CN100393848C - Catalytic cracking conversion method with relay use of catalyst curd its device - Google Patents
Catalytic cracking conversion method with relay use of catalyst curd its device Download PDFInfo
- Publication number
- CN100393848C CN100393848C CNB2005100178664A CN200510017866A CN100393848C CN 100393848 C CN100393848 C CN 100393848C CN B2005100178664 A CNB2005100178664 A CN B2005100178664A CN 200510017866 A CN200510017866 A CN 200510017866A CN 100393848 C CN100393848 C CN 100393848C
- Authority
- CN
- China
- Prior art keywords
- gasoline
- reaction
- reactor
- heavy oil
- oil
- 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 title claims abstract description 257
- 239000003054 catalyst Substances 0.000 title claims abstract description 70
- 238000004523 catalytic cracking Methods 0.000 title claims abstract description 29
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000003502 gasoline Substances 0.000 claims abstract description 173
- 239000000295 fuel oil Substances 0.000 claims abstract description 143
- 239000003921 oil Substances 0.000 claims abstract description 90
- 239000007787 solid Substances 0.000 claims abstract description 22
- 238000000926 separation method Methods 0.000 claims abstract description 13
- 230000008929 regeneration Effects 0.000 claims description 25
- 238000011069 regeneration method Methods 0.000 claims description 25
- 239000013049 sediment Substances 0.000 claims description 17
- 238000002791 soaking Methods 0.000 claims description 17
- 230000001172 regenerating effect Effects 0.000 claims description 10
- 239000003795 chemical substances by application Substances 0.000 claims description 7
- 230000000994 depressogenic effect Effects 0.000 claims description 7
- 235000008733 Citrus aurantifolia Nutrition 0.000 claims description 5
- 235000011941 Tilia x europaea Nutrition 0.000 claims description 5
- 239000004571 lime Substances 0.000 claims description 5
- 238000012546 transfer Methods 0.000 claims description 5
- 230000007246 mechanism Effects 0.000 claims description 4
- 230000009849 deactivation Effects 0.000 claims description 3
- 238000004939 coking Methods 0.000 claims description 2
- 238000005336 cracking Methods 0.000 abstract description 8
- 238000005504 petroleum refining Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 38
- 150000001336 alkenes Chemical class 0.000 description 18
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 17
- 230000035484 reaction time Effects 0.000 description 16
- 230000000694 effects Effects 0.000 description 12
- 239000000047 product Substances 0.000 description 11
- 230000003197 catalytic effect Effects 0.000 description 5
- 239000000571 coke Substances 0.000 description 5
- 238000005516 engineering process Methods 0.000 description 5
- 230000004048 modification Effects 0.000 description 5
- 238000012986 modification Methods 0.000 description 5
- 239000002994 raw material Substances 0.000 description 5
- 239000012295 chemical reaction liquid Substances 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 125000004435 hydrogen atom Chemical class [H]* 0.000 description 3
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 2
- 239000005864 Sulphur Substances 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 239000002826 coolant Substances 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- -1 inlet Substances 0.000 description 2
- 238000006317 isomerization reaction Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- TVMXDCGIABBOFY-UHFFFAOYSA-N octane Chemical compound CCCCCCCC TVMXDCGIABBOFY-UHFFFAOYSA-N 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000000889 atomisation Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 230000001143 conditioned effect Effects 0.000 description 1
- 230000006837 decompression Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 239000002010 green coke Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 230000009257 reactivity Effects 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 230000004044 response Effects 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000001256 tonic effect Effects 0.000 description 1
Images
Landscapes
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention is a catalyst relay catalytic cracking conversion method and device, belonging to petroleum refining technical field, making raw oil and back-refined oil firstly perform catalytic cracking reaction in the respective risers, successively merging and extracting deactivated catalyst, where the reacting oil gas changes to contact with low temperature catalyst used in the gasoline reaction and continue reaction; a heavy oil reactor is connected in parallel with a gasoline reactor; the gasoline and catalyst complete reaction in the gasoline reactor and then can make gas-solid separation in a gasoline settler, where the oil gas is discharged through pipeline, the extracted catalyst is fed into the position below heavy oil modifying reaction stage and cracking reaction stage to continue heavy oil reaction and can also be fed into a gas-solid separator arranged in the heavy oil modifying reaction stage for separating, where the gasoline gas is directly drawn out and the catalyst takes part in the reaction in this stage; a catalyst return pipe is arranged between the gasoline settler and gasoline reactor bottoms to make a part of catalyst used in the gasoline reaction return to the gasoline reactor bottom so as to take part in the gasoline reaction again.
Description
Technical field
The invention belongs to the petroleum refining technology field, catalytic cracking conversion method and device thereof that particularly a kind of catalyzer relay is used.
