CN102942954A - Double-reaction-pipe heavy-oil alkaline catalytic cracking and gasification coupling technology - Google Patents
Double-reaction-pipe heavy-oil alkaline catalytic cracking and gasification coupling technology Download PDFInfo
- Publication number
- CN102942954A CN102942954A CN2012104667053A CN201210466705A CN102942954A CN 102942954 A CN102942954 A CN 102942954A CN 2012104667053 A CN2012104667053 A CN 2012104667053A CN 201210466705 A CN201210466705 A CN 201210466705A CN 102942954 A CN102942954 A CN 102942954A
- Authority
- CN
- China
- Prior art keywords
- oil
- gas
- reaction
- heavy oil
- gasification
- 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.)
- Pending
Links
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a double-reaction-pipe heavy-oil alkaline catalytic cracking and gasification coupling technology, which comprises the following steps that: a high-efficiency atomizing spray nozzle is used to spray heavy oil which is preheated to 180-350DEG C into the upper part of a downward reaction pipe, oil mist is mixed with 700-950DEG C high-temperature regenerated alkaline catalyst which flows downwards from a material returning device, and then the oil mist is heated, gasified and cracked; the oil mist and alkaline catalyst to be regenerated downwards and rapidly flow to the bottom of the downward reaction pipe for gas and solid separation; the oil mist enters a fractionating tower for separation, oil slurry returns back to heavy oil for cyclic use and other parts are output as products; the alkaline catalyst to be regenerated is stripped, enters the lower part of a lifting pipe gasification reactor and realizes gasification reaction with oxidant and steam, and after reaction temperature reaches 750-1000DEG C, the produced synthetic gas and the regenerated alkaline catalyst upwards and rapidly flow to a gas-solid separator at the upper part of the lifting pipe gasification reactor for gas-solid separation; and the separated high-temperature regenerated alkaline catalyst flows into the material returning device and is continuously used as solid carriers for circulation, and the synthetic gas is output as a product after heat exchange.
Description
1. technical field
The invention provides the cracking of double-reaction tube heavy oil base catalysis and gasification coupling technique, belong to the refining of petroleum field.
2. background technology
The heavy oil lighting is one of important topic of world refining of petroleum.Residual oil content is high in the most of crude oil of China, and lightweight oil content is low, and the introduction of the in recent years continuous growth of some mink cell focuses (viscous crude) output and the external heavy crude of part makes heavy oil lighting problem more outstanding in addition.The heavy oil upgrading method often has the methods such as catalytic cracking, solvent deasphalting, visbreaking, coking, thermally splitting, heavy-oil hydrogenation, generally speaking, nothing more than hydrogenation and decarburization two large classes, wherein heavy oil decarburization processing is the major way of current refining of petroleum, and the reasonable utilization of deviating from carbon does not obtain fine solution always.In heavy oil solid phase carrier circulation cracking technology, mainly contain heavy oil catalytic pyrolysis, flexicoking, fluid coking, heavy oil fluidized upgrading etc.Heavy oil catalytic pyrolysis is except the purpose product that obtains (petrol and diesel oil and alkene industrial chemicals), the carbon residue that the removes heat release of in revivifier, burning, part heatable catalyst is as the thermal source of cracking, a part is sent outside with heat collector heat-obtaining generation steam or is generated electricity, low about 500 ℃-650 ℃ of temperature of reaction, higher to the heavy oil ingredient requirement, do not reach fully effectively utilizing petroleum resources; Low about 450 ℃-600 ℃ of flexicoking and fluid coking temperature of reaction, it mainly is the wax tailings of producing coker gasoline, diesel oil and being used as fcc raw material, char combustion partly circulates and produces synthetic gas as thermal barrier, partial gasification, but pyrolysis time is long, and yield of light oil is lower; Heavy oil fluidized upgrading (such as the ART technique of Engelhardt moral exploitation, the HCC technique of Luoyang Petrochemical designing institute etc.) adopts the circulating fluidized bed technique similar to heavy oil catalytic cracking process, about 400 ℃-600 ℃ of temperature of reaction, pyrolysis time is short, yield of light oil is higher, but the carbon residue that removes is not utilized effectively always.
