufactured by Horiba, Ltd.
  • reaction (NO.2) In the reaction (NO. 1), the feed rate of the raw hydrocarbon oil remains 0.0177 g / sec, the feed time is 64.4 seconds, and the catalyst / raw hydrocarbon oil ratio (C / O): 3.5
  • the reaction (NO. 2) was carried out in the same manner except that the reaction time was 64.4 sec, and the conversion rate and the yield of each component were determined.
  • reaction (NO.3) In the reaction (NO. 1), the feed rate of the raw hydrocarbon oil remains 0.0177 g / sec, the feed time is 56.4 seconds, the catalyst / raw hydrocarbon oil ratio (C / O): 4, the reaction The reaction (NO. 3) was carried out in the same manner except that the time was 56.4 sec, and the conversion rate and the yield of each component were determined.
  • the reactor 21 has a lower inner diameter of 1.58 cm, an upper inner diameter of 2.29 cm and an overall height of 38.4 cm.
  • the raw material supply partial cross-sectional area of the raw material oil and the gas supply nozzle 22 for dispersion is 0.2 mm 2 use gas supply unit divided area was 1.8 mm 2.
  • Fluid catalytic cracking catalyst A catalyst equilibrated in the same manner as in Example 1 was used.
  • the temperature in the reactor was set to 550 ° C., and an oil obtained by mixing desulfurized atmospheric residual oil (DSAR) and desulfurized vacuum distilled light oil (DSVGO) at a ratio of 1: 1 as a raw material hydrocarbon oil at a feed rate of 0.02 g / sec. Feeded for 120 seconds.
  • the space velocity (WHSV): 8 hr ⁇ 1 the reaction time is 120 sec.
  • the product was recovered from the product recovery line (24). Then, after the supply of the raw hydrocarbon oil was completed, N 2 gas was supplied to recover the product on the catalyst. The recovered product was separated and quantified into product gas and product oil with a cooler cooled to ⁇ 15 ° C., and then each component contained in the product gas and product oil was separated and quantified. Thereafter, the temperature of the reactor was raised to 700 ° C. in an air atmosphere, and the coke was quantified with a carbon analyzer (1440D manufactured by Servomex) while burning the coke remaining in the catalyst.
  • a carbon analyzer (1440D manufactured by Servomex
  • reaction (NO.2) In the reaction (NO. 1), the feed rate of the raw hydrocarbon oil remains at 0.02 g / sec, the feed time is 90 seconds, the catalyst / raw hydrocarbon oil ratio (C / O): 5, and the reaction time:
  • the reaction (NO. 2) was conducted in the same manner except that the period was 90 sec, and the conversion rate and the yield of each component were determined.
  • reaction (NO.3) In the reaction (NO. 1), the feed rate of the raw hydrocarbon oil remains at 0.02 g / sec, the feed time is 75 seconds, the catalyst / raw hydrocarbon oil ratio (C / O): 6, and the reaction time: The reaction (NO.3) was carried out in the same manner except for 75 sec, and the conversion rate and the yield of each component were determined.
  • test apparatus of Example 1 had a small difference from the test result of Reference Example 1 of the pilot test apparatus, and showed almost the same results as the pilot test apparatus.
  • comparative example 2 using the test apparatus of patent document 7 the difference with the test result of the reference example 1 was large by LPG and a gasoline production rate.
  • test apparatus of the present invention If the test apparatus of the present invention is employed, the evaluation of the fluid catalytic cracking catalyst in the commercial catalytic cracking apparatus and the evaluation of the catalyst extracted from the commercial catalytic cracking apparatus can be performed with a small scale test apparatus. For this reason, it is a test apparatus that can greatly contribute to the research and development of catalytic cracking catalysts.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Materials Engineering (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Health & Medical Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Immunology (AREA)
  • Biochemistry (AREA)
  • General Health & Medical Sciences (AREA)
  • General Physics & Mathematics (AREA)
  • Analytical Chemistry (AREA)
  • Pathology (AREA)
  • General Chemical & Material Sciences (AREA)
  • Fluid Mechanics (AREA)
  • Food Science & Technology (AREA)
  • Medicinal Chemistry (AREA)
  • Molecular Biology (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Abstract

