CN1311060A - Regenerated catalyst stripping tower and method for stripping regenerated catalyst - Google Patents
Regenerated catalyst stripping tower and method for stripping regenerated catalyst Download PDFInfo
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- CN1311060A CN1311060A CN 00103385 CN00103385A CN1311060A CN 1311060 A CN1311060 A CN 1311060A CN 00103385 CN00103385 CN 00103385 CN 00103385 A CN00103385 A CN 00103385A CN 1311060 A CN1311060 A CN 1311060A
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- stripper
- regenerated catalyst
- catalyst
- baffle plate
- steam
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Abstract
A stripper for regenerating catalyst and its method for regenerating the catalyst by gas stripping are characterized by that: a cylindrcal stripper for regenerating catalyst mainly contains degassing tubes on the longitudinal axis and horizontal tubes connected with the terminal ends of degassing tubes, and along the vertical direction, staggered arranged inner and outer annular bafflex; the catalyst to be regenerated enters the stripper from its upper portion to contact the steam from the annular steam tube with reverse and staggering flows, and the regenerated catalyst after deprived of smoke and gas leaves the stripper from its bottom; and the deprived-off smoke and gas and the excessive steam are discharged from the stripper top via the degassing tubes.
Description
The invention belongs to equipment and the method for isolating gas from solid, more particularly, is a kind of equipment and method of isolating flue gas from the regenerated catalyst of petroleum hydrocarbon catalytic conversion process.
Catalytic pyrolysis is to be that raw material production is the method for main purpose product with light olefins such as ethene, propylene with the heavy petroleum hydrocarbon.The main process of this method is: the heavy crude hydrocarbon feed is in riser or downstriker pipeline reactor, in the presence of high-temperature vapour, contact with solid acid catalyst, weight ratio (hereinafter to be referred as oil ratio) at 650～750 ℃ of reaction temperatures, reaction pressure 0.15～0.4MPa, 0.2～5 second reaction time, catalyst and feedstock oil is 15～40: 1, the weight ratio of steam and feedstock oil is under 0.3～1: 1 the condition, carries out the catalytic pyrolysis reaction.Product, steam and reclaimable catalyst are after quick gas solid separation, and reaction product isolated obtains main purpose product ethene, propylene; Reclaimable catalyst enters regenerator behind the steam stripping, contact with oxygen-containing gas to carry out coke burning regeneration, and the regenerated catalyst Returning reactor of heat recycles.
Owing in the catalyst granules a large amount of holes is arranged, retain in the regenerated catalyst hole and on the outer surface flue gas is arranged, although the exhaust gas volumn of retaining in each hole on the catalyst is very little, but because the oil ratio that adopts is very big, the catalyst circulation amount is a lot, has the flue gas of suitable volume to be reproduced catalyst and brings reactor into.For a cover year treating capacity is 1,000,000 tons catalytic pyrolysis device, and by recycle ratio 0.4, oil ratio 20, the internal circulating load of catalyst is 3500 tons/hour, and the exhaust gas volumn of taking reactor to is about 3500 meters
3/ hour, account for more than 10% of reaction dry gas amount.Contain N in the flue gas
2, O
2, CO
2, CO, NO
x, SO
xDeng gas, if directly the regenerated catalyst fluidisation is transported to reactor, then flue gas is reproduced catalyst entrainment and enters reactor and become foreign gas, and this not only increases the gas compressor load, and hinders normally carrying out of follow-up cryogenic separation process.Therefore, regenerated catalyst being removed the processing of flue gas, is the problem that catalytic pyrolysis must solve.For other catalysis conversion method, when oil ratio is big, all exist more flue gas to enter the problem of reactor.
USP4,051,013 adopts the regenerated catalyst stripper, and in the mode of stripping medium (being generally steam) with the regenerated catalyst counter current contacting, regenerated flue gas and intergranular regenerated flue gas that catalyst is adsorbed strip.The stripping medium is introduced stripper at the bottom of the tower, and baffle plate is arranged in the stripper, but the concrete shape and the structure of undeclared baffle plate in this patent.Because this patent does not consider that steam can cause the problem of high-temperature regenerated catalyst hydrothermal deactivation, in fact can't use.
