CN102019211B - Equipment and method for degassing regenerated catalyst - Google Patents
Equipment and method for degassing regenerated catalyst Download PDFInfo
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- CN102019211B CN102019211B CN200910170273XA CN200910170273A CN102019211B CN 102019211 B CN102019211 B CN 102019211B CN 200910170273X A CN200910170273X A CN 200910170273XA CN 200910170273 A CN200910170273 A CN 200910170273A CN 102019211 B CN102019211 B CN 102019211B
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Abstract
The invention relates to equipment and a method for degassing a regenerated catalyst, which belongs to the technical field of efficient degassing of the regenerated catalyst which is regenerated by singeing. The technology is characterized in that: the regenerated catalyst from a regenerator is fed into a three-stage degassing bed; a fresh degassing medium is injected into each stage of degassing bed; each stage of degassed gas is separately discharged; and the degassing medium injected into each stage of degassing bed is gradually reduced so as to form different fluidization forms of each stage of catalyst bed layer, so that the regenerated catalyst can effectively contact the fresh degassing medium at each stage, the mass transfer driving force for degassing is improved, and the degassing effect is improved.
Description
Technical field
The invention belongs to through the efficient degassing tank technology of the regenerated catalyst of coke burning regeneration, be specifically related to technologies such as catalytic cracking, methanol conversion system alkene.
Background technology
Regenerated catalyst is carried the regenerator non-hydrocarbon gas inevitably secretly and (is mainly comprised N in cyclic process
2, CO
2, CO, O
2Deng, also claim flue gas), this gas is present in catalyst particles intergranular and the catalyst pores, and the gas of catalyst particles intergranular is prone to remove, and what difficulty removed is the gas in the catalyst pores.For the catalytic cracking equilibrium catalyst,, be 500kg/m in apparent density when its pore volume is 0.24 ~ 0.4ml/g
3The time, gas flow accounts for 15 ~ 25v% of total gas entrainment in the catalyst pores, the catalyst particles intergranular entrainment be 75 ~ 85v%.
Because its oil ratio little (being generally 6-8) is not provided with regenerated catalyst degassing facility, and regenerated catalyst is carried a spot of flue gas secretly and got into reactor, stablizing piece-rate system for follow-up absorption influences less in the conventional catalytic cracking unit.
In the bigger cat-cracker of cracking severity (like DCC, ARGG, CPP etc.); The 2-3 that its catalyst circulation amount is a catalytic cracking unit times, the corresponding increase of the exhaust gas volumn that regenerated catalyst is carried secretly is a lot, especially for CPP technology (technology that processing heavy naphtha is produced ethene, propylene); Its follow-up gas needs through compression, deep cooling, rectifying, and separation process scheme is long, and energy consumption increases; Therefore, degassing facility-degassing tank need be set.Traditional degassing tank of existing commercial Application is simple in structure; Interior is barrier structure; The single hop degassing, its principle is in degassing tank, to feed steam (degassing medium), regenerated catalyst is kept lower bed linear speed in degassing tank; Make catalyst that the long time of staying arranged in degassing tank, the mass velocity through reducing catalyst, the bed density that improves catalyst are to remove the flue gas of carrying secretly between a part of particle.Owing to lack enough diffusion mass transfer motive forces, between most particle and the flue gas carried secretly of granule interior then be difficult to remove.
Therefore, the development and application regenerated catalyst technology that efficiently outgases has crucial meaning for farthest reducing the dry gas non-hydrocarbon impurities.
CN 1226100C discloses a kind of method that makes regenerative agent remove flue gas; Be to make the catalyst after the regeneration get into the regenerator flue gas stripper; Be horizontally disposed with the inner member of the tower disc type more than 4 layers or 4 layers in its stripper; The tower disc type inner member is mainly by the baffle plate more than 2 groups or 2 groups and be arranged on the vertical partition plate of respectively organizing between the baffle plate and form, every group of baffle plate by one group of inclination angle identical and baffle plate sheet that be fixedly connected with vertical partition plate form; Regenerated catalyst and stripping MEDIA FLOW its flow direction separately when each layer inner member all changes.