Background technology
Catalytic cracking is most important heavier petroleum fraction (comprising decompressed wax oil, wax tailings, normal pressure oil expression, decompression oil expression an etc.) processing unit (plant), is the production equipment of Chinese 80% gasoline.Catalytic cracking reaction uses riser reactor, and reaction raw materials enters in the riser tube bottom, and under the catalyzer environment, with the flow velocity about average 15m/s, the temperature about 500 ℃ is reacted, and the reaction times, generally about 3s, riser tube length was at 30～40 meters.Because raw material has 7～10% can change into coke approximately in the reaction process, these coke make catalyst deactivation attached in catalyst surface and the hole, the forfeiture catalytic capability.A large amount of full scale plant and experimental studies prove that heavy oil catalytic cracking process can make the regenerated catalyst loss of activity more than 50% through the 1s left and right sides time.For conventional riser reactor, usually main catalytic cracking reaction occurs in 1/3rd reaction zones of riser tube bottom, and riser tube latter half catalysis has been lost due effect substantially with a little less than quite.Opposite, because 500 ℃ high temperature, the ratio of thermally splitting is more outstanding, further produces byproducts such as dry gas and coke, has influenced economic benefit.On the other hand, the main products gasoline and the diesel quality of conventional catalytic cracking reaction process are not high, and especially content of olefin in gasoline is many 45～55% (v).And the recent standard that Environmental Protection in China requires is olefin(e) centent (v), developed country then requires olefin(e) centent (v), to propose great challenge to catalytic cracking unit less than 18% less than 35%.
In order to improve the efficient of riser reactor, improve the yield and the benefit of purpose product, how improving riser tube second half section activity of such catalysts is major issue.Chinese patent CN1118539C has proposed a kind of two-part riser tube reaction method.This patent is divided into two short riser tube series connection up and down to conventional riser tube, and the reaction times of each riser tube all shortens to about 1s.After the raw material riser tube reaction below, catalyzer is inactivation, and these catalyzer are isolated from reaction oil gas, sends into revivifier and recovers active; Oil gas then enters second riser tube of top; Replenish highly active regenerated catalyst by transport pipe in second riser tube, these regenerated catalysts are normally handled through cooling, as adopting the heat collector cooling.The effect of this invention is that the riser reactor second half section is replaced by brand-new regenerated catalyst, has reached the efficient of first section of reactor fully, can significantly improve the purpose product yield, generally can improve about 1.5%.Shortcoming is that energy consumption is higher.Catalyzer is sent into second section riser tube from regenerator bottoms want a large amount of delivery mediums and energy consumption.A large amount of delivering vapors enters second conversion zone, influences second section reaction.In addition, still there is the olefin(e) centent height in its gasoline, can't satisfy the problem of environmental requirement.
Chinese patent application 99109193.0,02149313.8 and CN1587352A have proposed more to relax a little schemes, carbon deposited catalyst in the riser tube of bottom is not separated, still participate in the reaction of reactor second half section, but replenish the partial regeneration catalyzer at the riser tube middle part, reach and improve active purpose of reactor second half section.This kind scheme has reduced middle catalyst separating link, but owing to all kept carbon deposited catalyst, reactor second half section catalyst activity increase rate is less, and the efficiency improvement degree also is restricted naturally.Still there is the catalyst transport energy consumption in addition and can't improves the quality of gasoline problem.
In order to reduce the olefin(e) centent that catalytic cracking reaction generates gasoline, use in a large number at heavy oil riser tube middle part and inject heat-eliminating medium, make reactor latter half of under lower temperature environments, suppress heat cracking reaction and over-drastic catalytic cracking reaction, strengthen the reaction that hydrogen transference, isomerization etc. help dropping to olefin(e) centent, obtained certain effect.
In order to reduce catalytic cracking gasoline olefine content by a relatively large margin, method is gasoline to be reacted again carry out upgrading preferably.Application number is 02139064.9,02116786.9 patent proposed on catalytic cracking unit to set up separately the method for a riser reactor for gasoline, the content of olefin in gasoline that heavy oil catalytic cracking reaction is generated drops to 15% (v), and increases octane value.
Chinese patent application CN1438296A, CN1526794A have proposed to design the method that three riser tubes are respectively applied for stock oil, recycle stock and gasoline reaction.Because three cover reactive systems all are independently, be substantially conventional process repeat be provided with, can not be with each reaction conditions usefulness mutually, also to set up delivery system and storing unit for stock oil and recycle stock react required catalyzer, too complicated.
Because gasoline reaction green coke seldom, independently the catalyst carbon deposit behind the gasoline reactor reaction is few, still have higher activity, and temperature of reaction is lower.In the prior art, these characteristics of gasoline reaction are not fully utilized.
Summary of the invention
The object of the present invention is to provide and a kind ofly can the degree of depth reduce the catalytic gasoline olefin(e) centent, can improve the heavy oil reaction efficiency again, improve catalytic cracking conversion method and device thereof that the catalyzer relay of yield is used.
For achieving the above object, the present invention takes following technical scheme: the catalytic cracking conversion method that a kind of catalyzer relay is used, the heavy oil reaction process is divided into two conversion zones up and down, below first conversion zone, stock oil and recycle stock carry out catalytic cracking reaction respectively in two riser tubes arranged side by side, mix then, enter the gas solid separation district, the catalyzer of coking deactivation is separated from reaction oil gas send with catalyzer; Oil gas upwards enters second conversion zone, in this district with use through gasoline reaction after catalyst mix, proceed to react, finish the reaction of requirement after, the catalyzer of second conversion zone and reaction oil gas are sent the heavy oil reactor from outlet pipe; The heavy oil reactor is other to be set up in parallel the gasoline reactor, finishes the gasoline catalyst for reaction and is admitted to the heavy oil reactor, continues to participate in the heavy oil reaction.
Enter petrol sediment bulb gasoline and catalyzer are finished reaction in the gasoline reactor after and carry out gas solid separation, the oil gas well lines sends, isolatedly finished that the gasoline catalyst for reaction is admitted to heavy oil reactor second conversion zone or/and first conversion zone participates in the heavy oil reaction.
