CN1754942A - Continuous reforming plant catalyst two-phase up-flow regeneration method - Google Patents
Continuous reforming plant catalyst two-phase up-flow regeneration method Download PDFInfo
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- CN1754942A CN1754942A CN 200410080203 CN200410080203A CN1754942A CN 1754942 A CN1754942 A CN 1754942A CN 200410080203 CN200410080203 CN 200410080203 CN 200410080203 A CN200410080203 A CN 200410080203A CN 1754942 A CN1754942 A CN 1754942A
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- revivifier
- gas
- burning
- regeneration
- resurgent gases
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- 238000011069 regeneration method Methods 0.000 title claims abstract description 29
- 239000003054 catalyst Substances 0.000 title claims abstract description 24
- 238000002407 reforming Methods 0.000 title claims description 12
- 238000000034 method Methods 0.000 claims abstract description 25
- 230000008929 regeneration Effects 0.000 claims abstract description 25
- 238000010791 quenching Methods 0.000 claims abstract description 4
- 239000007789 gas Substances 0.000 claims description 65
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 14
- 239000001301 oxygen Substances 0.000 claims description 14
- 229910052760 oxygen Inorganic materials 0.000 claims description 14
- 238000005406 washing Methods 0.000 claims description 9
- 230000005484 gravity Effects 0.000 claims description 5
- 238000001816 cooling Methods 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 4
- 230000008439 repair process Effects 0.000 claims description 4
- 238000001035 drying Methods 0.000 claims description 3
- 238000000746 purification Methods 0.000 claims description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 4
- 230000000171 quenching effect Effects 0.000 abstract 1
- 238000010992 reflux Methods 0.000 abstract 1
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- 238000005516 engineering process Methods 0.000 description 8
- 229910052799 carbon Inorganic materials 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 230000001172 regenerating effect Effects 0.000 description 6
- 239000001257 hydrogen Substances 0.000 description 5
- 229910052739 hydrogen Inorganic materials 0.000 description 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 4
- 239000000571 coke Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000012958 reprocessing Methods 0.000 description 4
- 238000003860 storage Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 238000001833 catalytic reforming Methods 0.000 description 2
- 238000011161 development Methods 0.000 description 2
- 230000018109 developmental process Effects 0.000 description 2
- 230000002779 inactivation Effects 0.000 description 2
- 239000003208 petroleum Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 239000004744 fabric Substances 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000005984 hydrogenation reaction Methods 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000010327 methods by industry Methods 0.000 description 1
- 230000036651 mood Effects 0.000 description 1
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000012827 research and development Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
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Abstract
The invention relates to catalyst two-segment reflux regeneration method for continual reformer with regeneration gas cycle reflow process as: for regeneration cycle gas from circulating compressor exchanges heat with charred product and be heated by electric heater to enter regenerator, flows through second-segment char zone radial bed, mixes with clean wind and quenching air in out loop cavity to flow through first-segment char zone bed and discharge out regenerator to exchange heat, cool, clean, dry, filter and revert to circulating compressor for step-up cycle. This invention has low water content in regenerated gas.
Description
Technical field
The invention belongs to the Petroleum Processing Technology field, the improvement of the reforming plant catalyst cyclic regeneration technology of more specifically saying so.
Background technology
Catalytic reforming is the main processes from oil production aromatic hydrocarbons and high octane gasoline component, and the hydrogen of institute's by-product is again the important source of refinery hydrogenation unit with hydrogen, therefore is subjected to the attention of countries in the world refinery and petroleum chemical industry.In recent years, catalytic reforming is except catalyzer has had the development that is exceedingly fast, process aspect also has very big development, particularly the U.S. of the seventies and France have developed the continuous catalyst regenerating technology in succession, make the activity of such catalysts of running remain higher level, quality product and yield all increase.China introduced once the research and development of UOP (UOP) and IFP (IFP) two kinds of continuous catalyst regenerating technologies (the Hou Xianglin chief editor, " Chinese oil Refining Technologies ", Sinopec press, in December, 1991, P158-183).