CN 100351016C discloses a kind of multiple segment steam stripping method for catalyst; Comprise the steps: in the stripper that is provided with two or more catalyst stripping sections; Treat that steam stripped catalyst is transported to the bottom of the stripping section that is positioned at the top; And under the effect of stripping medium flows from bottom to top in this stripping section, remove its adsorbed or carry secretly gas or liquid substance, catalyst flows in the stripping section of to this stripping section top overflow to below; Below stripping section in, repeat above-mentioned stripping step, in catalyst flows into the stripping section of below; In the stripping section below, catalyst from top to down under the effect of stripping medium flows to the bottom of this stripping section, discharges outside the stripper through the catalyst of catalyst line after with stripping then; Material through above-mentioned each stripping section stripping comes out is discharged through gas passage, stripper dilute phase space together with the stripping medium.
US 66562736 B1 disclose the method for a kind of multistage stripping chamber, the steps include: that catalyst granules gets into the first stripping chamber, and catalyst granules continues to flow to the second stripping chamber from top to bottom, and stripping gas gets into dilute phase from the first stripping chamber; The catalyst granules that gets into the second stripping chamber is through with after the stripping medium contacts, and catalyst flows into feed-line from top to bottom and discharges outside the stripper, and the stripping gas of the second stripping chamber directly gets into dilute phase without the first stripping chamber.
In sum, CN 1226100C discloses a kind of tower disc type inner member regenerative agent and has removed the flue gas method, is the degassing of single hop bed, and degassing efficiency is low; Though it is multiple segment steam stripping method for catalyst that CN 100351016C discloses a kind of, the degassing gas of next section mixes with the new degassing medium of introducing of the preceding paragraph mutually, has reduced the degassing (mass transfer) motive force of the preceding paragraph; US 66562736 B1 disclose the method for a kind of multistage stripping chamber, and the degassing gas of next section does not contact with the degassing medium of the preceding paragraph yet, but its each section is introduced degassing medium amount and degassing bed kenel is not done explanation.
Summary of the invention
The object of the present invention is to provide a kind of multistage degassing tank that adopts new structure, the technology of degassing medium with the flue gas that removes regenerated catalyst and carry secretly injected in classification.
A kind of regenerated catalyst degassing tank of one of the present invention is achieved in that
Regenerated catalyst degassing tank of the present invention comprises degassing bed, notes vapour distribution rings, degassing gas outlet, it is characterized in that:
Described degassing tank is 3 grades of degassing beds;
Described notes vapour distribution rings for degassing bed be complementary 3 grades annotate the vapour distribution rings;
Described degassing bed accessory has different mode of fluidizations, and from top to bottom, bed is introduced degassing tolerance and reduced successively;
Described notes vapour distribution rings is connected with stripped vapor alone respectively.
In practical implementation, regenerated catalyst degassing tank of the present invention can have three grades of degas systems,
Have one-level degassing bed 2, one-level to annotate vapour distribution rings 3 in the described degassing tank from top to bottom successively, secondary degassing bed 4, secondary are annotated 5, three grades of degassing beds of vapour distribution rings and are annotated vapour distribution rings 7 for 6, three grades;
Described one-level degassing bed 2, one-level are annotated vapour distribution rings 3, and secondary degassing bed 4, secondary are annotated vapour distribution rings 5 in a cylindrical shell; 6, three grades of three grades of degassing beds are annotated the top loop of cylindrical shell of vapour distribution rings 7 around the middle part of aforementioned cylindrical shell, and to extending below;
There is the degassing of reception one-level on the top of described one-level degassing bed 2 and it is derived the one-level degassing tracheae 10 at degassing tank top;
Described secondary degassing bed 4 is positioned at one-level to be annotated the bottom of vapour distribution rings 3 and accepts the catalyst through 2 degassings of one-level degassing bed, and the one-level cylindrical shell of annotating secondarys degassing bed 4 tops, vapour distribution rings 3 bottom has several secondary gas agent outlet distributing slots 8 and communicates with the top of the three grades of degassing 6 cylindrical shells;
The top of described second, third degassing bed cylindrical shell is provided with two or three grades of degassing gas outlet headers 9 that two or three grades of degassings led to the regenerator dilute phase separately.
