CN108587674A - Heavy oil double-reaction tube semicoke circulation fluidized bed millisecond pyrolysis-gasification coupling technique - Google Patents

Heavy oil double-reaction tube semicoke circulation fluidized bed millisecond pyrolysis-gasification coupling technique Download PDF

Info

Publication number
CN108587674A
CN108587674A CN201810341313.1A CN201810341313A CN108587674A CN 108587674 A CN108587674 A CN 108587674A CN 201810341313 A CN201810341313 A CN 201810341313A CN 108587674 A CN108587674 A CN 108587674A
Authority
CN
China
Prior art keywords
gas
semicoke
oil
gasification
heavy oil
Prior art date
Legal status (The legal status 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 status listed.)
Granted
Application number
CN201810341313.1A
Other languages
Chinese (zh)
Other versions
CN108587674B (en
Inventor
田原宇
乔英云
张金弘
盖希坤
李大伟
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
China University of Petroleum East China
Original Assignee
China University of Petroleum East China
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 China University of Petroleum East China filed Critical China University of Petroleum East China
Priority to CN201810341313.1A priority Critical patent/CN108587674B/en
Publication of CN108587674A publication Critical patent/CN108587674A/en
Application granted granted Critical
Publication of CN108587674B publication Critical patent/CN108587674B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • C10G9/00—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils
    • C10G9/28—Thermal non-catalytic cracking, in the absence of hydrogen, of hydrocarbon oils with preheated moving solid material
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
    • C10J3/56—Apparatus; Plants
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/723—Controlling or regulating the gasification process
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0956—Air or oxygen enriched air
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0973—Water
    • C10J2300/0976—Water as steam
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
    • C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water

Abstract

The present invention provides heavy oil double-reaction tube semicoke circulation fluidized bed millisecond pyrolytic gasification coupling technique.The heavy oil of preheating is sprayed into downlink reaction tube top from downlink reaction tube feed inlet with high-efficiency atomizing nozzle, mist of oil is mixed, heats, vaporizes and is pyrolyzed with the high-temperature semi-coke millisecond flowed down from material returning device；The gas-solid quick disconnector progress gas solid separation of bottom of the tube is reacted in the downward high speed fair current of semicoke to downlink after oil gas and coking；Oil gas is detached into fractionating column, and slurry oil is returned to be used with heavy oil mixing circulation, other are as output of products；Semicoke enters riser gasification reactor lower part and oxidant and vapor generation gasification reaction after coking, and the synthesis gas and high-temperature semi-coke of generation flow upward to the classification gas-solid separator at the top of riser gasification reactor and carry out gas solid separation；Big-and-middle particle high-temperature semicoke flows into and participates in cycle, cracking masout at the top of downlink reaction tube, and small particles continue to participate in gasification reaction by circulation pipe back to riser gasification reactor lower part, and output of products is used as after synthesis gas heat exchange.