Cette invention concerne un dispositif permettant de tester un catalyseur destiné à être utilisé dans le craquage catalytique fluide d'une huile hydrocarbonée, qui est capable de donner des résultats de réaction extrêmement similaires à ceux obtenus par un dispositif pilote pour le craquage catalytique fluide ou un dispositif de craquage catalytique fluide à usage commercial (dispositif réel), et qui peut être utilisé pour l'évaluation d'un catalyseur destiné à être utilisé dans le craquage catalytique fluide et l'évaluation et la recherche/développement d'un catalyseur retiré d'un dispositif de craquage catalytique fluide à usage commercial. Le dispositif permettant de tester un catalyseur destiné à être utilisé dans le craquage catalytique fluide selon l'invention est caractérisé en ce qu'il comprend une cuve de réaction (6), ladite cuve de réaction (6) étant pourvue d'une cellule de fluidisation de catalyseur (1), d'une buse (2) pour introduire une matière réactionnelle par le dessus et d'une buse (3) pour introduire un gaz de fluidisation de catalyseur par le dessus, dans lequel la cellule de fluidisation du catalyseur (1) est logée à l'intérieur de la cuve de réaction (6) et les buses (2) et (3) sont montées sur la cellule de fluidisation du catalyseur (1), une conduite de collecte de produit (5) se situant au bas de la cuve de réaction (6).
PCT/JP2015/057693 2014-03-17 2015-03-16 Dispositif pour tester un catalyseur destiné à être utilisé dans le craquage catalytique fluide WO2015141624A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
SG11201607749YA SG11201607749YA (en) 2014-03-17 2015-03-16 Testing unit for fluid catalytic cracking catalyst
JP2016508716A JP6407967B2 (ja) 2014-03-17 2015-03-16 流動接触分解用触媒試験装置
KR1020167025938A KR102278260B1 (ko) 2014-03-17 2015-03-16 유동 접촉 분해용 촉매 시험 장치

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
JP2014053618 2014-03-17
JP2014-053618 2014-03-17

Publications (1)

Publication Number Publication Date
WO2015141624A1 true WO2015141624A1 (fr) 2015-09-24

Family

ID=54144592

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/JP2015/057693 WO2015141624A1 (fr) 2014-03-17 2015-03-16 Dispositif pour tester un catalyseur destiné à être utilisé dans le craquage catalytique fluide

Country Status (4)

Country Link
JP (1) JP6407967B2 (fr)
KR (1) KR102278260B1 (fr)
SG (1) SG11201607749YA (fr)
WO (1) WO2015141624A1 (fr)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2020528347A (ja) * 2017-07-28 2020-09-24 ハーテーエー・ゲーエムベーハー・ザ・ハイ・スループット・イクスペリメンテイション・カンパニー ０．１〜１０秒の範囲の滞留時間で化学物質を触媒転換するための装置および方法
WO2021213974A1 (fr) * 2020-04-20 2021-10-28 Hte Gmbh The High Throughput Experimentation Company Appareil et procédé d'observation de réactions catalysées de manière hétérogène
CN114433175A (zh) * 2020-10-19 2022-05-06 中国石油化工股份有限公司 一种高固含量催化剂制备方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3976433A (en) * 1974-12-11 1976-08-24 Atlantic Richfield Company Apparatus for catalytic conversion
US4419328A (en) * 1981-07-30 1983-12-06 Mobil Oil Corporation Controlled fluidized bed reactor for testing catalysts
JPH10121057A (ja) * 1996-10-17 1998-05-12 Idemitsu Kosan Co Ltd 触媒評価装置
JP2003193065A (ja) * 2001-11-29 2003-07-09 China Petrochemical Corp 接触分解反応再生システム
JP2004203914A (ja) * 2002-12-24 2004-07-22 Catalysts & Chem Ind Co Ltd 炭化水素用流動接触分解触媒の擬平衡化装置
JP2004528582A (ja) * 2001-06-05 2004-09-16 アクゾ　ノーベル　ナムローゼ　フェンノートシャップ Ｆｃｃ触媒の小規模試験方法

Family Cites Families (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS60193543A (ja) 1984-03-15 1985-10-02 Shokubai Kasei Kogyo Kk 炭化水素接触分解用触媒組成物の製造法
JPH0516908A (ja) 1990-11-15 1993-01-26 Nec Yamagata Ltd 電子部品のテーピング方法
JPH08173816A (ja) 1994-12-27 1996-07-09 Catalysts & Chem Ind Co Ltd 炭化水素の流動接触分解用触媒組成物および該組成物の製造方法
US6069012A (en) 1997-05-23 2000-05-30 Kayser Technology, Inc. Versatile fluidized bed reactor
WO2007043742A1 (fr) 2005-10-07 2007-04-19 Sk Energy Co., Ltd. Catalyseur a tamis moleculaire microporeux a stabilite hydrothermique et procede d'elaboration
JP5628027B2 (ja) 2008-05-30 2014-11-19 日揮触媒化成株式会社 炭化水素油の流動接触分解触媒及びそれを用いた炭化水素油の流動接触分解方法
JP5390833B2 (ja) 2008-11-06 2014-01-15 日揮触媒化成株式会社 炭化水素油の流動接触分解触媒