The present invention's two the efficient degas method of regenerated catalyst is achieved in that
Regenerated catalyst degas method of the present invention, this method comprises the steps:
Regenerated catalyst from regenerator gets into multistage degassing bed from top to bottom successively; Degassing beds at different levels inject fresh degassing medium respectively; The regenerated catalyst that comes from regenerator is all contacted with fresh degassing medium in every grade, increase degassing mass transfer force, improve degasifying effect.Degassing gas at different levels are derived separately, and the degassing does not exert an influence degassing gas to other grade; In the next stage flow process, the flue gas of carrying secretly reduces step by step at catalyst, and the degassing does not exert an influence to other grade.
The degassing medium that in degassing beds at different levels, injects reduces from top to bottom successively, forms the different mode of fluidization of beds at different levels, and regenerated catalyst is all efficiently contacted with fresh degassing medium at different levels.
In practical implementation,
The amount of described injection degassing media at different levels reduces from top to bottom successively, and forms fast bed, the middling speed bed and low speed bed of gas, agent contact respectively, and the bed apparent density increases successively;
Described regenerated catalyst from regenerator can get into 3 grades of degassing beds from top to bottom successively; Wherein, one-level degassing bed bed linear speed is 0.4m/s, and secondary degassing bed bed linear speed is 0.2m/s, and three grades of degassing bed bed linear speeds are 0.1m/s.
It is one of following that described degassing medium is selected from: 1. low-pressure steam, 2. low-pressure steam and/or nitrogen, 3. low-pressure steam and/or fuel gas.
When the degassing medium that injects when described classification is steam, in each grade, has only a spot of steam with 700-760 ℃ high temperature catalyst contact, to reduce the hydrothermal deactivation of high-temperature regenerated catalyst;
As stated, regenerated catalyst at first gets in the one-level degassing bed, after the one-level stripped vapor contacts; Catalyst flows to secondary degassing bed from top to bottom; Degassing gas is directly drawn separately behind the one-level stripping, injects more stripped vapor in the one-level degassing bed, and the bed inner catalyst is kept the fast bed fluidisation; After getting into the interior catalyst of secondary degassing bed and stripped vapor contacting; Catalyst flows through the annulus from bottom to top; Through flowing to three grades of degassing beds from top to bottom after the overflow of secondary gas agent outlet distributing slot; Secondary degassing bed injects a spot of stripped vapor, and the bed inner catalyst is kept middling speed bed fluidisation; After getting into three grades of catalyst in the degassing bed and stripped vapor contacting; Catalyst flows into the catalyst transport pipeline from top to bottom; Three grades of degassing beds inject a spot of stripped vapor; The bed inner catalyst is kept low speed bed fluidisation, and the degassing gas of secondary, three grades of degassing beds also leads to the regenerator dilute phase separately.
Effect of the present invention is:
1) the classification degassing makes regenerated catalyst flue gas removing efficient improve 30%.
2) gases at different levels are derived separately, do not influence the degassing of other grade.
3) the different gas of formation at different levels-agent contact condition (being fast bed, middling speed bed and low speed bed), in catalyst flowed downward process, density of catalyst increased, and the flue gas of carrying secretly reduces.
4) have only a spot of steam to contact in every grade, reduce the hydrothermal deactivation of catalyst, reduce the device catalyst attrition with high temperature catalyst.