Finish the oil gas of gasoline reaction and catalyzer at the gasoline reactor and together be admitted to heavy oil reactor second conversion zone and carry out gas solid separation, isolated catalyzer participates in the heavy oil reaction, and oil gas is directly drawn.
Finishing the gasoline catalyst for reaction is partly refluxed to the gasoline reactor bottom and mixes the back with regenerated catalyst and continue to participate in the gasoline reaction.
Gasoline reactor, the shared cover regenerating unit of heavy oil reactor.
Heavy oil first conversion zone stock oil and recycle stock oil gas mean residence time are not more than 1.5s, 490～600 ℃ of temperature of reaction; When being purpose with voluminous petrol and diesel oil, temperature of reaction preferentially is recommended as 490～520 ℃, and when being purpose with the more producing chemical industry product, temperature of reaction is 530～600 ℃.The heavy oil second conversion zone temperature of reaction adopts the long reaction times of 2.5～5s than low 5～30 ℃ of first reaction zone.
The catalytic cracking conversion system that the catalyzer relay is used, the gasoline reactor that comprises the heavy oil reactor and be set up in parallel with it, the heavy oil reactor is composed in series by the soaking section of bottom, the separation stripping stage at middle part and the upgrading conversion zone on top, soaking section comprises stock oil riser tube and the recycle stock riser tube that is arranged in parallel, separate stripping stage and be provided with catalyst separating stripping mechanism and reclaimable catalyst standpipe, the gasoline reactor is connected by transfer lime with the heavy oil reactor.
The gasoline reactor outlet connects petrol sediment bulb, petrol sediment bulb by gasoline catalysts regeneration standpipe with heavy oil reactor upgrading conversion zone or/and soaking section bottom be connected.
Be provided with the petrol vapour solid separator in the heavy oil reactor upgrading conversion zone, its upper end connects the gasoline riser, the lower end connects gasoline catalyzing agent depressant prescription pipe, the depressant prescription pipe extends upgrading conversion zone bottom, form heavy oil reaction oil institute and catalyst channels between petrol vapour solid separator and the upgrading conversion zone tube wall, gasoline reactor oil gas is connected with petrol vapour solid separator inlet with the catalyzer fairlead.
Be provided with the catalyzer return line between petrol sediment bulb and the gasoline reactor bottom.
The recycle stock riser tube of heavy oil reactor is located at outside the stock oil riser tube, and its upper end joins; The upgrading conversion zone adopts riser tube form or fluidized-bed form; Gasoline reactor, the shared cover regenerating unit of heavy oil reactor.
The recycle stock riser tube of heavy oil reactor is sheathed in the stock oil riser tube, and the two is axially identical; The upgrading conversion zone adopts riser tube form or fluidized-bed form; Gasoline reactor, the shared cover regenerating unit of heavy oil reactor.
Generally speaking, the reacted catalyzer of gasoline all enters heavy oil and reacts second conversion zone (upgrading conversion zone).The reacted catalyzer of gasoline also can partly enter heavy oil and react first conversion zone (soaking section) recycle stock riser tube, after regenerated catalyst mixes, participates in the reaction of heavy oil first conversion zone.
After the reaction of heavy oil first conversion zone finishes, whole decaying catalysts are isolated, the part catalyst separating is gone out, still keep a part and enter second conversion zone, continue to participate in the heavy oil reaction.
The present invention makes heavy oil react second conversion zone and is replaced by gasoline and reacts used catalyzer, has increased substantially this section activity of such catalysts, has improved the efficient of heavy oil reactor; Because the reacted catalyst temperature of gasoline is lower than regenerated catalyst temperature, make the temperature of reaction of heavy oil second conversion zone be easy to reduce, help suppressing heat cracking reaction, improve product yield; The low-temp reaction condition of second conversion zone helps the reaction that hydrogen transference etc. reduces content of olefin in gasoline, can improve quality of gasoline; The reacted catalyzer of gasoline enters the recycle stock riser tube in the soaking section, and the catalyst temperature that contacts with recycle stock is reduced, and improves the agent-oil ratio of reaction, strengthens the recycle stock reaction; Owing to need not specially the catalyzer of mending heavy oil second conversion zone to be promoted conveying, saved the energy consumption that middle tonic needs.The present invention is provided with the gasoline reactor, and (v), octane value improves about 1 unit can to make quality of gasoline first mate raising, particularly olefin(e) centent can reduce to 15%.The reacted catalyzer of gasoline is participated in heavy oil reaction again, and the low temperature of gasoline post catalyst reaction, high reactivity characteristics are made full use of, and has reduced regenerated is influenced.The reacted catalyzer of gasoline refluxes, and gasoline is reduced with the temperature that contacts of catalyzer, improves the agent-oil ratio of gasoline reaction simultaneously, reduces the loss of gasoline reaction.
