CN100337737C - Hydrocarbon material catalytic cracking lift pipe reactor - Google Patents
Hydrocarbon material catalytic cracking lift pipe reactor Download PDFInfo
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- CN100337737C CN100337737C CNB2004100100186A CN200410010018A CN100337737C CN 100337737 C CN100337737 C CN 100337737C CN B2004100100186 A CNB2004100100186 A CN B2004100100186A CN 200410010018 A CN200410010018 A CN 200410010018A CN 100337737 C CN100337737 C CN 100337737C
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- reactor
- diameter
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- height
- inlet pipe
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- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 10
- 239000004215 Carbon black (E152) Substances 0.000 title claims abstract description 8
- 229930195733 hydrocarbon Natural products 0.000 title claims abstract description 8
- 150000002430 hydrocarbons Chemical class 0.000 title claims abstract description 8
- 239000000463 material Substances 0.000 title abstract description 3
- 238000005336 cracking Methods 0.000 claims abstract description 21
- 239000003054 catalyst Substances 0.000 claims abstract description 9
- 239000002002 slurry Substances 0.000 claims abstract description 8
- 241000209094 Oryza Species 0.000 claims description 16
- 235000007164 Oryza sativa Nutrition 0.000 claims description 16
- 235000009566 rice Nutrition 0.000 claims description 16
- 239000002994 raw material Substances 0.000 claims description 6
- 239000002826 coolant Substances 0.000 claims description 5
- 238000002791 soaking Methods 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 abstract description 10
- 230000029936 alkylation Effects 0.000 abstract description 4
- 238000005804 alkylation reaction Methods 0.000 abstract description 4
- 230000003197 catalytic effect Effects 0.000 abstract description 4
- 238000005504 petroleum refining Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 6
- 150000001336 alkenes Chemical class 0.000 description 3
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 230000035484 reaction time Effects 0.000 description 2
- 241000196324 Embryophyta Species 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 208000012826 adjustment disease Diseases 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000005243 fluidization Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 230000005012 migration Effects 0.000 description 1
- 238000013508 migration Methods 0.000 description 1
- 238000003541 multi-stage reaction Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 238000006276 transfer reaction Methods 0.000 description 1
- 230000000007 visual effect Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The present invention relates to a hydrocarbon material catalytic cracking lift pipe reactor which belongs to the technical field of petroleum refining equipment. The present invention comprises a first reactor and a second reactor which are arranged and connected in parallel, and a third reator and a fourth reactor which are coaxially connected in series; the upper ends of the first reactor and the second reactor are connected in series with the lower end of the third reactor, and the first reactor and the second reactor are composed of pre-lift segments on the lower parts and cracking reaction segments on the upper parts; the bottoms of the pre-lift segments of the first reactor and the second reactor are provided with pre-lift gas inlet pipes, the lower parts are provided with catalyst inlet pipes, the lower parts of the cracking segment of the first reactor and the second reactor are respectively provided with inlet pipe mozzles for raw oil, and inlet pipe nozzles for cycle oil and slurry oil; the third reactor is of an inverted cone structure with the cone angle of more than 0 to 20 degrees, the fourth reactor adopts a scaling structure, the diameter of a drawing-down area is 0.7 to 1 time as large as that of a non drawing-down area, and the upper part of the fourth reactor is provided with an oil gas outlet pipe. The present invention can be used to not only realize the two-segment catalytic function of remilling the raw oil and the cycle oil but also realize the alkylation conversion of catalytic gasoline, and to enable the yield of the gasoline to increase by 1% and the olefinic contents in the produced gasoline to decrease by 10 to 15%.
Description
Technical field
The invention belongs to the petroleum refining equipment technical field, particularly a kind of hydrocarbon raw material catalytic cracking riser reactor.
Background technology
Catalytic cracking unit is one of visual plant of refinery stock oil secondary operations, and riser reactor is the nucleus equipment of catalytic cracking unit.Existing riser reactor adopts the equal diameter reactor usually, and reactor top reaction efficiency is very low.In recent years, aspect riser reactor, carried out more improvement, for example Chinese patent application 99213769.1,00134054.9 has proposed the duo-lift tube reactor scheme, duo-lift tube reactor is two sections and arranges, first section (first riser reactor) is used for the feedstock oil cracking, product is after gas solid separation, and gasoline enters second riser reactor in top, introduces new regenerated catalyst again in second riser.Its two risers are all shorter, and the oil gas reaction time shortens one times than the popular response device, solved the inefficient problem in conventional riser reactor top, but each riser reactor is conventional structure, and structure is comparatively complicated.Chinese patent application has further proposed three riser reactor schemes, and realization feedstock oil, recycle oil, gasoline are processed in each riser.Every riser is all finished reaction about 1 second.Its advantage is a perfect control reaction condition more, improves product quality.But three tubular constructions are conventional design still, and too complicated on the engineering, equipment interoperability is relatively poor.
