CN1325152C - Riser reactor - Google Patents
Riser reactor Download PDFInfo
- Publication number
- CN1325152C CN1325152C CNB2004100100383A CN200410010038A CN1325152C CN 1325152 C CN1325152 C CN 1325152C CN B2004100100383 A CNB2004100100383 A CN B2004100100383A CN 200410010038 A CN200410010038 A CN 200410010038A CN 1325152 C CN1325152 C CN 1325152C
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- CN
- China
- Prior art keywords
- pre lift
- lift zone
- housing
- riser reactor
- zone
- 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
- 238000006243 chemical reaction Methods 0.000 claims abstract description 30
- 239000003054 catalyst Substances 0.000 claims abstract description 19
- 239000000571 coke Substances 0.000 abstract description 3
- 238000005504 petroleum refining Methods 0.000 abstract description 2
- 238000007670 refining Methods 0.000 abstract 1
- 238000004523 catalytic cracking Methods 0.000 description 5
- 239000003795 chemical substances by application Substances 0.000 description 5
- 238000001816 cooling Methods 0.000 description 5
- 230000001172 regenerating effect Effects 0.000 description 5
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000000047 product Substances 0.000 description 3
- 101100194816 Caenorhabditis elegans rig-3 gene Proteins 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 230000008676 import Effects 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 239000004615 ingredient Substances 0.000 description 1
- 230000001737 promoting effect Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000008234 soft water Substances 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention relates to a riser reactor which belongs to the technical field of petroleum refining devices. The present invention comprises a reaction section, wherein a casing below the reaction section is provided with a catalyst heat exchanger; the side wall of the casing is provided with a catalyst inlet pipe, and the lower end of the casing is provided with a medium lifting inlet pipe. The internal diameter of the casing of the pre-lifting section is 1.1 to 2.0 times larger than the internal diameter of an adjacent section. The heat exchanger can be a coil which is arranged along the inner side of the casing, and an inlet and an outlet of the coil are positioned on the side wall of the casing below the reaction section; the heat exchanger can also be sleeve pipes which are arranged at uniform intervals and are vertically arranged along the inner side of the casing, and the upper ends of the sleeve pipes penetrate out of the casing. The present invention which has multiple functions can be used for the refining cycle stock and enables the yield of dry gas to be reduced by 50% and the yield of coke to be reduced by 30%.
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 important device of refinery stock oil secondary operations.In catalytic cracking unit, hydrocarbon raw material issues angry solid phase cracking reaction in the catalyst existence, and high temperature catalyst reenters catalytic cracking unit performance catalytic action after regeneration is handled.Riser reactor is the nucleus equipment of catalytic cracking unit, and existing riser reactor comprises pre lift zone and conversion zone, and the catalyst after the regeneration enters pre lift zone from catalyst inlet, enters conversion zone and play a role under pre-lifting medium promotes.For recycle oil, because the boiling point of ingredient is low, its gasification is quite easy, do not need high regenerative agent temperature, catalyst temperature after general regeneration is handled is about 700 ℃, the pyroreaction that high temperature like this causes has increased the content of byproduct such as dry gas and coke in the target product, and the target product yield reduces, and directly influences the business economic benefit.If the reduction regenerated catalyst temperature must adopt other cooling system to regenerated catalyst cooling processing.Existing riser reactor obviously can not satisfy the cooling needs of regenerated catalyst in the recycle oil processing.
Summary of the invention
The object of the invention is to provide a kind of band regenerative agent thermostatic riser reactor.
For reaching above-mentioned purpose, the present invention adopts following technical scheme: a kind of riser reactor, comprise conversion zone, be provided with in the following pre lift zone housing of conversion zone that catalyst heat exchange device, pre lift zone lower housing portion are provided with catalyst inlet pipe, pre lift zone housing lower end is provided with and promotes the medium inlet pipe, pre lift zone housing internal diameter is greater than adjacency conversion zone internal diameter.
Pre lift zone housing internal diameter is 1.1-2.0 times in abutting connection with the conversion zone internal diameter.
Heat-exchanger rig is that coil pipe is imported and exported and is positioned at the following pre lift zone housing sidewall of conversion zone along the inboard coil pipe that is provided with of pre lift zone housing.
Heat-exchanger rig is along the U type coil pipe of pre lift zone housing medial shaft to setting, and coil pipe is imported and exported and is positioned at the following pre lift zone housing sidewall of conversion zone.