Description of drawings
Fig. 1 is that (heavy oil second conversion zone adopts the riser tube pattern to apparatus of the present invention structural representation, and the heavy oil first conversion zone recycle stock riser tube is located at outside the stock oil riser tube; Finish the reacted catalyzer of gasoline and introduce the heavy oil reactor);
Fig. 2 is that (heavy oil second conversion zone adopts the fluidized-bed pattern to second kind of structural representation of apparatus of the present invention, and the heavy oil first conversion zone recycle stock riser tube is located in the stock oil riser tube; Finish the reacted catalyzer of gasoline and introduce the heavy oil reactor);
Fig. 3 is that (heavy oil second conversion zone adopts the fluidized-bed pattern to the third structural representation of apparatus of the present invention, and the heavy oil first conversion zone recycle stock riser tube is located at outside the stock oil riser tube; Finish the reacted catalyzer of gasoline and introduce the heavy oil reactor, the gasoline reactor is provided with the catalyzer return line);
Fig. 4 is that (the heavy oil first conversion zone recycle stock riser tube is arranged in the stock oil riser tube the 4th kind of structural representation of apparatus of the present invention, and heavy oil second conversion zone is the riser tube pattern; Finish the reacted catalyzer of gasoline and introduce the heavy oil reactor);
Fig. 5 is that (the heavy oil first conversion zone recycle stock riser tube is arranged on outside the stock oil riser tube the 5th kind of structural representation of apparatus of the present invention; After the gasoline oil gas of finishing gasoline reaction and catalyzer were introduced heavy oil reactor second conversion zone and separated, catalyzer participated in heavy oil modification and reacts);
Fig. 6 is that (the heavy oil first conversion zone recycle stock riser tube is arranged in the stock oil riser tube the 6th kind of structural representation of the present invention; After the gasoline oil gas of finishing gasoline reaction and catalyzer were introduced heavy oil reactor second conversion zone and separated, catalyzer participated in heavy oil modification and reacts);
Fig. 7 is for using the reaction-regenerative device structural representation of Fig. 1 device.
Embodiment
At the gasoline catalysts through entering after the petrol sediment bulb sedimentation under the heavy oil reactor situation, 180～250 ℃ stock oil 11, recycle stock 21 about 350 ℃ is by after the nozzle atomization, through stock oil inlet 15, recycle stock inlet 25 enters heavy oil first conversion zone (soaking section) riser reactor separately, upwards flow along riser tube with the flow velocity about 10m/s, regenerated catalyst enters the pre lift zone of riser tube bottom through the regeneration standpipe, under the effect of pre-lifting medium, upwards enter reaction zone, with stock oil, the recycle stock contact, the limit reaction, upwards flow in the limit, under 500～550 ℃ of temperature environments, finished the catalytic cracking reaction of fs through 1 second left and right sides time, after the reactant of two riser tubes merges, catalyst separating in the middle of entering, stripping stage 40 is isolated catalyzer from oil gas; Isolated catalyzer by steam stripped after, send into revivifier regeneration from regeneration standpipe 41, recover active; Oil gas then continues upwards to enter second conversion zone (upgrading conversion zone) and react; Second conversion zone (upgrading conversion zone) is replaced by gasoline and is reacted used catalyzer, and the temperature of reaction of second conversion zone is low than first conversion zone, generally differs 5 ℃～30 ℃, can regulate by the fractional dose and the cooling medium of one section catalyzer; Reaction times 1～the 5s of second conversion zone changes according to product requirement: when the high vapour of major requirement, diesel yield, adopt the short reaction times, as 1～2s, when requiring to produce gasoline with low olefine content, adopt the longer reaction times of 3～5s; Except that continuing to finish the catalytic cracking reaction, also suppressed heat cracking reaction in second conversion zone, carried out product upgradings such as hydrogen transference, isomerization simultaneously and transform; After finishing the reaction process of requirement, reaction oil gas and catalyzer flow out heavy oil reactor 100 from outlet pipe 54, enter heavy oil settling vessel 60, isolated catalyzer by gas-solid separator, oil gas is through gas pipeline 62 bleeders, catalyzer then contacts with steam in stripper 80, displaces entrained oil gas, enters revivifier 70 from regeneration standpipe 81 then; The branch output that the reaction of first conversion zone finishes the middle catalyzer in back can change according to the requirement of heavy oil second conversion zone temperature of reaction and reaction depth, can all separate and displace, also can only separate a displacement part, keep a part and continue to participate in second section reaction.40～70 ℃ gasoline 31 enters gasoline reactor 200 through gasoline inlet 35, regenerated catalyst is through regeneration standpipe 71B, the reacted catalyzer of gasoline enters the catalyst mix of bottom through return line 34, pre lift zone 32, after two strands of catalyzer mix earlier, under the effect of pre-lifting medium 33, enter reaction zone, contact with gasoline, 400～500 ℃ of temperature, under agent-oil ratio 6～10 environment, after the 36s time is finished reaction, enter settling vessel 37, isolated catalyzer by gas-solid separator 38, oil gas is through pipeline 39 bleeders, catalyzer is then as required through gasoline reaction regeneration standpipe 53,53B sends into heavy oil second conversion zone (upgrading conversion zone) 50 and first conversion zone (soaking section) 10 respectively, the catalyst mix of 20 riser tubes bottom, pre lift zone 12,22, or all send into heavy oil second conversion zone, continue to participate in the heavy oil reaction, should preferentially make the reacted catalyzer of gasoline enter heavy oil second conversion zone; The catalyzer that enters revivifier 70 contacts with air under 650～720 ℃ of temperature regenerates, and after the recovery activity, enters each reactor through regeneration standpipe 71A, 71B, 71C, finishes circulation.In order to adapt to heavy oil and the different reaction conditions of gasoline reaction, the present invention can use the single hop regeneration, also can use the regeneration of two revivifiers, can also use single device two-stage regeneration mode.For improving the gasoline reaction effect, reduce dry gas yied, the present invention makes the reacted catalyzer of part gasoline return the gasoline reactor bottom, makes the regenerated catalyst cooling that contacts with gasoline; The reacted catalyzer of gasoline generally directly enters the heavy oil reactor, does not need stripping, also can enter the heavy oil reactor again behind the first stripping.The temperature of reaction of gasoline reaction and heavy oil first conversion zone is by guiding valve 73A, 73B, 73C control; The temperature of reaction procatalyst is by guiding valve 36 controls in the gasoline reactor.The gasoline that gasoline reactor of the present invention uses can also can be the gasoline of other devices from the self-produced gasoline of this device.