Description

Heavy oil double-reaction tube semicoke circulation fluidized bed millisecond pyrolysis-gasification coupling technique
1. technical field
The present invention provides heavy oil double-reaction tube semicoke circulation fluidized bed millisecond pyrolysis-gasification coupling technique, belongs to processing of heavy oil neck Domain.
2. background technology
Heavy oil lighting is one of the important topic of countries in the world today PETROLEUM PROCESSING.Residual oil contains in China's major part crude oil Amount is high, and lightweight oil content is low, some mink cell focus (viscous crude) yield constantly increase and the external heavy crude in part in recent years in addition Introduction keeps heavy oil lighting problem more prominent.Processing of heavy oil method often has catalytic cracking, solvent deasphalting, visbreaking, coking, heat The methods of cracking, heavy-oil hydrogenation, generally speaking, nothing more than hydrogen and decarburization two major classes is added, wherein heavy oil decarburization processing is current stone The major way of oil refining, reasonable utilize for deviating from carbon are not solved always very well.Cracking work is recycled in heavy oil solid phase carrier Mainly there are heavy oil catalytic pyrolysis, flexicoking, fluid coking, heavy oil fluidized modification etc. in skill.Heavy oil catalytic cracking is removed and is obtained Purpose product (petrol and diesel oil and alkene industrial chemicals) outside, the carbon residue of removing combustion heat release in a regenerator, a part of heatable catalytic Heat source of the agent as cracking, a part take heat to generate steam and send outside or generate electricity with heat collector, relatively low about 500 DEG C of reaction temperature- 650 DEG C, more demanding to the carbon residue and content of beary metal of heavy oil feedstock, inferior heavy oil is difficult to meet the requirements；Inferior heavy oil is flexible Coking and fluid coking reaction temperature are low, about 450 DEG C -600 DEG C, mainly produce coker gasoline, diesel oil and are used as fcc raw material Wax tailings, char combustion part cycle generates synthesis gas as heat carrier, partial gasification, but pyrolysis time is long, lightweight Oil yield is relatively low；Inferior heavy oil fluidisation modification (such as ART techniques, the HCC techniques of Luoyang Petrochemical designing institute of Engelhardt moral exploitation Deng) use circulating fluidized bed technique similar with heavy oil catalytic cracking process, about 400 DEG C -600 DEG C of reaction temperature, pyrolysis time Short, yield of light oil is higher, but due to removing carbon left it is excessive, outside heat removing difficult design and limit popularization and application.
It is higher and higher additionally, due to national requirements for environmental protection, petroleum refining enterprise need again a large amount of hydrogen to light-end products into Row hydrofinishing meets qualified vehicle fuel to produce, but each Petrochemical Enterprises lack a large amount of cheap hydrogen sources at present.
How most economical, most cleaning most rationally and has maximally utilized heavy oil, realizes without scorification, will have become China's stone Oily worker compels key subjects to be solved.
3. invention content
The purpose of the present invention is exactly to overcome existing for existing Heavy Oil Processing Technology insufficient and to develop a kind of heavy oil double anti- Should pipe semicoke circulation fluidized bed millisecond pyrolysis-gasification coupling technique, light-end products can be produced and obtain a large amount of cheap hydrogen moneys Source realizes processing of heavy oil without scorification.
Technical scheme of the present invention：
The purpose of the present invention is by semicoke Double-tube cyclic, high-temperature semi-coke is pyrolyzed heavy oil and produces light-end products, after coking Semicoke partial gasification produces synthesis gas hydrogen making, is absorbed heat using steam gasification and solves semicoke riser combustive regeneration cycling hot Superfluous problem is measured, realizes processing of heavy oil without scorification.It is characterized in that 180 DEG C -350 DEG C of weight will be preheating to high-efficiency atomizing nozzle Oil sprays into downlink reaction tube top, mist of oil and 800 DEG C of -1100 DEG C of height flowed down from dual control material returning device from downlink reaction tube feed inlet Warm semicoke millisecond mixing, heating, vaporization and pyrolysis；The downward high speed fair current of semicoke reacts bottom of the tube to downlink after oil gas and coking Gas-solid quick disconnector carries out gas solid separation；Oil gas is detached from pyrolysis gas outlet into fractionating column, and slurry oil return is mixed with heavy oil to follow Ring uses, other pyrolysis petrol and diesel oils and liquefied gas and pyrolysis dry gas are exported as intermediate products；Lead to after semicoke stripping after coking Overcurrent amount controller enters riser gasification reactor lower part and gasification reaction, reaction temperature 850 occurs with oxidant and vapor After DEG C -1200 DEG C, the synthesis gas and high-temperature semi-coke of generation flow at a high speed the synthesis qi leel at the top of riser gasification reactor upwards Grade separator carries out gas solid separation；The big-and-middle particle high-temperature semicoke isolated flows into double regulation and control material returning devices, big-and-middle of part high temperature Grain semicoke flows into according to 1~10 tar ratio and participates in cycle, cracking masout at the top of downlink reaction tube, the big-and-middle particle of rest part half Burnt and small particles semi-coke powder continues to participate in gasification reaction, synthesis gas by circulation pipe back to riser gasification reactor lower part It is used as output of products after heat exchange, realizes that heavy oil is processed without scorification.