CN1154400A proposes: adopt the temperature adjustment degassing tank that regenerated catalyst is handled, fluidisation, stripping medium are catalysis drying gas.Because its main purpose is in order to change the temperature that catalyst enters reactor, so the member in the temperature adjustment degassing tank is vertical heat removing tube.Growing up of the uncontrollable bubble of this kind structure causes gas-solid contact variation, and steam stripping efficiency is not high.And the competitive Adsorption of dry gas is indifferent, and displacement efficiency is not high enough, when regenerated catalyst contains exhaust gas volumn after reaching identical stripping, the dry gas amount that consumes is more, and in use dry gas and regenerated flue gas mix, and is diluted, can't further utilize, benefit is good inadequately.
In the catalytic pyrolysis process, catalyst after the regeneration is 700～750 ℃, if can cause the catalyst deactivation with the steam Long contact time, so USP4,051,013 regenerated catalyst steam-stripping method that proposes is not suitable for the flue gas removing of catalytic pyrolysis regenerated catalyst and handles, and also there is weak point in the method and apparatus structure that CN1154400A proposes.
One of purpose of the present invention provides a kind of regenerated catalyst stripper.
Two of purpose of the present invention provides a kind of method of regenerated catalyst stripping flue gas.
Regenerated catalyst stripper architectural feature provided by the invention is:
The regenerated catalyst stripper is a upright cylinder, comprise in the tube: (1), be positioned at the deaeration pipe on the longitudinal axis, (2), the horizontal tube that links to each other with the deaeration pipe lower end, (3), be fixed on interior ring baffle plate on the deaeration pipe, (4), be fixed on the outer shroud baffle plate of the inner surface of cylinder, (5), annular steam pipe in the following side space of outer shroud baffle plate, that have some apertures, (6), the steam inlet tube that links to each other with annular steam pipe, (7), the gas vent on top, the catalyst tangential inlet on (8), top.
The height of described cylinder and its diameter ratio are 5～20: 1.The equal diameters of deaeration pipe and horizontal tube is 2～20% of cylinder cross section diameter of a circle.The deaeration pipe upper end links to each other with the tower inner surface by the metal lacing wire, play supporting role.
Interior ring baffle plate and outer shroud baffle plate vertically keep at a certain distance away and are staggered.
Interior ring baffle plate is made up of the inclined-plane on top and the skirt cover of bottom, not perforate on inclined-plane and the skirt cover, and the front view on inclined-plane is trapezoidal, and vertical view is an annulus, and the external diameter of annulus is that the diameter ratio of cylinder is 0.4～0.7: 1; The front view of skirt cover is a rectangle, and vertical view is circle, and this diameter of a circle equates with the external diameter of annulus.Described deaeration pipe part below interior ring baffle plate is mushy earthenware, has some apertures and cover the common metal pipe of woven wire or the pipe that woven wire is rolled into.Interior ring baffle plate links to each other with the tower inner surface by the metal lacing wire, play supporting role.
The outer shroud baffle plate is made up of the inclined-plane on top and the skirt cover of bottom, all has some apertures on inclined-plane and the skirt cover, and percent opening is 1～5%.The front view on inclined-plane is trapezoidal, and vertical view is an annulus, and the external diameter of annulus is that the diameter ratio of cylinder is 0.4～0.7: 1; The front view of skirt cover is a rectangle, and vertical view is circle, and this diameter of a circle equates with the external diameter of annulus.
The catalyst inlet on top is tangentially, and it is perpendicular that promptly catalyst is gone into arbitrary diameter of tower route and cylinder cross circular section.This catalyst inlet plays the effect of similar thick cyclone inlet.
The stripper bottom is a catalyst outlet, and this outlet links to each other with the catalyst transport pipeline by changeover portion.
Structure below in conjunction with description of drawings regenerated catalyst stripper.
Accompanying drawing is the structural representation of regenerated catalyst stripper.