The oil gas and the gasoline catalyzing agent that form in gasoline reaction back enter under the heavy oil reactor second conversion zone situation together, gasoline oil gas and gasoline catalyzing agent are sent in heavy oil reactor second conversion zone in the petrol vapour solid separator through transfer lime, inlet, gasoline oil gas after the separation through gasoline riser independently directly draw, catalyzer enters heavy oil second conversion zone bottom and heavy oil reaction oil gas through heavy oil first conversion zone through the depressant prescription pipe and is blended in and promotes steam and promote up reaction down, after fairlead enters regenerating unit.The heavy oil oil gas that forms through heavy oil first conversion zone upwards enter with catalyzer separate, stripping stage, reclaimable catalyst after gas solid separation enters regenerating unit through regeneration standpipe, and heavy oil oil gas upwards enters the isolated catalyst mix of heavy oil second conversion zone and gasoline reaction back and carries out the upgrading reaction.Other enter heavy oil reactor situation with the gasoline catalysts after the petrol sediment bulb sedimentation.
The catalytic cracking conversion system (see figure 1) that embodiment 1, catalyzer relay are used, the gasoline reactor 200 that comprises heavy oil reactor 100 and be set up in parallel with it.Heavy oil reactor 100 is composed in series by the soaking section of bottom, the separation stripping stage 40 at middle part and the upgrading conversion zone 50 on top, soaking section comprises stock oil riser tube 10 and the recycle stock riser tube 20 that is arranged in parallel, recycle stock riser tube 20 is located at stock oil riser tube 10 outsides, and its upper end joins.Separation stripping stage 40 is provided with catalyst separating stripping mechanism and reclaimable catalyst standpipe 41,41 is recommended matter for the reclaimable catalyst gas of heavy oil soaking section, and 43 is guiding valve to be generated, and catalyst separating stripping mechanism adopts ability and routine techniques; Upgrading conversion zone 50 adopts the riser tube forms, the 54 oil reactor outlet pipes of attaching most importance to, and cooling medium 52 can enter the adjustment temperature of reaction from the tube wall inlet.200 outlets of gasoline reactor connect petrol sediment bulb 37, and petrol sediment bulb 37 is connected with heavy oil reactor upgrading conversion zone 50 bottoms by gasoline catalysts regeneration standpipe 53, guiding valve to be generated 56, and 38 is the petrol vapour solid separator, and 39 is the gasoline gas pipeline.Being provided with catalyzer return line 34,36 between petrol sediment bulb 37 and gasoline reactor 200 bottoms is guiding valve.Gasoline reactor 200, heavy oil reactor 100 shared cover regenerating units.
11,21,31 be respectively stock oil, recycle stock and gasoline, 15,25,35 are respectively stock oil, recycle stock and gasoline inlet; 13,23,33 is the pre-medium that promotes, and enters from reactor bottom; 12,22,32 be respectively stock oil, recycle stock, gasoline catalyzing agent mixing, pre lift zone; 71A, 71B, 71C are the regeneration standpipe, and 73A, 73B, 73C are the regeneration guiding valve.
Adopt the present embodiment device anti--refill to put and see Fig. 5, regenerating unit is a routine techniques.Among the figure, 60 is the heavy oil settling vessel, and 61 is cyclone separator, and 62 is gas pipeline; 70 is revivifier; 80 is stripper, and 81 is regeneration standpipe; 77 is external warmer, and 75 is air.
Adopt following condition 1 to compare reaction: reaction mass is: the defeated atmospheric residue of pipe, and 100t/h heavy oil, gasoline feeding are that whole heavy oil react self-produced gasoline; 220 ℃ of heavy oil preheatings, 40 ℃ in gasoline; Raw material oil content four tunnel incoming stock oil risers, freshening oil content two-way enters the recycle stock riser tube; Gasoline divides two-way to enter the gasoline reactor; 510 ℃ of stock oil riser tube temperature of reaction, reaction times 0.8s; 515 ℃ of recycle stock riser tube temperature of reaction, reaction times 1s; 495 ℃ of heavy oil modification conversion zone temperature of reaction, reaction times 2.8s; 450 ℃ of gasoline temperature of reaction, reaction times 2.3s, gasoline reaction procatalyst temperature is by 580 ℃ of controls; 690 ℃ of regeneration temperatures; Heavy oil is finished the reacted catalyzer of soaking section and is all isolated (fractional dose is greater than 95%), and the reacted catalyzer of gasoline all enters heavy oil reactor upgrading conversion zone.
Comparative Examples: adopt existing independently double lifting leg reaction technology, conventional riser tube is used in gasoline reaction and heavy oil reaction; The gasoline reaction directly contacts with regenerated catalyst, and the reacted catalyzer of gasoline directly enters revivifier; What the heavy oil reactive moieties was different with the embodiment of the invention is, stock oil, the shared conventional riser tube of recycle stock, and catalyst changeout is declined in the centre.