Summary of the invention
The object of the invention is to provide a kind of simple in structure, hydrocarbon raw material catalytic cracking riser reactor that result of use is good.
For reaching above-mentioned purpose, the present invention adopts following technical scheme: a kind of hydrocarbon raw material catalytic cracking riser reactor, comprise be arranged in parallel first, the 3rd of second reactor and coaxial series connection setting, the 4th reactor, first, connect with the 3rd reactor lower end in second reactor upper end, first, second reactor is made up of the pre lift zone of bottom and the soaking section on top, first, second reactor pre lift zone bottom is provided with pre-extracting gas inlet pipe, the bottom is provided with catalyst inlet pipe, first, the second reactor cracking zone bottom is respectively equipped with feedstock oil inlet pipe nozzle, recycle oil and slurry oil inlet pipe nozzle, the 4th reactor top are provided with oil gas and go out pipe.
The 3rd reactor be cone angle greater than 0 the degree and be less than or equal to 20 the degree inverted cone-shaped structures.
The 4th reactor is pantograph structure, its undergauge district goes to upper and lower the cancave cambered surface planform that section diameter is big, the mid portion diameter is little, perhaps the top extension diameter section that enlarges gradually of the bottom undergauge section that reduced gradually by diameter from bottom to top of its undergauge district, isometrical section of middle part that diameter is constant and diameter is formed, and undergauge district maximum gauge equals not undergauge district diameter, minimum diameter and is not less than 0.7 times of undergauge district diameter not.
First, second reactor cracking zone bottom is respectively equipped with 1-3 layer feedstock oil inlet pipe nozzle, recycle oil and slurry oil inlet pipe nozzle, presses the even number symmetric arrangement for every layer; The 3rd sidewall of reactor is provided with cooling medium inlet pipe nozzle, gasoline feeding nozzle.
The 1.0-2.0 that first, second reactor pre lift zone diameter is the cracking zone diameter doubly.
First, second reactor is the section of carrying height 3-6 rice in advance, cracking zone height 10-20 rice; The 3rd height for reactor 4-10 rice, the 4th height for reactor 5-10 rice.
Among the present invention, four sections reactors organically link together by series and parallel, and are simple in structure.In a reactor, realize the multistage reaction, both can realize the high strength cracking, can reduce olefin(e) centent again, improved product quality.First reactor of the present invention is used for the cracking of fresh feed oil, and second reactor is used for recycle oil and slurry oil reaction, and the 3rd, the 4th reactor is used for product reconstruct, carries out alkylation and hydrogen transfer reaction, reduces the olefin(e) centent of gasoline.First, second reactor pre lift zone diameter enlarges than first conversion zone, and it is mobile stable to help catalyst, and the reaction temperature fluctuation is less.Mainly carry out cracking reaction in first, second reactor, the multilayer designs of nozzles can adapt to the requirement that different material separates, and can also adjust the reaction time by selecting differing heights position nozzle for use, changes reaction result.Every layer of nozzle pressed the even number symmetric arrangement, can prevent that high pressure charging from causing damage to reactor shell.The 3rd reactor be tapering greater than 0 the degree and be less than or equal to 20 the degree inverted cone-shaped structures, caliber enlarges gradually from bottom to top, this structure more meets the fluidization flow principles, can effectively prevent gas-solid back-mixing and backflow, can eliminate effectively especially that high speed gas-solid fluid from first, second two reactor causes mobile inhomogeneous and refluxing.The cooling medium that this reactor side is provided with is taken over and can be fed 20-70 ℃ of demineralized water adjustment reaction temperature, and set gasoline feeding nozzle can be used for the raw gasoline upgrading.The 4th reactor adopts the scaling type structure, and undergauge district diameter is 0.7-1 a times of not undergauge district diameter, can make catalyst break away from tube wall surface, obviously reduce the catalyst back-mixing, the density of catalyst height helps product and further finishes alkylation and hydrogen migration, improves quality of gasoline.Utilize the present invention both to realize the two-stage catalytic function of feedstock oil and recycle oil back mixing, realized that again the catalytic gasoline alkylation transforms, can improve yield of gasoline 1%, olefin(e) centent reduces 10-15% in institute's oil that steams.