The relative an acidic catalyst of basic catalyst (such as FCC molecular sieve catalyst, ZSM-5) is adapted to Pintsch process alkene processed, is not afraid of the water vapour high temperature deactivation, be conducive to suppress coke and generate and the coke catalytic gasification, the cracking of heavy oil base catalysis has become a focus of heavy oil upgrading research.
Because national requirements for environmental protection is more and more higher, refining of petroleum enterprise needs again a large amount of hydrogen that light-end products are carried out hydrofining to satisfy qualified vehicle fuel with production in addition, but each Petrochemical Enterprises lacks a large amount of cheap sources of hydrogen at present.
How most economical, cleaning, the most reasonable and good heavy oil of maximum using are realized without scorification, will become the China's oil worker and compel key subjects to be solved.
3. summary of the invention
Purpose of the present invention is exactly the cracking of a kind of double-reaction tube heavy oil base catalysis and gasification coupling technique for the deficiency that overcomes existing Heavy Oil Processing Technology existence, can high produced in yields alkene and lightweight oil, can reduce again the gasification reaction temperature, obtain a large amount of cheap hydrogen resources, realize that heavy oil upgrading is without scorification.
Technical scheme of the present invention:
The objective of the invention is to circulate by basic catalyst solid double-reaction tube, high-temperature alkaline cracking catalyst heavy oil is produced alkene and lightweight oil, the synthetic gas hydrogen making is produced in the gasification of coking basic catalyst, utilize the steam gasification heat absorption to solve the difficult problem of basic catalyst reactivation heat surplus, less energy-consumption realizes that heavy oil upgrading is without scorification.It is characterized in that will be preheating to 180 ℃-350 ℃ heavy oil with high-efficiency atomizing nozzle sprays into descending reaction tubes top from descending reaction tubes opening for feed, mist of oil mixes heating, vaporization and cracking with 700 ℃ that flow down from material returning device-950 ℃ of high temperature regeneration basic catalysts; The downward high speed following current of oil gas and coking basic catalyst to be generated is carried out gas solid separation to the gas-solid quick disconnector of descending reaction tubes bottom; Oil gas advances separation column to be separated, and slurry oil returns heavy oil and recycles, and other are as output of products; Enter the reaction of riser tube gasifying reactor bottom and oxygenant and water vapour generating gasification behind the coking basic catalyst stripping to be generated, after 750 ℃-1000 ℃ of the temperature of reaction, the gas-solid separator that the synthetic gas of generation and regenerated alkaline catalyzer upwards flow at a high speed riser tube gasifying reactor top carries out gas solid separation; The high temperature regeneration basic catalyst that separates flows into material returning device and proceeds to circulate as solid carrier, and as output of products, realization less energy-consumption heavy oil is processed without scorification after the synthetic gas heat exchange.
Oxygenant is oxygen, air and oxygen-rich air.
The present invention is described in detail characteristics of the present invention with embodiment.
4. description of drawings
Accompanying drawing is process schematic representation of the present invention.
The drawing of accompanying drawing is described as follows:
1. synthetic gas separator, 2. material returning device, 3. high-efficiency atomizing nozzle, 4. descending reaction tubes, 5. gas-solid quick disconnector, 6. splitting gas outlet, 7. flow regulator, 8. steam-in, 9. oxidant inlet, 10. riser tube gasifying reactor, 11. interchanger, 12. syngas outlet
Below in conjunction with drawings and Examples in detail process characteristic of the present invention is described in detail.
5. embodiment
Embodiment 1, high-efficiency atomizing nozzle (3) will be preheating to 180 ℃-350 ℃ heavy oil and spray into descending reaction tubes (4) top from descending reaction tubes (4) opening for feed, mist of oil mixes heating, vaporization and cracking with 700 ℃ that flow down from material returning device (2)-950 ℃ of high temperature regeneration basic catalysts; The downward high speed following current of oil gas and coking basic catalyst to be generated is carried out gas solid separation to the gas-solid quick disconnector (5) of descending reaction tubes () bottom; Oil gas advances separation column from splitting gas outlet (6) to be separated, and slurry oil returns heavy oil and recycles, and other are as output of products; Enter riser tube gasifying reactor (10) bottom and the oxygen and the vapor generation gasification reaction that enter from vapour inlet (8) and oxidant inlet (9) by flow director (7) behind the coking basic catalyst stripping to be generated, after 750 ℃-1000 ℃ of the temperature of reaction, the synthetic gas separator (1) that the synthetic gas of generation and regenerated alkaline catalyzer upwards flow at a high speed riser tube gasifying reactor (10) top carries out gas solid separation; The high temperature regeneration basic catalyst that separates flows into material returning device (2) to be continued solid carrier and circulates, synthetic gas through interchanger (11) heat exchange after from syngas outlet (12) as output of products, realize that less energy-consumption heavy oil processes without scorification.