Heat-exchanger rig be along pre lift zone housing inner disc around coil pipe, coil pipe is imported and exported and to be positioned at the following pre lift zone housing sidewall of conversion zone.
Heat-exchanger rig is along the interval uniform sleeve pipe of pre lift zone housing medial shaft to setting, and the sleeve pipe upper end passes the pre lift zone housing; Sleeve pipe outer tube closed at both ends, its upper end are provided with outlet, and the interior pipe of sleeve pipe lower end is communicated with outer tube, the upper end passes end closure on the outer tube.
The present invention adopts the design that heat-exchanger rig (heat sink) is set in the following pre lift zone housing of conversion zone of existing riser reactor, about 700 ℃ regenerated catalyst after regeneration is handled does not need special cooling device to carry out cooling processing can directly enter riser reactor, cool with the lower part at conversion zone, be cooled to technology temperature required (550-650 ℃), be promoted to conversion zone by promoting medium again, contact uply with the reaction logistics that enters reactor through the conversion zone sidewall, catalytic reaction is carried out.At last, product and catalyst export outflow reactor through reactor head.Heat-exchanger rig can be arranged in the following pre lift zone housing of conversion zone.Heat-exchanger rig can adopt coil exchanger, and low-temperature heat exchange medium (soft water or various hydro carbons) flows through from coil pipe and the abundant heat exchange of regenerated catalyst, and it is temperature required to make the regenerative agent temperature reduce to technology; Also can adopt double-tube heat exchanger, low-temperature heat exchange medium pipe lower end in the sleeve pipe enters outer tube, flows out from the outlet of sleeve pipe outer tube with high temperature heat transferring medium after the abundant heat exchange of regenerative agent.Riser reactor multi-use of the present invention has reduced production equipment, has simplified production process, makes production process compacter.Use riser reactor of the present invention, can make dry gas yied reduce by 50%, coke yield reduces by 30%.
Description of drawings
Fig. 1 is a structural representation of the present invention;
Fig. 2 is embodiment 2 structural representations.
The specific embodiment
Embodiment 1, a kind of riser reactor comprise conversion zone 2, are provided with in conversion zone 2 following pre lift zone 1 housings that catalyst heat exchange device 3, pre lift zone 1 housing sidewall bottom are provided with catalyst inlet pipe 4, pre lift zone 1 housing lower end is provided with and promotes medium inlet pipe 5.Pre lift zone 1 housing internal diameter is 1.1 times in abutting connection with conversion zone 2 internal diameters.Heat-exchanger rig 3 is along the interval uniform sleeve pipe of pre lift zone 1 housing medial shaft to setting, and the sleeve pipe upper end passes pre lift zone 1 housing; Sleeve pipe outer tube 8 closed at both ends, its upper end are provided with outlet 9, and the interior pipe of sleeve pipe 10 lower ends are communicated with outer tube, the upper end passes end closure on the outer tube.In the use, low-temperature heat exchange medium pipe 10 in the sleeve pipe enters, and flow out from 8 outlets 9 of sleeve pipe outer tube the heat absorption back.
In embodiment 2, the present embodiment, pre lift zone 1 housing internal diameter is 1.5 times in abutting connection with conversion zone 2 internal diameters.Heat-exchanger rig 3 is that coil pipe import 6, outlet 7 are positioned at pre lift zone 1 housing sidewall along the vertical U type coil pipe that is provided with of pre lift zone 1 housing madial wall.In the use, the low-temperature heat exchange medium enters from coil pipe import 6, and flow out from coil pipe outlet 7 the heat absorption back.Other are with embodiment 1
Among above-mentioned two embodiment, by control low-temperature heat exchange medium temperature, flow velocity is adjustable regenerative agent temperature.
For easy, improvement part only draws among the figure.
Claims (6)
1, a kind of riser reactor, comprise conversion zone, it is characterized in that, be provided with in the following pre lift zone housing of conversion zone that catalyst heat exchange device, pre lift zone lower housing portion are provided with catalyst inlet pipe, pre lift zone housing lower end is provided with and promotes the medium inlet pipe, pre lift zone housing internal diameter is greater than adjacency conversion zone internal diameter.
2, riser reactor as claimed in claim 1 is characterized in that, pre lift zone housing internal diameter is 1.1-2.0 times in abutting connection with the conversion zone internal diameter.