1, the technical process of French IFP regenerating continuous reforming catalyst is: catalyzer is to move axially in the catalyst regeneration process, and resurgent gases is to move radially, and both are the cross-flow contact.Reclaimable catalyst at first is stored in the storage zone on revivifier top, rely on gravity successively by one section of revivifier, two sections scorch regions burn, flow out revivifier at last, catalyst regeneration loop wherein: the regeneration gas that comes from the outlet of resurgent gases recycle compressor is divided into two portions: main part through and burn the product gas heat exchange, enter revivifier after burning the electric heater heating, at first preheating enters the catalyzer of revivifier scorch region, the radially bed of one section scorch region of flowing through then burns the back and converges at the pipe core place and send revivifier, outside revivifier, mix to regulate oxygen level and temperature with purification general mood and quench gas, send two sections scorch regions of revivifier then back to, the inspection section that enters catalyzer after the two sections scorch region beds of flowing through burn; Checking section, one checks that gas enters revivifier in addition, guaranteeing that carbon deposit on the catalyzer all burns down the back and burns gas and mix at the pipe core place, mixed gas oxygen content is about 0.3～0.7% (mol), after burning feed exchanger and the heat exchange of regeneration recycle gas aftercooler cooling, enter the resurgent gases washing tank, to remove HCl, the CO in the gas
2Deng material, process washing and exsiccant gas are got back to the resurgent gases recycle compressor and are recycled after boosting, and check the not increase of temperature of section, can think that catalyzer does not contain coke.The regenerative process operational condition: one section scorch region temperature is 465 ℃, pressure 0.55Mpa, inlet resurgent gases oxygen level 0.8% (mol); Two sections scorch region temperature are 480 ℃, pressure 0.54Mpa, inlet resurgent gases oxygen level 0.8% (mol); Check section inlet gas oxygen level 1.0% (mol), pressure 0.53mpa.
IFP continuous reforming regenerator structure: a storage zone is arranged at the revivifier top, and the reclaimable catalyst storage flow to scorch region by 8 downtakes after 1-2 hour, and scorch region is made up of two radial bed.These two radial bed are separated by 8 downtakes.Have one to burn the test zone in the bottom in second district, purpose is to check whether the coke on the catalyzer all burns.
IFP process using co-current regeneration technology, be that the mobile direction of catalyzer is identical with the mobile direction of resurgent gases, the water that the catalyzer burning process produces causes that water-content raises gradually in the catalyzer burning process, and two sections water-contents reach 3000-4000ppm, thereby influence activity of such catalysts.
2, Uop Inc.'s continuous reforming regeneration technical process: catalyzer relies on gravity to flow into the revivifier scorch region, flow downward by the ring-like district between inside and outside column and the taper screen cloth, flow out revivifier at last, wherein the revivifier top gas enters the regeneration blower fan, blower fan come out one the tunnel be recycled to regeneration the heating zone, another road is behind air cooler, electric heater, a part is removed scorch region, another part is through Venturi scrubber emptying, burns used oxygen and the wind comes from by the oxychlorination section and keep.The regenerative process operational condition: scorch region inlet resurgent gases oxygen level is 0.5-1.0% (mol), and temperature is 477-565 ℃, pressure 0.241Mpa.
The UOP process catalyst is regenerated as single hop regeneration, and regeneration temperature height, circulation gas do not have the dehydration facility, water content higher (reaching 40000ppm), and chlorinity is big, claims damp and hot circulation, and this process catalyst inactivation is fast, and equipment corrosion is more serious, equipment material is required high
Summary of the invention
The objective of the invention is to overcome the shortcoming of prior art, propose a kind of improved continuous reforming plant catalyst process engineering for regenerating.
Continuous reforming plant catalyst two-phase up-flow regeneration technical process of the present invention: reclaimable catalyst relies on gravity successively by one section and two sections scorch regions of revivifier by revivifier top buffer zone, flow out revivifier at last, resurgent gases circulation loop process wherein: from the regeneration gas that the outlet of resurgent gases recycle compressor comes inject purify wind after, with enter the gas converting heat that burns after the burning of feed exchanger, enter revivifier after burning the electric heater heating, at first enter the revivifier pipe core, the radially bed of two sections scorch regions of flowing through then burns, through two sections gases after burning outside ring cavity with purify wind and quench gas and mix with adjusting oxygen level and temperature; The blended gas stream enters the revivifier pipe core after one section scorch region bed burns, discharge revivifier, enters the resurgent gases washing tank again after burning feed exchanger and the heat exchange of regeneration recycle gas aftercooler cooling, to remove HCl, the CO in the gas
2Deng material, getting back to the resurgent gases recycle compressor behind drying device, the strainer dry filter more at last recycles after boosting, the regenerative process operational condition: one section scorch region temperature is 460-530 ℃, pressure 0.50-0.53Mpa, inlet resurgent gases oxygen level 0.5-0.8% (mol); 470-530 ℃ of two sections scorch region temperature, pressure 0.51-0.54Mpa, inlet resurgent gases oxygen level 0.5-0.8% (mol).
The described revivifier of reclaiming process of the present invention has been applied for utility model patent, application number is 200420093187.6, the structure of revivifier: comprise the catalyzer buffer zone by communicating pipe to revivifier, in the middle of the central lumen of revivifier is provided with, its outer catalyzer ring casing, outer ring cavity of setting gradually, its central lumen is divided into upper and lower, first, second chamber by dividing plate, and first chamber is provided with the resurgent gases outlet, and second chamber is provided with inlet mouth.
Advantage of the present invention and effect:
The present invention adopts two-phase up-flow regeneration technology, the mobile direction of catalyzer is opposite with the mobile direction of resurgent gases, because the combustionvelocity of hydrogen is higher than the combustionvelocity of carbon in the coke, make the water that produces in the catalyzer coke burning regeneration process reduce gradually along with catalyzer flows, the present invention is burnt whole hydrogen of burning-off and part carbon for one section, water-content higher (2000-4000ppm), but it is lower to burn temperature, two sections carbon that burn the burning-off remainder, temperature is higher, but water-content lower (500-1500ppm) has solved the inactivation problem of catalyzer preferably.
Description of drawings
1, Fig. 1 is French IFP regenerating continuous reforming catalyst process flow diagram.1 is the resurgent gases recycle compressor among the figure, and 2 for burning feed exchanger, and 3 for burning electric heater, and 4 is revivifier, and 5 is revivifier circulation aftercooler, and 6 is washing tank, and 7 is the regeneration recycle gas moisture eliminator, and 8 is the reprocessing cycle air filter, and 9 is NaOH solution circulating pump.
2, Fig. 2 is Uop Inc.'s regenerating continuous reforming catalyst process flow diagram.1 is gas blower among the figure, and 2 is air cooler, and 3 is electric heater, and 4 is revivifier.
3, Fig. 3 is continuous reforming plant catalyst two phase up-flow regeneration process flow diagrams of the present invention.1 is the resurgent gases recycle compressor among the figure, and 2 for burning feed exchanger, and 3 for burning electric heater, and 4 is revivifier, and 5 is resurgent gases circulation aftercooler, and 6 is washing tank, and 7 is the regeneration recycle gas moisture eliminator, and 8 is the reprocessing cycle air filter, and 9 is NaOH solution circulating pump.
4, Fig. 4 is the described revivifier structural representation of reclaiming process of the present invention.1 is the buffer zone of catalyzer among the figure, and 101 is catalyzer, and 2 is communicating pipe, and 3 is revivifier, and 4 are the tonifying Qi pipeline, 5 is communicating pipe, and 301 is first chamber, and 302 is dividing plate, and 303 is second chamber, 304 is catalyzer, and 305 is inlet mouth, and 306 are the resurgent gases outlet, and 307 is outer ring cavity.
Embodiment
Further specify characteristics of the present invention below by specific embodiment.
Embodiment
Below in conjunction with Fig. 3 process flow diagram operating process of the present invention is described.
Reclaimable catalyst relies on gravity to burn back outflow revivifier by one section scorch region and two sections scorch regions of revivifier 4 successively by storage zone, revivifier 4 top, resurgent gases loop flow process wherein: inject from the regeneration gas of reprocessing cycle compressor 1 outlet and to purify wind, again with enter the gas converting heat that burns that burns feed exchanger 2, it is 0.5-0.8% (mol) that electric heater is heated to oxygen level, temperature is to enter revivifier 4 after 470-530 ℃, at first enter revivifier 4 pipe core bottoms, entering outer ring cavity by beds is second section and burns, this section burnt one section carbon that burns remainder, two sections resurgent gaseses after burning outside ring cavity with purify wind and mix by the chilling wind of resurgent gases recycle compressor 1, being adjusted to temperature is 460-530 ℃, oxygen level is 0.5-0.8% (mol), flow through and enter revivifier 4 pipe cores after one section scorch region bed burns, discharge revivifier, this section burnt the carbon of whole hydrogen and 40-70%.The gas of discharging revivifier enters washing tank 6 after burning feed exchanger 2 heat exchange and 5 coolings of resurgent gases circulation aftercooler, the alkali liquid washing that injects via NaOH solution circulating pump 9 is to remove wherein HCL, CO
2Deng sour gas, last gas gets back to recycling after resurgent gases recycle compressor 1 boosts behind regeneration recycle gas moisture eliminator 7 and reprocessing cycle air filter 8 dry filters.The water-content of two sections resurgent gaseses is 500-1500ppm, and the water-content of one section resurgent gases reaches 2000-4000ppm.
Claims (1)
1, a kind of continuous reforming plant catalyst two-phase up-flow regeneration method, comprise that reclaimable catalyst relies on gravity to burn by one section scorch region of revivifier and two sections scorch regions successively by revivifier top buffer zone, flow out the process of revivifier at last, it is characterized in that resurgent gases circulation loop process is: after the regeneration gas that the outlet of resurgent gases recycle compressor comes injects purification wind, enter revivifier after burning the gas converting heat after the burning of feed exchanger and burning the electric heater heating with entering, at first enter the revivifier pipe core, the radially bed of two sections scorch regions of flowing through then burns, through two sections gases after burning outside ring cavity with purify wind and quench gas and mix; The blended gas stream enters the revivifier pipe core after one section scorch region bed burns, discharge revivifier, after burning the cooling of feed exchanger heat exchange and regeneration recycle gas aftercooler, enter the washing of resurgent gases washing tank again, after last drying device drying and strainer filter, gas is got back to the resurgent gases recycle compressor and is recycled after boosting, the regenerative process operational condition: one section scorch region temperature is 460-530 ℃, pressure 0.50-0.53Mpa, inlet resurgent gases oxygen level 0.5-0.8% (mol); Two sections scorch region temperature are 470-530 ℃, pressure 0.51-0.54Mpa, inlet resurgent gases oxygen level 0.5-0.8% (mol).
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100802032A CN100434495C (en) | 2004-09-27 | 2004-09-27 | Continuous reforming plant catalyst two-phase up-flow regeneration method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100802032A CN100434495C (en) | 2004-09-27 | 2004-09-27 | Continuous reforming plant catalyst two-phase up-flow regeneration method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1754942A true CN1754942A (en) | 2006-04-05 |
| CN100434495C CN100434495C (en) | 2008-11-19 |
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| Application Number | Title | Priority Date | Filing Date |
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| CNB2004100802032A Expired - Lifetime CN100434495C (en) | 2004-09-27 | 2004-09-27 | Continuous reforming plant catalyst two-phase up-flow regeneration method |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104342195A (en) * | 2013-07-25 | 2015-02-11 | 中国石油天然气股份有限公司 | Catalyst lifting device of continuous catalytic reforming device |
| CN105148986A (en) * | 2015-09-30 | 2015-12-16 | 西南化工研究设计院有限公司 | Methanol-to-olefin catalyst bed temperature rise and regeneration device |
| CN116059802A (en) * | 2021-10-29 | 2023-05-05 | 中国石油化工股份有限公司 | A method and system for drying and dehydrating acid gas |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3652231A (en) * | 1969-09-25 | 1972-03-28 | Universal Oil Prod Co | Reconditioning system for moving column of reforming catalyst |
| US4094817A (en) * | 1977-06-15 | 1978-06-13 | Uop Inc. | Regeneration method for gravity-flowing deactivated catalyst particles |
| CN1003980B (en) * | 1986-01-27 | 1989-04-26 | 环球油品公司 | Apparatus for transferring particles from one zone to another |
| CN1023077C (en) * | 1989-01-13 | 1993-12-15 | 法国石油公司 | Process for regenerating catalyst for aromatic hydrocarbon production or reforming |
-
2004
- 2004-09-27 CN CNB2004100802032A patent/CN100434495C/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104342195A (en) * | 2013-07-25 | 2015-02-11 | 中国石油天然气股份有限公司 | Catalyst lifting device of continuous catalytic reforming device |
| CN104342195B (en) * | 2013-07-25 | 2016-09-07 | 中国石油天然气股份有限公司 | Catalyst lifting device of continuous catalytic reforming device |
| CN105148986A (en) * | 2015-09-30 | 2015-12-16 | 西南化工研究设计院有限公司 | Methanol-to-olefin catalyst bed temperature rise and regeneration device |
| CN116059802A (en) * | 2021-10-29 | 2023-05-05 | 中国石油化工股份有限公司 | A method and system for drying and dehydrating acid gas |
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| Publication number | Publication date |
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| CN100434495C (en) | 2008-11-19 |
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