Oxidant is oxygen, air and oxygen-enriched air, preferably oxygen.
Synthesis gas classification separator is a kind of or more in inertia separator, horizontal inertia cyclone separator, vertical cyclone device The combination of kind.
Embodiment is described the features of the present invention by the present invention in detail.
4. description of the drawings
Attached drawing 1 is the process schematic representation of the present invention.
The drawing of attached drawing sets bright as follows：
1. synthesis gas classification separator, 2. dual control material returning devices, 3. high-efficiency atomizing nozzles, 4. downlink reaction tubes, 5. gas-solids are fast Fast separator, 6. pyrolysis gas outlets, 7. flow regulators, 8. steam inlets, 9. oxidant inlets, 10. riser gasification reactions Device, 11. heat exchangers, 12. syngas outlets, 13. circulation pipes
With reference to the accompanying drawings and examples come be described in detail the present invention process characteristic.
5. specific implementation mode
Embodiment 1, high-efficiency atomizing nozzle (3) will be preheating to 180 DEG C -350 DEG C of heavy oil from downlink reaction tube (4) feed inlet Downlink reaction tube (4) top is sprayed into, mist of oil and 800 DEG C of -1100 DEG C of high-temperature semi-coke milliseconds flowed down from dual control material returning device (2) are mixed It closes, heating, vaporize and be pyrolyzed, pyrolysis reaction temperature is 480 DEG C -850 DEG C；The downward high speed fair current of semicoke is arrived down after oil gas and coking The gas-solid quick disconnector (5) of row reaction tube (4) bottom carries out gas solid separation；Oil gas divides from pyrolysis gas outlet (6) into fractionating column From slurry oil is returned to be used with heavy oil mixing circulation, other pyrolysis petrol and diesel oils and liquefied gas and pyrolysis dry gas are as intermediate products Output；After coking after semicoke stripping by flow controller (7) enter riser gasification reactor (10) lower part with from steam Entrance (8) and oxidant inlet (9) enter the vapor that the oxygen that oxidant inlet (8) enters and steam entry (9) enter Gasification reaction occurs, after 850 DEG C -1200 DEG C of reaction temperature, the synthesis gas and high-temperature semi-coke of generation flow at a high speed riser upwards Synthesis gas classification separator (1) at the top of gasification reactor (10) carries out gas solid separation；The big-and-middle particle high-temperature semicoke isolated Double regulation and control material returning devices (2) are flowed into, high temperature big-and-middle particle semicoke in part flows into downlink reaction tube (4) according to 1~10 tar ratio and pushes up Portion participates in cycle, cracking masout, and the big-and-middle particle semicoke of rest part and small particles semi-coke powder are returned to by circulation pipe (13) Riser gasification reactor (10) lower part continues to participate in gasification reaction, synthesis gas is after heat exchanger (11) heat exchange from synthesis gas It exports (12) and is used as output of products, realize that heavy oil is processed without scorification.
Oxygen in embodiment 1 is changed to oxygen-enriched air by embodiment 2, other same.
Oxygen in embodiment 1 is changed to air by embodiment 3, other same.
Heavy oil double-reaction tube semicoke circulation fluidized bed millisecond pyrolysis-gasification coupling technique provided by the present invention, it is double by semicoke Pipe recycles, and light-end products, yield of light oil are produced with the heavy oil of downlink reaction tube high temperature super short contact time fast pyrogenation carbon residue 20% It is opposite to improve 10 percentage points or more；Burnt partial gasification, which is carried out, using riser gasification reactor produces synthesis gas hydrogen making, Solve the problems, such as that coal-char combustion circulated heat is superfluous using steam gasification heat absorption, device structure is simple, coke burning degree is high；Semicoke Riser gasification regeneration production synthesis gas hydrogen making is carried out with high-temperature vapor and oxidant, passes through the big-and-middle particle semicoke in part Solve coke gasification regeneration rate and heavy oil pyrolysis green coke rate not with small particles semi-coke powder circulation pipe returning charge cycle gasification Matched problem；Hydrogen cost substantially reduces (about 50%), and the intensity of gasification is big, and equipment volume is small, and steel consumption is low, fixed to throw Money substantially reduces；Atmospheric operation is simple, and driving and parking is convenient, and continuity is good, and oil kind is adaptable；Petroleum resources obtain fully effectively It utilizes, realizes heavy oil and processed without scorification.