Description of drawings
Fig. 1 is a structural representation of the present invention;
Fig. 2, Fig. 3 are respectively the pantograph structure schematic diagram of the 4th reactor.
The specific embodiment
Embodiment, a kind of hydrocarbon raw material catalytic cracking riser reactor, comprise be arranged in parallel first, second reactor 1,2 and coaxial series connection be provided with the 3rd, the 4th reactor 3,4, first, second reactor 1, connect with the 3rd reactor 3 lower ends in 2 upper ends, first, second reactor 1,2 are made up of the pre lift zone a of bottom and the soaking section b on top, first, second reactor 1,2 pre lift zone a bottom is provided with pre-extracting gas inlet pipe 7, the bottom is provided with catalyst inlet pipe 8, first, second reactor 1,2 cracking zone b bottoms are respectively equipped with feedstock oil inlet pipe nozzle 9, recycle oil and slurry oil inlet pipe nozzle 10, first, second reactor is 3 meters of the section of carrying height in advance, 10 meters of cracking zone height.The 3rd reactor 3 is the inverted cone-shaped structure of cone angle 10 degree, 9 meters of its height, and its sidewall is provided with cooling medium inlet pipe nozzle 11, gasoline feeding nozzle 12.The 4th reactor 4 is convergent-divergent shape structure, undergauge district 13 vertical section structures as shown in Figure 2, undergauge district 13 diameters be not undergauge district 14 diameters 0.7-1 doubly, 5 meters of its height, its top is provided with oil gas and goes out pipe 15.
In embodiment 2, the present embodiment, first, second reactor 1,2 is 5 meters of the section of carrying a height in advance, 15 meters of cracking zone b height.The 3rd reactor 3 is the inverted cone-shaped structure of cone angle 20 degree, 4 meters of its height.The 4th reactor 4 is convergent-divergent shape structure, undergauge district 13 vertical section structures as shown in Figure 3, undergauge district 13 diameters be not undergauge district 14 diameters 0.7-1 doubly, 10 meters of height.Other are with embodiment 1.
Claims (10)
1, a kind of hydrocarbon raw material catalytic cracking riser reactor, it is characterized in that, comprise be arranged in parallel first, the 3rd of second reactor and coaxial series connection setting, the 4th reactor, first, connect with the 3rd reactor lower end in second reactor upper end, first, second reactor is made up of the pre lift zone of bottom and the soaking section on top, first, second reactor pre lift zone bottom is provided with pre-extracting gas inlet pipe, the bottom is provided with catalyst inlet pipe, first, the second reactor cracking zone bottom is respectively equipped with feedstock oil inlet pipe nozzle, recycle oil and slurry oil inlet pipe nozzle, the 4th reactor top are provided with oil gas and go out pipe.
2, reactor as claimed in claim 1 is characterized in that, the 3rd reactor be cone angle greater than 0 the degree and be less than or equal to 20 the degree inverted cone-shaped structures.
3, reactor as claimed in claim 1 or 2, it is characterized in that, the 4th reactor is pantograph structure, its undergauge district goes to upper and lower the cancave cambered surface planform that section diameter is big, the mid portion diameter is little, perhaps the top extension diameter section that enlarges gradually of the bottom undergauge section that reduced gradually by diameter from bottom to top of its undergauge district, isometrical section of middle part that diameter is constant and diameter is formed, and undergauge district maximum gauge equals not undergauge district diameter, minimum diameter and is not less than 0.7 times of undergauge district diameter not.
4, reactor as claimed in claim 1 or 2 is characterized in that,, the second reactor cracking zone bottom is respectively equipped with 1-3 layer feedstock oil inlet pipe nozzle, recycle oil and slurry oil inlet pipe nozzle, presses the even number symmetric arrangement for every layer; The 3rd sidewall of reactor is provided with cooling medium inlet pipe nozzle, gasoline feeding nozzle.
5, reactor as claimed in claim 3 is characterized in that, first, second reactor cracking zone bottom is respectively equipped with 1-3 layer feedstock oil inlet pipe nozzle, recycle oil and slurry oil inlet pipe nozzle, presses the even number symmetric arrangement for every layer; The 3rd sidewall of reactor is provided with cooling medium inlet pipe nozzle, gasoline feeding nozzle.