Double-reaction tube heavy oil base catalysis provided by the present invention cracking and gasification coupling technique, circulate by basic catalyst solid double-reaction tube, produce alkene and lightweight oil with descending reaction tubes high temperature super short contact time base catalysis cracking masout, olefin yields improves 10%-30% relatively; Utilize the riser tube gasifying reactor to carry out the gasification of coking basic catalyst and produce the synthetic gas hydrogen making, utilize the steam gasification heat absorption to solve the difficult problem of basic catalyst reactivation heat surplus, device structure is simple, coke burning degree is high, and temperature is low; Coking basic catalyst and high-temperature vapor and oxygenant carry the bed gasification and produce the synthetic gas hydrogen making, and the hydrogen cost reduces (being about 70%) greatly, and gasification intensity is large, and equipment volume is little, and steel consumption is low, and fixed investment reduces greatly; Atmospheric operation is simple, and the start-stop car is convenient, and continuity is good, and oil is planted strong adaptability; Petroleum resources obtain fully effectively utilizing, and less energy-consumption has realized that heavy oil processes without scorification.
Claims (2)
1. the cracking of double-reaction tube heavy oil base catalysis and gasification coupling technique, its technical characterictic is will be preheating to 180 ℃-350 ℃ heavy oil with high-efficiency atomizing nozzle to spray into descending reaction tubes top from descending reaction tubes opening for feed, mist of oil mixes heating, vaporization and cracking with 700 ℃ that flow down from material returning device-950 ℃ of high temperature regeneration basic catalysts; The downward high speed following current of oil gas and coking basic catalyst to be generated is carried out gas solid separation to the gas-solid quick disconnector of descending reaction tubes bottom; Oil gas advances separation column to be separated, and slurry oil returns heavy oil and recycles, and other are as output of products; Enter the reaction of riser tube gasifying reactor bottom and oxygenant and water vapour generating gasification behind the coking basic catalyst stripping to be generated, after 750 ℃-1000 ℃ of the temperature of reaction, the gas-solid separator that the synthetic gas of generation and regenerated alkaline catalyzer upwards flow at a high speed riser tube gasifying reactor top carries out gas solid separation; The high temperature regeneration basic catalyst that separates flows into material returning device and proceeds to circulate as solid carrier, after the synthetic gas heat exchange as output of products.
2. carry according to claim 1 the cracking of double-reaction tube heavy oil base catalysis and the gasification coupling technique stated, it is characterized in that oxygenant is oxygen, air and oxygen-rich air.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012104667053A CN102942954A (en) | 2012-11-16 | 2012-11-16 | Double-reaction-pipe heavy-oil alkaline catalytic cracking and gasification coupling technology |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012104667053A CN102942954A (en) | 2012-11-16 | 2012-11-16 | Double-reaction-pipe heavy-oil alkaline catalytic cracking and gasification coupling technology |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN102942954A true CN102942954A (en) | 2013-02-27 |
Family
ID=47725948
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2012104667053A Pending CN102942954A (en) | 2012-11-16 | 2012-11-16 | Double-reaction-pipe heavy-oil alkaline catalytic cracking and gasification coupling technology |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102942954A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104232147A (en) * | 2013-06-21 | 2014-12-24 | 中国科学院过程工程研究所 | Lightweight treatment process of heavy oil |
| CN108300508A (en) * | 2018-04-17 | 2018-07-20 | 中国石油大学(华东) | Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins coupling device |