Claims (3)

1. heavy oil double-reaction tube semicoke circulation fluidized bed millisecond pyrolysis-gasification coupling technique, technical characteristic is to use high-efficiency atomizing nozzle The heavy oil for being preheating to 180 DEG C -350 DEG C is sprayed into downlink reaction tube top from downlink reaction tube feed inlet, mist of oil is returned with from dual control The mixing of 800 DEG C of -1100 DEG C of high-temperature semi-coke milliseconds that glassware flows down, heating, vaporization and pyrolysis, pyrolysis reaction temperature is 480 DEG C - 850℃；The gas-solid quick disconnector progress gas-solid point of bottom of the tube is reacted in the downward high speed fair current of semicoke to downlink after oil gas and coking From；Oil gas is detached from pyrolysis gas outlet into fractionating column, and slurry oil is returned to be used with heavy oil mixing circulation, other pyrolysis petrol and diesel oils and liquid Change gas and pyrolysis dry gas is exported as intermediate products；Riser gasification is entered by flow controller after semicoke stripping after coking Gasification reaction occurs for reactor lower part and oxidant and vapor, after 850 DEG C -1200 DEG C of reaction temperature, the synthesis gas of generation and High-temperature semi-coke flows at a high speed the synthesis gas classification separator at the top of riser gasification reactor and carries out gas solid separation upwards；It isolates Big-and-middle particle high-temperature semicoke flow into double regulation and control material returning devices, high temperature big-and-middle particle semicoke in part is flowed into according to 1~10 tar ratio Cycle, cracking masout are participated at the top of downlink reaction tube, the big-and-middle particle semicoke of rest part and small particles semi-coke powder pass through cycle Pipe continues to participate in gasification reaction back to riser gasification reactor lower part, is used as output of products after synthesis gas heat exchange, realizes weight Oil is processed without scorification.
2. putting forward the heavy oil double-reaction tube semicoke circulation fluidized bed millisecond pyrolysis-gasification coupling technique stated, feature according to claim 1 It is that oxidant is one kind in oxygen, air and oxygen-enriched air.
3. putting forward the heavy oil double-reaction tube semicoke circulation fluidized bed millisecond pyrolysis-gasification coupling technique stated, feature according to claim 1 It is that synthesis gas classification separator is one or more in inertia separator, horizontal inertia cyclone separator, vertical cyclone device Combination.
CN201810341313.1A 2018-04-17 2018-04-17 Millisecond pyrolysis-gasification coupling process for heavy oil double-reaction tube semicoke circulating bed Active CN108587674B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201810341313.1A CN108587674B (en) 2018-04-17 2018-04-17 Millisecond pyrolysis-gasification coupling process for heavy oil double-reaction tube semicoke circulating bed

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201810341313.1A CN108587674B (en) 2018-04-17 2018-04-17 Millisecond pyrolysis-gasification coupling process for heavy oil double-reaction tube semicoke circulating bed

Publications (2)

Publication Number Publication Date
CN108587674A true CN108587674A (en) 2018-09-28
CN108587674B CN108587674B (en) 2020-09-15