3, riser reactor as claimed in claim 2 is characterized in that, heat-exchanger rig is that coil pipe is imported and exported and is positioned at the following pre lift zone housing sidewall of conversion zone along the inboard coil pipe that is provided with of pre lift zone housing.
4, riser reactor as claimed in claim 3 is characterized in that, heat-exchanger rig is along the U type coil pipe of pre lift zone housing medial shaft to setting, and coil pipe is imported and exported and is positioned at the following pre lift zone housing sidewall of conversion zone.
5, riser reactor as claimed in claim 3 is characterized in that, heat-exchanger rig be along pre lift zone housing inner disc around coil pipe, coil pipe is imported and exported and to be positioned at the following pre lift zone housing sidewall of conversion zone.
6, riser reactor as claimed in claim 2 is characterized in that, heat-exchanger rig is along the interval uniform sleeve pipe of pre lift zone housing medial shaft to setting, and the sleeve pipe upper end passes the pre lift zone housing; Sleeve pipe outer tube closed at both ends, its upper end are provided with outlet, and the interior pipe of sleeve pipe lower end is communicated with outer tube, the upper end passes end closure on the outer tube.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100100383A CN1325152C (en) | 2004-01-29 | 2004-01-29 | Riser reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100100383A CN1325152C (en) | 2004-01-29 | 2004-01-29 | Riser reactor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1647851A CN1647851A (en) | 2005-08-03 |
| CN1325152C true CN1325152C (en) | 2007-07-11 |
Family
ID=34867690
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100100383A Expired - Fee Related CN1325152C (en) | 2004-01-29 | 2004-01-29 | Riser reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1325152C (en) |
Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4356082A (en) * | 1980-12-18 | 1982-10-26 | Mobil Oil Corporation | Heat balance in FCC process |
| US4430302A (en) * | 1982-04-12 | 1984-02-07 | Uop Inc. | Fluidized catalyst regeneration apparatus |
| US4917790A (en) * | 1989-04-10 | 1990-04-17 | Mobil Oil Corporation | Heavy oil catalytic cracking process and apparatus |
| US6267873B1 (en) * | 1997-04-11 | 2001-07-31 | Indian Oil Corporation, Ltd. | Fluidized catalytic cracking process |
-
2004
- 2004-01-29 CN CNB2004100100383A patent/CN1325152C/en not_active Expired - Fee Related
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4356082A (en) * | 1980-12-18 | 1982-10-26 | Mobil Oil Corporation | Heat balance in FCC process |
| US4430302A (en) * | 1982-04-12 | 1984-02-07 | Uop Inc. | Fluidized catalyst regeneration apparatus |
| US4917790A (en) * | 1989-04-10 | 1990-04-17 | Mobil Oil Corporation | Heavy oil catalytic cracking process and apparatus |
| US6267873B1 (en) * | 1997-04-11 | 2001-07-31 | Indian Oil Corporation, Ltd. | Fluidized catalytic cracking process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1647851A (en) | 2005-08-03 |
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| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| EE01 | Entry into force of recordation of patent licensing contract |
Assignee: QINGDAO JINGRUN PETROCHEMICAL ENGINEERING CO., LTD. Assignor: Luoyang Petro-Chemical Equipment Inst. Contract fulfillment period: 2008.9.23 to 2013.10.1 Contract record no.: 2008410000237 Denomination of invention: Lift-pipe reactor Granted publication date: 20070711 License type: Exclusive license Record date: 20081222 |
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| LIC | Patent licence contract for exploitation submitted for record |
Free format text: EXCLUSIVE LICENSE; TIME LIMIT OF IMPLEMENTING CONTACT: 2008.9.23 TO 2013.10.1; CHANGE OF CONTRACT Name of requester: QINGDAO JINGRUN PETROCHEMICAL ENGINEERING CO., LTD Effective date: 20081222 |
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Owner name: SHI BAOZHEN Free format text: FORMER OWNER: LUOYANG PETRO-CHEMICAL EQUIPMENT INST. Effective date: 20110607 |
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| TR01 | Transfer of patent right |
Effective date of registration: 20110607 Address after: 471003 Tsinghua Science Park, three mountain road, hi tech Zone, Henan, Luoyang 609 Patentee after: Shi Baozhen Address before: 471003 Zhongzhou West Road, Henan, Luoyang Patentee before: Luoyang Petro-Chemical Equipment Inst. |
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