| CN108424785A (en) * | 2018-04-17 | 2018-08-21 | 中国石油大学(华东) | Inferior heavy oil double-reaction tube alkalinity millisecond catalytic pyrolysis and gasification coupling technique |
| CN108485704A (en) * | 2018-04-17 | 2018-09-04 | 中国石油大学(华东) | Crude oil millisecond classification gas phase catalysis, which cracks and hydrogen combination is added to maximize, produces industrial chemicals technique |
| CN108504387A (en) * | 2018-04-17 | 2018-09-07 | 中国石油大学(华东) | Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins technique |
| CN108504386A (en) * | 2018-04-17 | 2018-09-07 | 中国石油大学(华东) | The heavy oil solid thermal carriers millisecond pyrolytic process strengthened based on small molecule hydrocarbon activation |
| CN112538371A (en) * | 2019-09-23 | 2021-03-23 | 中国石油大学(北京) | Heavy oil lightening coupling reaction device |
| CN112538377A (en) * | 2019-09-23 | 2021-03-23 | 中国石油大学(北京) | Method and device for coproducing synthesis gas by heavy oil contact lightening |
| CN112538367A (en) * | 2019-09-23 | 2021-03-23 | 中国石油大学(北京) | Heavy oil cracking-gasification coupling reaction device |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1504541A (en) * | 2002-12-03 | 2004-06-16 | 中国科学院大连化学物理研究所 | Catalyst for preparing olefin with arene as side product by hydrocarbon catalytic cracking, preparing method and uses thereof |
| CN1521234A (en) * | 2003-02-12 | 2004-08-18 | 田原宇 | Cyclic cracking and gasification technology for heavy oil solid heat carrier |
| CN102031137A (en) * | 2009-09-29 | 2011-04-27 | 中国石油化工股份有限公司 | Weak catalytic cracking processing method for residual oil |
-
2012
- 2012-11-16 CN CN2012104667053A patent/CN102942954A/en active Pending
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1504541A (en) * | 2002-12-03 | 2004-06-16 | 中国科学院大连化学物理研究所 | Catalyst for preparing olefin with arene as side product by hydrocarbon catalytic cracking, preparing method and uses thereof |
| CN1521234A (en) * | 2003-02-12 | 2004-08-18 | 田原宇 | Cyclic cracking and gasification technology for heavy oil solid heat carrier |
| CN102031137A (en) * | 2009-09-29 | 2011-04-27 | 中国石油化工股份有限公司 | Weak catalytic cracking processing method for residual oil |
Non-Patent Citations (1)
| Title |
|---|
| K.E.彼得斯: "《生物标志化合物指南（第二版·上册）》", 31 October 2011, 石油工业出版社 * |
Cited By (17)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104232147A (en) * | 2013-06-21 | 2014-12-24 | 中国科学院过程工程研究所 | Lightweight treatment process of heavy oil |
| CN104232147B (en) * | 2013-06-21 | 2016-04-13 | 中国科学院过程工程研究所 | A kind of heavy oil lightweight treatment technique |
| CN108300508A (en) * | 2018-04-17 | 2018-07-20 | 中国石油大学(华东) | Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins coupling device |
| CN108424785A (en) * | 2018-04-17 | 2018-08-21 | 中国石油大学(华东) | Inferior heavy oil double-reaction tube alkalinity millisecond catalytic pyrolysis and gasification coupling technique |
| CN108485704A (en) * | 2018-04-17 | 2018-09-04 | 中国石油大学(华东) | Crude oil millisecond classification gas phase catalysis, which cracks and hydrogen combination is added to maximize, produces industrial chemicals technique |
| CN108504387A (en) * | 2018-04-17 | 2018-09-07 | 中国石油大学(华东) | Heavy oil millisecond is classified gas phase catalysis and cracks producing light olefins technique |
| CN108504386A (en) * | 2018-04-17 | 2018-09-07 | 中国石油大学(华东) | The heavy oil solid thermal carriers millisecond pyrolytic process strengthened based on small molecule hydrocarbon activation |
| US20190316046A1 (en) * | 2018-04-17 | 2019-10-17 | China University Of Petroleum (East China) | Process of alkaline catalytic cracking of inferior heavy oil with double reaction tubes in milliseconds and gaseous coupling |
| CN108504386B (en) * | 2018-04-17 | 2020-04-28 | 中国石油大学(华东) | Millisecond pyrolysis process of heavy oil solid heat carrier based on small molecule hydrocarbon activation and reinforcement |
| CN108424785B (en) * | 2018-04-17 | 2020-09-15 | 中国石油大学(华东) | Alkaline millisecond catalytic cracking and gasification coupling process for double reaction tubes of inferior heavy oil |