The contrast reaction result provides in table 1.As can be seen, under identical reaction conditions, heavy oil reaction liquid product yield of the present invention has increased by 2.0 percentage points, generates gasoline olefin and reduces by 12 percentage points; Gasoline reaction result gasoline loss has again reduced 30%, and alkene has descended 20%.
Adopt following condition 2 to compare reaction: reaction mass is: the grand celebration atmospheric residue, and 100t/h heavy oil, gasoline feeding are the catalytic gasoline of other devices, 40t/h; 220 ℃ of heavy oil preheatings, 40 ℃ in gasoline; Raw material oil content four tunnel incoming stock oil risers, freshening oil content two-way enters the recycle stock riser tube; Gasoline divides two-way to enter reactor; 510 ℃ of heavy oil cracking conversion zone temperature of reaction, reaction times 1.0s; 490 ℃ of heavy oil modification conversion zone temperature of reaction, reaction times 3.5s; 410 ℃ of gasoline temperature of reaction, reaction times 3.5s; The backflow catalytic amount is according to the requirement control of 550 ℃ of gasoline reaction procatalyst temperature; 690 ℃ of regeneration temperatures; The reacted catalyzer of gasoline all enters the heavy oil modification conversion zone; The used catalyst separating of heavy oil cracking conversion zone is gone out 85%, keep the reaction of 15% participation upgrading conversion zone.
Comparative Examples: not existing together of heavy oil reactive moieties and embodiment is, the heavy oil reaction is used and is divided into the riser tube in two districts up and down, stock oil, the shared reactor of recycle stock replenish the reclaimable catalyst of heavy oil reaction back (Tathagata is from the heavy oil settling vessel) to second reaction zone.Not existing together of gasoline reactive moieties and embodiment be, from the high temperature catalyst of revivifier directly and the gasoline contact reacts, reacted catalyzer directly enters revivifier.
Comparing result sees Table 2.From table 2 data as can be seen, under identical reaction conditions, heavy oil reaction liquid product yield of the present invention has increased by 1.4 percentage points, and gasoline olefin reduces by 5 percentage points more; After gasoline reacted again, olefin(e) centent can hang down 25%, and sulphur content is low by 28%, and dry gas adds coke to be reduced.
Employing condition 2 compares with three sections reaction scheme using CN1438269A, and comparing result provides in table 3.As can be seen, under identical reaction conditions, heavy oil reaction liquid product yield of the present invention has increased by 0.4 percentage point, and gasoline olefin reduces by 12 percentage points more; After gasoline reacted again, olefin(e) centent can hang down 25%, and sulphur content is low by 28%, and dry gas adds coke to be reduced.
Embodiment 2, present embodiment device be as different from Example 1: the recycle stock riser tube 20 of heavy oil reactor 100 is sheathed in the stock oil riser tube 10, and the two is axially identical; Recycle stock 21 enters recycle stock riser tube 20 from reactor bottom, stock oil riser tube 10, recycle stock riser tube 20 shared regeneration standpipe 71A, guiding valve 73A.Upgrading conversion zone 50 adopts the fluidized-bed form, and 51 are heavy oil reaction transfer lime.Do not establish the catalyzer return line between petrol sediment bulb 37 and gasoline reactor 200 bottoms.
Embodiment 3, present embodiment device be as different from Example 1: upgrading conversion zone 50 adopts the fluidized-bed forms, and 51 react transfer lime for heavy oil.
Device as different from Example 1 in embodiment 4, the present embodiment: the recycle stock riser tube 20 of heavy oil reactor 100 is sheathed in the stock oil riser tube 10, and the two is axially identical; Recycle stock 21 enters recycle stock riser tube 20 from reactor bottom, stock oil riser tube 10, recycle stock riser tube 20 shared regeneration standpipe 71A, guiding valve 73A.Petrol sediment bulb 37 is connected with heavy oil reactor soaking section bottom by gasoline catalysts regeneration standpipe 53B, guiding valve 56B.Do not establish the catalyzer return line between petrol sediment bulb 37 and gasoline reactor 200 bottoms.
Device as different from Example 1 in embodiment 5, the present embodiment, be provided with petrol vapour solid separator 501 in the upgrading conversion zone 50 of heavy oil reactor 100, its upper end connects gasoline riser 502, the lower end connects gasoline catalyzing agent depressant prescription pipe 503, depressant prescription pipe 503 extends upgrading conversion zone 50 bottoms, forms heavy oil reaction oil gas and catalyst channels between petrol vapour solid separator 501 and upgrading conversion zone 50 tube walls.Petrol sediment bulb is not established in 200 outlets of gasoline reactor, does not establish gasoline catalyzing agent return line on it yet, and its oil gas directly is connected with petrol vapour solid separator 50 inlets 504 with catalyzer fairlead 391.
Adopt following conditioned response: 200 ℃ of stock oil feeding temperatures, 350 ℃ of recycle stock, 40 ℃ in gasoline.520 ℃ of stock oil cracking reaction temperature, 515 ℃ of recycle stock cracking reaction temperature, 498 ℃ of second section temperature of reaction of heavy oil, 420 ℃ of gasoline temperature of reaction.0.8 second stock oil catalytic cracking section reaction times, recycle stock soaking time 1.2 seconds, 3 seconds gasoline reaction times, the 3.0 seconds second conversion zone reaction times of heavy oil.Isolating catalytic amount in the middle of the heavy oil reaction is 80% of catalytic cracking section catalyzer.