6, reactor as claimed in claim 4 is characterized in that, the 1.0-2.0 that first, second reactor pre lift zone diameter is the cracking zone diameter doubly.
7, reactor as claimed in claim 5 is characterized in that, the 1.0-2.0 that first, second reactor pre lift zone diameter is the cracking zone diameter doubly.
As claim 1,2,5,6 or 7 described reactors, it is characterized in that 8, first, second reactor is the section of carrying height 3-6 rice in advance, cracking zone height 10-20 rice; The 3rd height for reactor 4-10 rice, the 4th height for reactor 5-10 rice.
9, reactor as claimed in claim 3 is characterized in that, first, second reactor is the section of carrying height 3-6 rice in advance, cracking zone height 10-20 rice; The 3rd height for reactor 4-10 rice, the 4th height for reactor 5-10 rice.
10, reactor as claimed in claim 4 is characterized in that, first, second reactor is the section of carrying height 3-6 rice in advance, cracking zone height 10-20 rice; The 3rd height for reactor 4-10 rice, the 4th height for reactor 5-10 rice.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100100186A CN100337737C (en) | 2004-01-09 | 2004-01-09 | Hydrocarbon material catalytic cracking lift pipe reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100100186A CN100337737C (en) | 2004-01-09 | 2004-01-09 | Hydrocarbon material catalytic cracking lift pipe reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1640538A CN1640538A (en) | 2005-07-20 |
| CN100337737C true CN100337737C (en) | 2007-09-19 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100100186A Expired - Fee Related CN100337737C (en) | 2004-01-09 | 2004-01-09 | Hydrocarbon material catalytic cracking lift pipe reactor |
Country Status (1)
| Country | Link |
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| CN (1) | CN100337737C (en) |
Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4422925A (en) * | 1981-12-28 | 1983-12-27 | Texaco Inc. | Catalytic cracking |
| US5565176A (en) * | 1992-08-20 | 1996-10-15 | Stone & Webster Engineering Corporation | Catalytically cracking paraffin rich feedstocks comprising high and low concarbon components |
| CN1118539C (en) * | 2000-12-13 | 2003-08-20 | 中国石油天然气股份有限公司 | Catalytic cracking technology with two-stage lift pipe |
-
2004
- 2004-01-09 CN CNB2004100100186A patent/CN100337737C/en not_active Expired - Fee Related
Patent Citations (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4422925A (en) * | 1981-12-28 | 1983-12-27 | Texaco Inc. | Catalytic cracking |
| US5565176A (en) * | 1992-08-20 | 1996-10-15 | Stone & Webster Engineering Corporation | Catalytically cracking paraffin rich feedstocks comprising high and low concarbon components |
| CN1118539C (en) * | 2000-12-13 | 2003-08-20 | 中国石油天然气股份有限公司 | Catalytic cracking technology with two-stage lift pipe |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1640538A (en) | 2005-07-20 |
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| C14 | Grant of patent or utility model | ||
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| ASS | Succession or assignment of patent right |
Owner name: SHI BAOZHEN Free format text: FORMER OWNER: LUOYANG PETRO-CHEMICAL EQUIPMENT INST. Effective date: 20070907 |
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Effective date of registration: 20070907 Address after: 471003 three mountain road, hi tech Development Zone, Henan Province, Tsinghua Science and Technology Park, 6, Luoyang Patentee after: Shi Baozhen Address before: 471003 Zhongzhou West Road, Henan, Luoyang Patentee before: Luoyang Petro-Chemical Equipment Inst. |
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| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: Shanghai HEC Co., Ltd. Assignor: Shi Baozhen Contract fulfillment period: 2009.12.10 to 2014.12.30 contract change Contract record no.: 2010310000010 Denomination of invention: Hydrocarbon material catalytic cracking lift pipe reactor Granted publication date: 20070919 License type: Exclusive license Record date: 2010.1.26 |
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| LIC | Patent licence contract for exploitation submitted for record |
Free format text: EXCLUSIVE LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2009.12.10 TO 2014.12.30; CHANGE OF CONTRACT Name of requester: SHANGHAI HOTO PETROCHEMICAL ENGINEERING CO., LTD. Effective date: 20100126 |
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| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20070919 Termination date: 20150109 |
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| EXPY | Termination of patent right or utility model |