Description of drawings
Below in conjunction with accompanying drawing the present invention is described in further detail:
The efficient degassing tank sketch map of Fig. 1
Among the figure: 1, regenerator; 2, one-level degassing bed; 3, one-level is annotated the vapour distribution rings; 4, secondary degassing bed; 5, secondary is annotated the vapour distribution rings; 6, three grades of degassing beds; 7, annotate the vapour distribution rings for three grades; 8, secondary gas agent outlet distributing slot; 9, two or three grades of degassing gas outlet headers; 10, one-level degassing gas outlet
The specific embodiment
Regenerated catalyst at first gets into one-level degassing bed 2 from regenerator 1; Annotate vapour distribution rings 3 by one-level and inject stripped vapor; Catalyst flows to secondary degassing bed 4 from top to bottom; Degassing gas is directly drawn separately through one-level degassing tracheae 10 behind the one-level stripping; Inject more stripped vapor in the one-level degassing bed 2, the bed inner catalyst is kept the fast bed fluidisation; The catalyst that gets into secondary degassing bed 4 is with after stripped vapor contacts; Catalyst flows through the annulus from bottom to top; By flowing to three grades of degassing beds 6 behind the secondary gas agent outlet distributing slot 8 from top to bottom; Secondary degassing bed 4 is annotated vapour distribution rings 5 by secondary and is injected a spot of stripped vapor, and the bed inner catalyst is kept middling speed bed fluidisation; After getting into three grades of catalyst in the degassing bed 6 and stripped vapor contacting; Catalyst flows into the catalyst transport pipeline from top to bottom; Three grades of degassing beds 6 are annotated vapour distribution rings 7 by three grades and are injected a spot of stripped vapor; The bed inner catalyst is kept low speed bed fluidisation, and the degassing gas of second, third degassing bed leads to the regenerator dilute phase separately by two or three grades of degassing gas outlet headers 9.
Specific embodiment:
Below be the design and running parameter of the efficient degassing tank of certain catalytic cracking unit regenerated catalyst:
| Sequence number | Project | Unit | Numerical value | Remarks |
| 1 | Catalyst temperature | ℃ | 720 | ? |
| 2 | Degassing tank pressure | kPa(g) | 180 | ? |
| 3 | Catalyst flow | t/h | 2920 | ? |
| 4 | The catalyst entrainment flue gas flow | Nm 3/h | 5439.54 | ? |
| 5 | One-level degassing bed diameter | mm | 2400 | ? |
| 6 | One-level degassing bed injects quantity of steam | Nm 3/h | 3239.2 | ? |
| 7 | One-level degassing bed bed linear speed | m/s | 0.4 | ? |
| 8 | One-level degassing bed averag density/height of bed | (kg/m 3)/m | 550/4 | ? |
| 9 | The one-level degassing bed time of staying | s | 12 | ? |
| 10 | One-level degassing bed degassing efficiency | ％ | 61.41 | ? |
| 11 | Secondary degassing bed diameter | mm | 2200 | ? |
| 12 | Secondary degassing bed injects quantity of steam | Nm 3/h | 2143.5 | ? |
| 13 | Secondary degassing bed bed linear speed | m/s | 0.2 | ? |
| 14 | Secondary degassing bed averag density/height of bed | (kg/m 3)/m | 600/3 | ? |
| 15 | The secondary degassing bed time of staying | s | 7 | ? |
| 16 | Secondary degassing bed degassing efficiency | ％ | 38.26 | ? |
| 17 | Three grades of degassing bed diameters | mm | 2800 | ? |
| 18 | Three grades of degassing beds inject quantity of steam | Nm 3/h | 1785.48 | ? |
| 19 | Three grades of degassing bed bed linear speeds | m/s | 0.1 | ? |
| 20 | One-level degassing bed averag density/height of bed | (kg/m 3)/m | 600/3 | ? |
| 21 | Three grades of degassing bed time of staying | s | 10 | ? |
| 22 | Three grades of degassing bed degassing efficiencies | ％ | 40.36 | ? |
| 23 | Total degassing efficiency | ％ | 85.79 | ? |
Annotate: degassing efficiency (η)=(import catalyst flue gas flow-outlet catalyst flue gas flow)/import catalyst flue gas flow.