Family

ID=63622780

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201810341313.1A Active CN108587674B (en) 2018-04-17 2018-04-17 Millisecond pyrolysis-gasification coupling process for heavy oil double-reaction tube semicoke circulating bed

Country Status (1)

Country Link
CN (1) CN108587674B (en)

Cited By (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112538367A (en) * 2019-09-23 2021-03-23 中国石油大学(北京) Heavy oil cracking-gasification coupling reaction device
CN112538382A (en) * 2019-09-23 2021-03-23 中国石油大学(北京) Integrated method and device for heavy oil catalytic cracking coupled coke catalytic gasification
CN112538376A (en) * 2019-09-23 2021-03-23 中国石油大学(北京) Integrated method and device for heavy oil cracking coupling coke catalytic gasification
CN112538381A (en) * 2019-09-23 2021-03-23 中国石油大学(北京) Method and device for co-production of heavy oil lightening and synthesis gas
CN112538370A (en) * 2019-09-23 2021-03-23 中国石油大学(北京) Method and device for coupling hydro-pressurized catalytic cracking of heavy oil with coke gasification
CN112538372A (en) * 2019-09-23 2021-03-23 中国石油大学(北京) Integrated method and device for co-producing synthesis gas by catalytic cracking of heavy oil
WO2021118741A1 (en) * 2019-12-11 2021-06-17 Exxonmobil Chemical Patents Inc. Processes and systems for converting a hydrocarbon-containing feed

Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102559240A (en) * 2012-01-17 2012-07-11 马俊杰 Dual-cycle mode catalytic cracking reaction regenerative system production technology and device
CN102965138A (en) * 2012-11-16 2013-03-13 中国石油大学(华东) Double-reaction-tube semi-coke circulating bed pyrolysis, gasification and coupling process of heavy oil
US20130184510A1 (en) * 2012-01-13 2013-07-18 United Technologies Corporation Method for reducing coke deposition

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20130184510A1 (en) * 2012-01-13 2013-07-18 United Technologies Corporation Method for reducing coke deposition
CN102559240A (en) * 2012-01-17 2012-07-11 马俊杰 Dual-cycle mode catalytic cracking reaction regenerative system production technology and device
CN102965138A (en) * 2012-11-16 2013-03-13 中国石油大学(华东) Double-reaction-tube semi-coke circulating bed pyrolysis, gasification and coupling process of heavy oil

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
陈滨等: "《石油化工手册》", 31 May 1988, 化学工业出版社 *

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11230674B2 (en) 2019-09-23 2022-01-25 China University Of Petroleum-Beijing Integrated method and apparatus for catalytic cracking of heavy oil and production of syngas
CN112538370A (en) * 2019-09-23 2021-03-23 中国石油大学(北京) Method and device for coupling hydro-pressurized catalytic cracking of heavy oil with coke gasification
CN112538367A (en) * 2019-09-23 2021-03-23 中国石油大学(北京) Heavy oil cracking-gasification coupling reaction device
CN112538381A (en) * 2019-09-23 2021-03-23 中国石油大学(北京) Method and device for co-production of heavy oil lightening and synthesis gas
US11230671B2 (en) 2019-09-23 2022-01-25 China University Of Petroleum-Beijing Coupling reaction apparatus for heavy oil pyrolysis-gasification
CN112538372A (en) * 2019-09-23 2021-03-23 中国石油大学(北京) Integrated method and device for co-producing synthesis gas by catalytic cracking of heavy oil
US11370978B2 (en) 2019-09-23 2022-06-28 China University Of Petroleum-Beijing Method and apparatus for integrating pressurized hydrocracking of heavy oil and coke gasification
CN112538367B (en) * 2019-09-23 2022-02-22 中国石油大学(北京) Heavy oil cracking-gasification coupling reaction device
CN112538376A (en) * 2019-09-23 2021-03-23 中国石油大学(北京) Integrated method and device for heavy oil cracking coupling coke catalytic gasification
CN112538382A (en) * 2019-09-23 2021-03-23 中国石油大学(北京) Integrated method and device for heavy oil catalytic cracking coupled coke catalytic gasification
US11230677B2 (en) 2019-09-23 2022-01-25 China University Of Petroleum-Beijing Method and device for heavy oil lightening and synthesis gas production
CN112538372B (en) * 2019-09-23 2022-02-22 中国石油大学(北京) Integrated method and device for co-producing synthesis gas by catalytic cracking of heavy oil
CN112538382B (en) * 2019-09-23 2022-02-22 中国石油大学(北京) Integrated method and device for heavy oil catalytic cracking coupled coke catalytic gasification
CN112538381B (en) * 2019-09-23 2022-02-25 中国石油大学(北京) Method and device for co-production of heavy oil lightening and synthesis gas
CN112538370B (en) * 2019-09-23 2022-02-25 中国石油大学(北京) Method and device for coupling hydro-pressurized catalytic cracking of heavy oil with coke gasification
CN112538376B (en) * 2019-09-23 2022-02-25 中国石油大学(北京) Integrated method and device for heavy oil cracking coupling coke catalytic gasification
WO2021118741A1 (en) * 2019-12-11 2021-06-17 Exxonmobil Chemical Patents Inc. Processes and systems for converting a hydrocarbon-containing feed