Compare with conventional catalytic cracking technology, heavy oil reaction liquid product yield improves 1.5%, and heavy oil reaction direct production content of olefin in gasoline reduces by 20 percentage points; After the gasoline reaction, content of olefin in gasoline reduces to 15% (v).
Device as different from Example 5 in embodiment 6, the present embodiment, soaking section at heavy oil reactor 100, recycle stock riser tube 20 is arranged on stock oil riser tube 10 inside, and the two shared regeneration standpipe 72 and regeneration guiding valve 74, recycle stock 21 enter in the bottom.
Table 1, embodiment 1 scheme and prior art contrast
Table 2, embodiment 2 schemes and prior art contrast
The technology contrast of table 3, embodiment 2 schemes and CN1438269A
Claims (12)
1. the catalytic cracking conversion method that uses of a catalyzer relay, it is characterized in that, the heavy oil reaction process is divided into two conversion zones up and down, below first conversion zone, stock oil and recycle stock carry out catalytic cracking reaction respectively in two riser tubes arranged side by side, mix then, enter the gas solid separation district, the catalyzer of coking deactivation is separated from reaction oil gas send with catalyzer; Oil gas upwards enters second conversion zone, in this district with use through gasoline reaction after catalyst mix, proceed to react, finish the reaction of requirement after, the catalyzer of second conversion zone and reaction oil gas are sent the heavy oil reactor from outlet pipe; The heavy oil reactor is other to be set up in parallel the gasoline reactor, finishes the gasoline catalyst for reaction and is admitted to the heavy oil reactor, continues to participate in the heavy oil reaction.
2. the method for claim 1, it is characterized in that, enter petrol sediment bulb gasoline and catalyzer are finished reaction in the gasoline reactor after and carry out gas solid separation, the oil gas well lines sends, isolatedly finished that the gasoline catalyst for reaction is admitted to heavy oil reactor second conversion zone or/and first conversion zone participates in the heavy oil reaction.
3. the method for claim 1 is characterized in that, finishes the oil gas of gasoline reaction and catalyzer at the gasoline reactor and together is admitted to heavy oil reactor second conversion zone and carries out gas solid separation, and isolated catalyzer participates in the heavy oil reaction, and oil gas is directly drawn.
4. method as claimed in claim 2 is characterized in that, finishes the gasoline catalyst for reaction and is partly refluxed to the gasoline reactor bottom and mixes the back with regenerated catalyst and continue to participate in the gasoline reaction.
5. as claim 1,2,3 or 4 described methods, it is characterized in that gasoline reactor, the shared cover regenerating unit of heavy oil reactor.
6. method as claimed in claim 5 is characterised in that, heavy oil first conversion zone stock oil and recycle stock oil gas mean residence time are not more than 1.5s, 490～600 ℃ of temperature of reaction; The heavy oil second conversion zone temperature of reaction is than low 5～30 ℃ of first reaction zone.
7. the catalytic cracking conversion system that uses of catalyzer relay, it is characterized in that, the gasoline reactor that comprises the heavy oil reactor and be set up in parallel with it, the heavy oil reactor is composed in series by the soaking section of bottom, the separation stripping stage at middle part and the upgrading conversion zone on top, soaking section comprises stock oil riser tube and the recycle stock riser tube that is arranged in parallel, separate stripping stage and be provided with catalyst separating stripping mechanism and reclaimable catalyst standpipe, the gasoline reactor is connected by transfer lime with the heavy oil reactor.
8. device as claimed in claim 7 is characterized in that the gasoline reactor outlet connects petrol sediment bulb, petrol sediment bulb by gasoline catalysts regeneration standpipe with heavy oil reactor upgrading conversion zone or/and soaking section bottom be connected.
9. device as claimed in claim 7, it is characterized in that, be provided with the petrol vapour solid separator in the heavy oil reactor upgrading conversion zone, its upper end connects the gasoline riser, the lower end connects gasoline catalyzing agent depressant prescription pipe, the depressant prescription pipe extends upgrading conversion zone bottom, form heavy oil reaction oil gas and catalyst channels between petrol vapour solid separator and the upgrading conversion zone tube wall, gasoline reactor oil gas is connected with petrol vapour solid separator inlet with the catalyzer fairlead.
10. device as claimed in claim 8 is characterized in that, is provided with the catalyzer return line between petrol sediment bulb and the gasoline reactor bottom.
11., it is characterized in that the recycle stock riser tube of heavy oil reactor is located at outside the stock oil riser tube as claim 7,8,9 or 10 described devices, its upper end joins; The upgrading conversion zone adopts riser tube form or fluidized-bed form; Gasoline reactor, the shared cover regenerating unit of heavy oil reactor.