Claims (9)
1. a regenerated catalyst degassing tank comprises degassing bed, notes vapour distribution rings, degassing gas outlet, it is characterized in that:
Described degassing tank is 3 grades of degassing beds;
Described notes vapour distribution rings is 3 grades of notes vapour distribution rings that are complementary with degassing bed;
Described degassing bed accessory has different mode of fluidizations, and from top to bottom, bed is introduced degassing tolerance and reduced successively;
Described notes vapour distribution rings is connected with the stripped vapor house steward alone respectively.
2. regenerated catalyst degassing tank as claimed in claim 1 is characterized in that:
Have one-level degassing bed (2), one-level to annotate vapour distribution rings (3) in the described degassing tank from top to bottom successively, secondary outgases bed (4), secondary is annotated vapour distribution rings (5), three grades of degassing beds (6), three grades of notes vapour distribution rings (7);
Described one-level degassing bed (2), one-level are annotated vapour distribution rings (3), and secondary degassing bed (4), secondary are annotated vapour distribution rings (5) in a cylindrical shell; Three grades of degassing beds (6), three grades are annotated the top loop of cylindrical shell of vapour distribution rings (7) around the middle part of aforementioned cylindrical shell, and to extending below.
3. regenerated catalyst degassing tank as claimed in claim 2 is characterized in that:
There is the degassing of reception one-level on the top of described one-level degassing bed (2) and it is derived the one-level degassing tracheae (10) at degassing tank top;
Described secondary degassing bed (4) is positioned at one-level to be annotated the bottom of vapour distribution rings (3) and accepts the catalyst through one-level degassing bed (2) degassing, and the one-level cylindrical shell of annotating secondary degassing bed (4) top, vapour distribution rings (3) bottom has several secondary gas agent outlet distributing slots (8) and communicates with the top of the three grades of degassing (6) cylindrical shells;
The top of described second, third degassing bed cylindrical shell is provided with two or three grades of degassing gas outlet headers (9) that two or three grades of degassings led to the regenerator dilute phase separately.
4. like the described regenerated catalyst degas method of one of claim 1～3, this method comprises the steps:
Regenerated catalyst from regenerator gets into multistage degassing bed from top to bottom successively, and degassing beds at different levels inject fresh degassing medium respectively, and degassing gas at different levels are derived separately, and the degassing does not exert an influence degassing gas to other grade; In the next stage flow process, the flue gas of carrying secretly reduces step by step at catalyst;
The degassing medium that in degassing beds at different levels, injects reduces from top to bottom successively, forms the different mode of fluidization of beds at different levels, and regenerated catalyst is all efficiently contacted with fresh degassing medium at different levels.
5. regenerated catalyst degas method as claimed in claim 4 is characterized in that:
The amount of described injection degassing media at different levels reduces from top to bottom successively, and forms fast bed, the middling speed bed and low speed bed of gas, agent contact respectively, and the bed apparent density increases successively.
6. regenerated catalyst degas method as claimed in claim 4 is characterized in that:
It is one of following that described degassing medium is selected from: 1. low-pressure steam, 2. low-pressure steam and/or nitrogen, 3. low-pressure steam and/or fuel gas.
7. regenerated catalyst degas method as claimed in claim 6 is characterized in that:
When the degassing medium that injects when described classification is steam, in each grade, has only a spot of steam with 700-760 ℃ high temperature catalyst contact, to reduce the hydrothermal deactivation of high-temperature regenerated catalyst.
8. regenerated catalyst degas method as claimed in claim 5 is characterized in that:
Described regenerated catalyst from regenerator gets into 3 grades of degassing beds from top to bottom successively; Wherein, one-level degassing bed bed linear speed is 0.4m/s, and secondary degassing bed bed linear speed is 0.2m/s, and three grades of degassing bed bed linear speeds are 0.1m/s.