Also Published As

Publication number Publication date
CN108587674B (en) 2020-09-15

Similar Documents

Publication Publication Date Title
CN108587674A (en) Heavy oil double-reaction tube semicoke circulation fluidized bed millisecond pyrolysis-gasification coupling technique
CN102115675B (en) Heavy oil lightening method and device
CN108424785A (en) Inferior heavy oil double-reaction tube alkalinity millisecond catalytic pyrolysis and gasification coupling technique
CN103450922B (en) Heavy oil thermal conversion and green coke gasification method and integrated device
CN101328415A (en) Piston type fluidized bed low temperature dry distillation technological process
CN102942954A (en) Double-reaction-pipe heavy-oil alkaline catalytic cracking and gasification coupling technology
CN102234522A (en) Processing method and apparatus for converting heavy oil to light fractions
CN105316015A (en) Upper-heating down-moving low-temperature pyrolysis furnace for powdered coal and oil shale powder
CN202912908U (en) Heavy oil thermal cracking and gasification coupled double reaction tube circulating bed device
CN104531222B (en) Pyrolysis of coal system and method using spouted bed reactor
CN206033677U (en) Powder coal carbonization device
CN102965139A (en) Heavy oil pyrolysis and gasification device coupling combined type lifting pipe and downstream reactor
CN105018119A (en) External heating type descending low-temperature pyrolysis furnace for pulverized coal and oil shale powder
CN106947541B (en) Combined method and system for hydrogen production based on low-rank coal pyrolysis water vapor coke quenching water gas
CN206266493U (en) The system that a kind of coal is classified dual treatment
CN101481626B (en) Process for producing spherical coke by cracking heavy oil
CN107723031A (en) High-pressure gasification and pyrolysis integrated device for pulverized coal
CN102965138A (en) Double-reaction-tube semi-coke circulating bed pyrolysis, gasification and coupling process of heavy oil
CN202936381U (en) Heavy oil pyrolysis and gasification device with coupled combined type lifting pipe and downer reactor
CN110373231B (en) Double-fluidized-bed double-particle heavy inferior fuel cracking and gasifying device and method
CN210656802U (en) Hydrocarbon material pyrolysis and gasification coupling device
CN107858177A (en) A kind of coal fast pyrogenation and the integral system and method for gasification
CN203833881U (en) External heating vertical type descending low-temperature pyrolysis furnace for powdered coal or oil shale powder
CN103450923B (en) Heavy oil thermocontact lightening method
CN103224808B (en) Inferior heavy oil fluidization conversion technology

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant