CN101481626B - Process for producing spherical coke by cracking heavy oil - Google Patents
Process for producing spherical coke by cracking heavy oil Download PDFInfo
- Publication number
- CN101481626B CN101481626B CN 200810000613 CN200810000613A CN101481626B CN 101481626 B CN101481626 B CN 101481626B CN 200810000613 CN200810000613 CN 200810000613 CN 200810000613 A CN200810000613 A CN 200810000613A CN 101481626 B CN101481626 B CN 101481626B
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- China
- Prior art keywords
- riser tube
- spherical coke
- gas
- heavy oil
- coke
- 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.)
- Expired - Fee Related
Links
- 239000000571 coke Substances 0.000 title claims abstract description 24
- 239000000295 fuel oil Substances 0.000 title claims abstract description 24
- 238000000034 method Methods 0.000 title claims abstract description 13
- 238000005336 cracking Methods 0.000 title claims description 11
- 239000003921 oil Substances 0.000 claims abstract description 13
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 239000007787 solid Substances 0.000 claims abstract description 12
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 8
- 239000003546 flue gas Substances 0.000 claims abstract description 8
- 239000007789 gas Substances 0.000 claims abstract description 7
- 238000000197 pyrolysis Methods 0.000 claims abstract description 7
- 230000005484 gravity Effects 0.000 claims abstract description 4
- 239000003595 mist Substances 0.000 claims abstract description 4
- 239000002245 particle Substances 0.000 claims description 6
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims description 3
- 238000009834 vaporization Methods 0.000 claims description 3
- 230000008016 vaporization Effects 0.000 claims description 3
- 230000001737 promoting effect Effects 0.000 claims description 2
- 238000004939 coking Methods 0.000 abstract description 5
- 239000003208 petroleum Substances 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 238000006243 chemical reaction Methods 0.000 description 3
- 238000004523 catalytic cracking Methods 0.000 description 2
- 238000007233 catalytic pyrolysis Methods 0.000 description 2
- 238000005261 decarburization Methods 0.000 description 2
- 239000002283 diesel fuel Substances 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000005984 hydrogenation reaction Methods 0.000 description 2
- 238000007670 refining Methods 0.000 description 2
- 241000772415 Neovison vison Species 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 238000010420 art technique Methods 0.000 description 1
- 230000004888 barrier function Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 239000003054 catalyst Substances 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 239000003317 industrial substance Substances 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention provides a technique for making spherical coke by heavy oil pyrolysis. The heavy oil which is preheated to 150-340 DEG C is injected into the bottom of a jetting bed from a feed inlet at the lower part of the jetting bed by an efficient atomizing nozzle, and oil mist is heated, vaporized and cracked by high temperature spherical coke jetted at 550-950 DEG C; oil gas flows out from the top of the jetting bed and then enters a fractionating tower separation system after gas-solid separation, and the high temperature spherical coke flowing out from the side is processed by steam stripping by a stripper and enters a riser tube coking device to be scorched by air; the large grained spherical coke is discharged from the bottom of a riser tube by virtue of gravity, and the small grained spherical coke is risen to the top of the riser tube coking device by flue gas for gas-solid separation; after heat exchange, the separated flue gas is discharged outside, and the high temperature small grained spherical coke returns to the bottom of the jetting bed from a dipleg of a gas-solid separator and can be taken as a heat source of heavy oil pyrolysis for cycle use.
Description
1. technical field
The invention provides a kind of process for producing spherical coke by cracking heavy oil, belong to petrochemical industry.
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, temperature of reaction is low approximately 500 ℃-650 ℃, higher to the heavy oil ingredient requirement, do not reach fully effectively utilizing petroleum resources; Flexicoking and fluid coking temperature of reaction are low approximately 350 ℃-600 ℃, 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, approximately 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.How most economical, cleaning, the most reasonable and good these non-renewable petroleum resources of maximum using have become the urgent key subjects to be solved of China's oil worker.
3. summary of the invention
The invention provides a kind of process for producing spherical coke by cracking heavy oil.To be preheating to 150 ℃-340 ℃ heavy oil sprays into spouted bed device from the underfeed mouth of spouted bed bioreactor bottom with high-efficiency atomizing nozzle, mist of oil is by 550 ℃-950 ℃ spouted heating of high temperature spherical coke, vaporization and cracking; Oil gas flows out to go forward side by side from the top of spouted bed bioreactor and goes the separation column separation system after promoting the circulation of qi separates admittedly, and the high temperature spherical coke that flows out from the side enters riser tube and burns device and carry out air and burn behind the stripper stripping; Large granular spherical is burnt to be relied on gravity to burn the device bottom from riser tube to discharge, and the small-particle spherical coke is risen to the top that riser tube burns device by flue gas and carries out gas solid separation; Efflux behind the isolated flue gas heat exchange, high temperature small-particle spherical coke returns the bottom of spouted reactor from the gas-solid separator dipleg, as the heat-source Cycles use of heavy oit pyrolysis.
Riser tube burns device and is comprised of the fluidized-bed of bottom and riser tube two portions of middle and upper part.
4, description of drawings
Accompanying drawing is process flow sheet of the present invention.
Wherein: the 1-high-efficiency atomizing nozzle, the spouted bed bioreactor of 2-, the spouted bed of 3-gas-solid separator, the 4-stripper, the 5-riser tube burns device, the 6-fluidized-bed, the 7-riser tube, 8-riser tube gas-solid separator, the 9-dipleg,, the 10-interchanger
5. embodiment
The present invention will be described in detail below in conjunction with accompanying drawing: will be preheating to 150 ℃-340 ℃ heavy oil sprays into spouted bed device 2 from the underfeed mouth of spouted bed bioreactor 2 bottom with high-efficiency atomizing nozzle 1, mist of oil is by 550 ℃-950 ℃ spouted heating of high temperature spherical coke, vaporization and cracking; Oil gas from the top of spouted bed bioreactor 2 flow out and separation through spouted bed gas-solid separator 3 after go the separation column separation system, the high temperature spherical coke that flows out from the side enters riser tube and burns device 5 and carry out air and burn behind stripper 4 strippings; The burnt gravity that relies on of large granular spherical burns the discharge of device 5 bottoms from riser tube, and the small-particle spherical coke is risen to riser tube by flue gas and burns the top of device 5 through the separation of riser tube gas-solid separator 8; Isolated flue gas effluxes after interchanger 10 heat exchange, and high temperature small-particle spherical coke returns the bottom of spouted reactor 2 from riser tube gas-solid separator dipleg 9, as the heat-source Cycles use of heavy oit pyrolysis.
Riser tube burns device 5 and is comprised of the fluidized-bed 6 of bottom and riser tube 7 two portions of middle and upper part.
Claims (2)
1. process for producing spherical coke by cracking heavy oil, it is characterized in that will being preheating to 150 ℃-340 ℃ heavy oil sprays into spouted bed bioreactor from the underfeed mouth of spouted bed bioreactor bottom with high-efficiency atomizing nozzle, mist of oil is by 550 ℃-950 ℃ spouted heating of high temperature spherical coke, vaporization and cracking; Oil gas flows out to go forward side by side from the top of spouted bed bioreactor and goes the separation column separation system after promoting the circulation of qi separates admittedly, and the high temperature spherical coke that flows out from the side enters riser tube and burns device and carry out air and burn behind the stripper stripping; Large granular spherical is burnt to be relied on gravity to burn the device bottom from riser tube to discharge, and the small-particle spherical coke is risen to the top that riser tube burns device by flue gas and carries out gas solid separation; Efflux behind the isolated flue gas heat exchange, high temperature small-particle spherical coke returns the bottom of spouted bed bioreactor from the gas-solid separator dipleg, as the heat-source Cycles use of heavy oit pyrolysis.
2. a kind of process for producing spherical coke by cracking heavy oil that provides according to claim 1 is characterized in that riser tube burns device and is comprised of the fluidized-bed of bottom and riser tube two portions of middle and upper part.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200810000613 CN101481626B (en) | 2008-01-11 | 2008-01-11 | Process for producing spherical coke by cracking heavy oil |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 200810000613 CN101481626B (en) | 2008-01-11 | 2008-01-11 | Process for producing spherical coke by cracking heavy oil |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101481626A CN101481626A (en) | 2009-07-15 |
| CN101481626B true CN101481626B (en) | 2013-10-23 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 200810000613 Expired - Fee Related CN101481626B (en) | 2008-01-11 | 2008-01-11 | Process for producing spherical coke by cracking heavy oil |
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| Country | Link |
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Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN105586079B (en) * | 2014-10-21 | 2017-11-03 | 中国石油化工股份有限公司 | A kind of heavy oil coking method |
| CN105586078B (en) * | 2014-10-21 | 2017-11-03 | 中国石油化工股份有限公司 | A kind of heavy oil coking method |
| EP3765579A4 (en) * | 2018-03-13 | 2021-11-17 | Lummus Technology LLC | In situ coking of heavy pitch and other feedstocks with high fouling tendency |
| 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 |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB559026A (en) * | 1942-09-15 | 1944-02-01 | Standard Oil Dev Co | Improvements in or relating to the thermal conversion of hydrocarbon oils |
| US4097363A (en) * | 1976-07-12 | 1978-06-27 | Gulf Research & Development Company | Thermal cracking of light gas oil at high severity to ethylene |
| CN1069016A (en) * | 1992-07-16 | 1993-02-17 | 中国石油化工总公司 | The method of preparing ethene by direct conversion of heavy hydrocarbon |
| CN1600831A (en) * | 2003-09-25 | 2005-03-30 | 田原宇 | Technique of solid phase heat carrier for recycle cracking heavy oil and gasification technique |
-
2008
- 2008-01-11 CN CN 200810000613 patent/CN101481626B/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB559026A (en) * | 1942-09-15 | 1944-02-01 | Standard Oil Dev Co | Improvements in or relating to the thermal conversion of hydrocarbon oils |
| US4097363A (en) * | 1976-07-12 | 1978-06-27 | Gulf Research & Development Company | Thermal cracking of light gas oil at high severity to ethylene |
| CN1069016A (en) * | 1992-07-16 | 1993-02-17 | 中国石油化工总公司 | The method of preparing ethene by direct conversion of heavy hydrocarbon |
| CN1600831A (en) * | 2003-09-25 | 2005-03-30 | 田原宇 | Technique of solid phase heat carrier for recycle cracking heavy oil and gasification technique |
Non-Patent Citations (2)
| Title |
|---|
| 喷动床研究与进展;张翠宣等;《化工进展》;20021231;第21卷(第9期);第630-634页 * |
| 张翠宣等.喷动床研究与进展.《化工进展》.2002,第21卷(第9期),第630-634页. |
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| Publication number | Publication date |
|---|---|
| CN101481626A (en) | 2009-07-15 |
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