9. regenerated catalyst degas method as claimed in claim 8 is characterized in that:
Described regenerated catalyst from regenerator gets into 3 grades of degassing beds from top to bottom successively; Wherein:
One-level degassing bed diameter is 2400mm;
It is 3239.2Nm that one-level degassing bed injects quantity of steam
3/ h;
One-level degassing bed bed linear speed is 0.4m/s;
One-level degassing bed averag density is 550 (kg/m
3), height of bed 4m;
The one-level degassing bed time of staying is 12s;
Secondary degassing bed diameter is 2200mm;
It is 2143.5Nm that secondary degassing bed injects quantity of steam
3/ h;
Secondary degassing bed bed linear speed is 0.2m/s;
Secondary degassing bed averag density is 600 (kg/m
3), height of bed 3m;
The secondary degassing bed time of staying is 7s;
Three grades of degassing bed diameters are 2800mm;
It is 1785.48Nm that three grades of degassing beds inject quantity of steam
3/ h;
Three grades of degassing bed bed linear speeds are 0.1m/s;
Three grades of degassing bed averag densities are 600 (kg/m
3), height of bed 3m;
Three grades of degassing bed time of staying are 10s.
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| CN200910170273XA CN102019211B (en) | 2009-09-10 | 2009-09-10 | Equipment and method for degassing regenerated catalyst |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200910170273XA CN102019211B (en) | 2009-09-10 | 2009-09-10 | Equipment and method for degassing regenerated catalyst |
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| CN102019211B true CN102019211B (en) | 2012-07-25 |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6652736B1 (en) * | 1998-07-02 | 2003-11-25 | Total Raffinage Distribution S.A. | Stripping method for extracting solid fluidized particles and implementing device |
| CN1485138A (en) * | 2002-09-28 | 2004-03-31 | 中国石油化工股份有限公司 | Method of eliminating fume for regenerated catalyst |
| CN1754626A (en) * | 2004-09-28 | 2006-04-05 | 中国石油化工股份有限公司 | Flue gas stripping device |
| CN1762566A (en) * | 2004-10-22 | 2006-04-26 | 中国石油化工股份有限公司 | Regenerated catalyst steam-stripping method |
| CN101391234A (en) * | 2008-10-30 | 2009-03-25 | 石宝珍 | Catalyst multistage regeneration method and device |
-
2009
- 2009-09-10 CN CN200910170273XA patent/CN102019211B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6652736B1 (en) * | 1998-07-02 | 2003-11-25 | Total Raffinage Distribution S.A. | Stripping method for extracting solid fluidized particles and implementing device |
| CN1485138A (en) * | 2002-09-28 | 2004-03-31 | 中国石油化工股份有限公司 | Method of eliminating fume for regenerated catalyst |
| CN1754626A (en) * | 2004-09-28 | 2006-04-05 | 中国石油化工股份有限公司 | Flue gas stripping device |
| CN1762566A (en) * | 2004-10-22 | 2006-04-26 | 中国石油化工股份有限公司 | Regenerated catalyst steam-stripping method |
| CN101391234A (en) * | 2008-10-30 | 2009-03-25 | 石宝珍 | Catalyst multistage regeneration method and device |
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Address after: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Co-patentee after: Sinopec Engineering Incorporation Patentee after: China Petrochemical Group Corp. Address before: 100728 Beijing, Chaoyangmen, North Street, No. 22, No. Co-patentee before: Engrg Construction Co., SINOPEC Patentee before: China Petrochemical Group Corp. |
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Address after: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee after: SINOPEC Group Patentee after: Sinopec Engineering Construction Co., Ltd Address before: 100728 No. 22 North Main Street, Chaoyang District, Beijing, Chaoyangmen Patentee before: CHINA PETROLEUM & CHEMICAL Corp. Patentee before: Sinopec Engineering Construction Co., Ltd |