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3976433A (en) * 1974-12-11 1976-08-24 Atlantic Richfield Company Apparatus for catalytic conversion
US4419328A (en) * 1981-07-30 1983-12-06 Mobil Oil Corporation Controlled fluidized bed reactor for testing catalysts
JPH10121057A (ja) * 1996-10-17 1998-05-12 Idemitsu Kosan Co Ltd 触媒評価装置
JP2004528582A (ja) * 2001-06-05 2004-09-16 アクゾ　ノーベル　ナムローゼ　フェンノートシャップ Ｆｃｃ触媒の小規模試験方法
JP2003193065A (ja) * 2001-11-29 2003-07-09 China Petrochemical Corp 接触分解反応再生システム
JP2004203914A (ja) * 2002-12-24 2004-07-22 Catalysts & Chem Ind Co Ltd 炭化水素用流動接触分解触媒の擬平衡化装置

Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2020528347A (ja) * 2017-07-28 2020-09-24 ハーテーエー・ゲーエムベーハー・ザ・ハイ・スループット・イクスペリメンテイション・カンパニー ０．１〜１０秒の範囲の滞留時間で化学物質を触媒転換するための装置および方法
WO2021213974A1 (fr) * 2020-04-20 2021-10-28 Hte Gmbh The High Throughput Experimentation Company Appareil et procédé d'observation de réactions catalysées de manière hétérogène
CN114433175A (zh) * 2020-10-19 2022-05-06 中国石油化工股份有限公司 一种高固含量催化剂制备方法
CN114433175B (zh) * 2020-10-19 2023-09-05 中国石油化工股份有限公司 一种高固含量催化剂制备方法

Also Published As

Publication number Publication date
JPWO2015141624A1 (ja) 2017-04-06
KR20160135727A (ko) 2016-11-28
KR102278260B1 (ko) 2021-07-15
JP6407967B2 (ja) 2018-10-17
SG11201607749YA (en) 2016-11-29

Similar Documents

Publication Publication Date Title
US10357761B2 (en) Catalyst for fluidized catalytic cracking and method for fluidized catalytic cracking
US8845882B2 (en) High light olefins FCC catalyst compositions
ES2682257T3 (es) Aditivos para maximización de olefinas ligeras en unidades de craqueamiento catalítico fluido y proceso
US9415380B2 (en) Method for manufacturing catalytic cracking catalyst for hydrocarbon oil
KR100783987B1 (ko) 열적으로 안정한, 고표면적의 개질된 메조다공성알루미노포스페이트
JP6407967B2 (ja) 流動接触分解用触媒試験装置
JP5904922B2 (ja) 炭化水素油の接触分解触媒及び炭化水素油の接触分解方法
WO2013077836A1 (fr) Passivant de métaux/piège à métaux amélioré pour processus fcc
JP2020520798A (ja) ボトムアップグレーディングおよび低コークス流動接触分解触媒
JP7046763B2 (ja) 炭化水素油用流動接触分解触媒
JP6719980B2 (ja) 鉄堆積流動接触分解用触媒の再活性化方法、再活性化装置、流動接触分解方法
JP6327709B2 (ja) 炭化水素油の接触分解触媒および炭化水素油の接触分解方法
JP6234829B2 (ja) 重質油の流動接触分解法
RU2554884C1 (ru) Способ приготовления катализатора крекинга вакуумного газойля с регулируемым выходом олефинов с3 и с4
JPS60143834A (ja) 炭化水素供給油転化方法
JP5947797B2 (ja) 生成物分布を改善するための触媒変成処理
JP6329436B2 (ja) 重質油の流動接触分解法
JP2019089907A (ja) 軽質オレフィンの製造方法
JP2013537926A5 (fr)
US20160090538A1 (en) Apparatuses and methods for fluid catalytic cracking with limited particulate emissions
US9283533B1 (en) Catalyst regenerators and methods for regenerating catalysts
JP2008173529A (ja) 炭化水素油の接触分解触媒及び該触媒を用いる炭化水素油の接触分解方法

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 15764273

Country of ref document: EP

Kind code of ref document: A1

ENP Entry into the national phase

Ref document number: 2016508716

Country of ref document: JP

Kind code of ref document: A

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 20167025938

Country of ref document: KR

Kind code of ref document: A

WWE Wipo information: entry into national phase

Ref document number: IDP00201606875

Country of ref document: ID

122 Ep: pct application non-entry in european phase

Ref document number: 15764273

Country of ref document: EP

Kind code of ref document: A1