12., it is characterized in that the recycle stock riser tube of heavy oil reactor is sheathed in the stock oil riser tube as claim 7,8,9 or 10 described devices, the two is axially identical; The upgrading conversion zone adopts riser tube form or fluidized-bed form; Gasoline reactor, the shared cover regenerating unit of heavy oil reactor.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100178664A CN100393848C (en) | 2005-08-08 | 2005-08-08 | Catalytic cracking conversion method with relay use of catalyst curd its device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2005100178664A CN100393848C (en) | 2005-08-08 | 2005-08-08 | Catalytic cracking conversion method with relay use of catalyst curd its device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1912067A CN1912067A (en) | 2007-02-14 |
| CN100393848C true CN100393848C (en) | 2008-06-11 |
Family
ID=37721131
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2005100178664A Expired - Fee Related CN100393848C (en) | 2005-08-08 | 2005-08-08 | Catalytic cracking conversion method with relay use of catalyst curd its device |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100393848C (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102051210B (en) * | 2009-11-04 | 2014-07-16 | 青岛京润石化设计研究院有限公司 | Dual-riser petroleum hydrocarbon feed stock catalytic conversion method and device |
| WO2012062173A1 (en) * | 2010-11-11 | 2012-05-18 | Shi Baozhen | Catalytic cracking method and apparatus |
| CN102465006B (en) * | 2010-11-11 | 2014-01-29 | 石宝珍 | Catalytic cracking method and device |
| CN102477311A (en) * | 2010-11-28 | 2012-05-30 | 石宝珍 | Catalytic cracking method and its apparatus |
| CN102485840B (en) * | 2010-12-01 | 2014-03-05 | 石宝珍 | Catalytic cracking method and device thereof |
| CN102485841B (en) * | 2010-12-01 | 2014-02-26 | 石宝珍 | Catalytic cracking method and apparatus |
| CN102277193B (en) * | 2011-03-18 | 2014-04-02 | 青岛京润石化设计研究院有限公司 | Method and apparatus for catalytic cracking |
| CN102391889B (en) * | 2011-10-10 | 2013-12-18 | 石宝珍 | Catalytic conversion method |
| CN110240932B (en) * | 2018-05-29 | 2020-07-21 | 石宝珍 | Petroleum hydrocarbon multistage fluidized catalytic reaction method and reactor |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1490383A (en) * | 2003-03-18 | 2004-04-21 | 上海鲁齐信息科技有限公司 | Catfoming process and apparatus for producing high-quality gasoline and increasing light products and propylene |
-
2005
- 2005-08-08 CN CNB2005100178664A patent/CN100393848C/en not_active Expired - Fee Related
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1490383A (en) * | 2003-03-18 | 2004-04-21 | 上海鲁齐信息科技有限公司 | Catfoming process and apparatus for producing high-quality gasoline and increasing light products and propylene |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1912067A (en) | 2007-02-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN100393848C (en) | Catalytic cracking conversion method with relay use of catalyst curd its device | |
| JP5232135B2 (en) | Raw material oil conversion equipment using catalyst | |
| CN108017496B (en) | Apparatus for producing olefins and aromatic hydrocarbons and method thereof | |
| CN104583373A (en) | Fluid catalytic cracking process and apparatus for maximizing light olefins or middle distillates and light olefins | |
| CN101440014A (en) | Method for producing light olefins | |
| CN110117214A (en) | A kind of device and method of methanol Efficient Conversion producing light olefins | |
| CN110499182A (en) | A kind of catalyst cracking method of hydro carbons and its derivative | |
| CN100519704C (en) | Catalytic cracking method for producing more propylene | |
| CN102086402B (en) | Catalytic cracking method and device capable of increasing propylene yield and improving properties of gasoline | |
| CN102250641B (en) | Method and apparatus for preparing ethylene and propylene with maximized yield | |
| CN110194967B (en) | Catalytic reaction regeneration method for producing more propylene | |
| CN1888025B (en) | Catalytic conversion method and apparatus | |
| CN100519703C (en) | Catalytic conversion method of double reactor and its device | |
| CN100393847C (en) | Catalytic cracking conversion method of hydrocarbon raw material and its device | |
| CN102268286A (en) | C4 hydrocarbon catalytic splitting and heavy oil catalytic cracking combined technology and device | |
| CN112723970B (en) | Method for producing propylene, ethylene and aromatic hydrocarbon from heavy oil and catalytic conversion device | |
| CN201695001U (en) | Device for preparing ethylene and propylene | |
| CN100393849C (en) | Method and device of heavy oil two stage catalytic cracking reforming and gasoline upgrade coupling | |
| CN111606771B (en) | Methanol and light hydrocarbon coupling cracking device and method | |
| CN1861753A (en) | Catalyzing transforming process and apparatus of using gasoline heavy oil coupling reactor | |
| CN113366089A (en) | Process for converting naphtha containing feedstock to lower olefins and aromatics | |
| CN102276391B (en) | Method for catalyzing and converting methanol and naphtha into low-carbon olefins | |
| CN102276389B (en) | Reaction and regeneration device for catalyzing and converting methanol and naphtha into lower olefins | |
| CN212425965U (en) | Device for increasing aromatic hydrocarbon content in propylene and gasoline | |
| CN103788992A (en) | Catalytic cracking method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| ASS | Succession or assignment of patent right |
Owner name: SHI BAOZHEN Free format text: FORMER OWNER: LUOYANG PETRO-CHEMICAL EQUIPMENT INST. Effective date: 20110607 |
|
| C41 | Transfer of patent application or patent right or utility model | ||
| COR | Change of bibliographic data |
Free format text: CORRECT: ADDRESS; FROM: 471003 NO. 27, ZHONGZHOU WEST ROAD, LUOYANG CITY, HE NAN PROVINCE TO: 471003 609, TSINGHUA SCIENCE PARK, SANSHAN ROAD, HIGH-TECH. ZONE, LUOYANG CITY, HE NAN PROVINCE |
|
| 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, China, No. 27, No. Patentee before: Luoyang Petro-Chemical Equipment Inst. |
|
| C17 | Cessation of patent right | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20080611 Termination date: 20120808 |