| CN112538371A (en) * | 2019-09-23 | 2021-03-23 | 中国石油大学(北京) | Heavy oil lightening coupling reaction device |
| CN112538377A (en) * | 2019-09-23 | 2021-03-23 | 中国石油大学(北京) | Method and device for coproducing synthesis gas by heavy oil contact lightening |
| CN112538367A (en) * | 2019-09-23 | 2021-03-23 | 中国石油大学(北京) | Heavy oil cracking-gasification coupling reaction device |
| US11230671B2 (en) | 2019-09-23 | 2022-01-25 | China University Of Petroleum-Beijing | Coupling reaction apparatus for heavy oil pyrolysis-gasification |
| CN112538377B (en) * | 2019-09-23 | 2022-02-22 | 中国石油大学(北京) | Method and device for coproducing synthesis gas by heavy oil contact lightening |
| CN112538367B (en) * | 2019-09-23 | 2022-02-22 | 中国石油大学(北京) | Heavy oil cracking-gasification coupling reaction device |
| CN112538371B (en) * | 2019-09-23 | 2022-02-25 | 中国石油大学(北京) | Heavy oil lightening coupling reaction device |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN102942954A (en) | Double-reaction-pipe heavy-oil alkaline catalytic cracking and gasification coupling technology | |
| CN102653691B (en) | Device and method for preparing oxygen-containing liquid fuel by catalytically converting biological oil | |
| CN108587674B (en) | Millisecond pyrolysis-gasification coupling process for heavy oil double-reaction tube semicoke circulating bed | |
| CN108424785B (en) | Alkaline millisecond catalytic cracking and gasification coupling process for double reaction tubes of inferior heavy oil | |
| CN101544529B (en) | Method and equipment for pre-treatment of reaction produced gas in olefin preparation technology by oxygen-containing compounds | |
| CN104232147B (en) | A kind of heavy oil lightweight treatment technique | |
| JP6752399B2 (en) | Method and apparatus for producing aromatic hydrocarbons and olefins by coupling of catalytic hydrogenation and catalytic cracking of biological oils | |
| CN104140847B (en) | A kind of F-T synthesis petroleum naphtha upgrading produces the method for stop bracket gasoline | |
| CN103571530B (en) | Wax catalysis cracking is for the method for low-carbon alkene | |
| CN202912908U (en) | Heavy oil thermal cracking and gasification coupled double reaction tube circulating bed device | |
| CN102965139A (en) | Heavy oil pyrolysis and gasification device coupling combined type lifting pipe and downstream reactor | |
| CN102031135A (en) | Comprehensive processing and utilizing method for heavy oil | |
| US10508247B2 (en) | Process of maximizing production of chemical raw materials by gaseous phase catalytic cracking crude oil with multi-stages in milliseconds in combination with hydrogenation | |
| CN1521234A (en) | Cyclic cracking and gasification technology for heavy oil solid heat carrier | |
| CN109054875B (en) | Efficient biomass conversion method | |
| CN101481626B (en) | Process for producing spherical coke by cracking heavy oil | |
| CN1600831A (en) | Technique of solid phase heat carrier for recycle cracking heavy oil and gasification technique | |
| 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 | |
| CN202543163U (en) | Device for preparing oxygen-containing liquid fuel by performing catalytic conversion on bio oil | |
| CN106609151B (en) | A kind of method for producing low-carbon alkene | |
| CN110373231B (en) | Double-fluidized-bed double-particle heavy inferior fuel cracking and gasifying device and method | |
| CN103224808B (en) | Inferior heavy oil fluidization conversion technology | |
| CN110511773B (en) | Device and method for coupling biomass pyrolysis and catalytic cracking reaction | |
| CN102989409A (en) | Double-reaction-tube circulation bed device for heavy oil pyrolysis and gasification coupling |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C02 | Deemed withdrawal of patent application after publication (patent law 2001) | ||
| WD01 | Invention patent application deemed withdrawn after publication |
Application publication date: 20130227 |