The structure of regenerated catalyst stripper is: the regenerated catalyst stripper is a upright cylinder, Establish a upright deaeration pipe 1 at the longitudinal axis of cylinder, in lower end and level of this deaeration pipe Pipe 2 links to each other, and vertically is provided with some steam inlet tubes 3 at the outer surface of degassing tower. Justifying Interior ring baffle plate 4 and the outer shroud baffle plate 5 of being crisscross arranged that vertically keep at a certain distance away in the tube, wherein in The ring baffle plate is fixed on the deaeration pipe 1, and interior ring baffle plate is divided into inclined-plane 4a and skirt cover 4b, and deaeration pipe 1 exists Interior ring baffle plate below part is mushy earthenware, has the general of some apertures and covering metal silk screen The pipe that logical metal tube or woven wire are rolled into; The outer shroud baffle plate is fixed on the inner surface of cylinder, at outer shroud Space 5c between the inclined-plane 5a of baffle plate and the skirt cover 5b is provided with annular steam pipe 6, this steam Have some apertures around the pipe, link to each other with steam inlet tube 3. The upper end of stripper and flue gas pipeline 7 connect, and are connected with catalyst tangential inlet pipe 8 on the top of stripper, and regenerated catalyst is from stripper The lower tower that brings out.
The method of regenerated catalyst stripping provided by the invention is:
Regenerated catalyst enters in the tower from the stripper upper tangential, and steam enters annular water through inlet tube Steam pipe passes the aperture on the outer shroud baffle plate, carries out adverse current with catalyst, cross-flow contacts, steam The rapid flue gas that carries of displacement regenerated catalyst, the regenerated catalyst that removes behind the flue gas goes out tower at the bottom of tower, The flue gas of deviating from and excessive water steam enter deaeration pipe, bring out tower from cat head.
The flow velocity that regenerated catalyst tangentially enters in the stripper is 10～18 meter per seconds, and the catalyst in the stripper is close phase state and flows, and mass flowrate is 20～200 kilogram-meters-2Second-1, the catalyst in the stripper Flow velocity is 0.05～0.3 meter per second.
Described catalytic conversion process can be the bigger catalytic pyrolysis of oil ratio or catalytic pyrolysis, also Can be conventional catalytic cracking or other improved catalytic conversion process.
Specifically describe below method provided by the invention and operation principle: a large amount of from containing of regenerator The regenerated catalyst of flue gas enters in the tower from the stripper upper tangential. Since the effect of centrifugal force, catalysis Agent is tending towards flowing to the tower inner surface, and gas is tending towards flowing to the tower center, thereby flue gas and catalyst are advanced The row crude separation. Catalyst enters behind the stripper because Action of Gravity Field flows downward, and interior ring baffle plate makes catalysis Agent outwards flows to the outer shroud baffle plate, and the outer shroud baffle plate makes again catalyst turn to ring baffle plate in the inside flow direction, is positioned at A series of outer shroud baffle plates of differing heights, interior ring baffle plate make catalyst tortuous mobile, avoid occurring bigger Vertical catalyst stream circulation passage actual internal area, free. Steam enters annular by inlet tube The steam pipe, from the aperture ejection of annular steam pipe, the steam of ejection passes the outer shroud baffle plate then Aperture on inclined-plane and the skirt cover carries out adverse current with the catalyst that flows downward, cross-flow contacts, and displaces Between the catalyst granules and the intrapore flue gas of particle. Most of steam directly flows to from the outer shroud baffle plate The lower space of interior ring baffle plate, owing to do not have aperture on interior ring baffle plate inclined-plane and the skirt cover, so this part Steam collects in interior ring baffle plate below. Because empty in stripper inner catalyst dense-phase bed and the deaeration pipe Between between have a differential pressure pressure field, the deaeration pipe Pressure Field is lower than stripper inner catalyst dense bed The pressure field of layer any point, thus the gas in the stripper when upwards flowing to the stripper center Draw close, most of gas will collect in interior ring baffle plate below, from interior ring baffle plate below by on the deaeration pipe The hole enter deaeration pipe, go out tower from the exhanst gas outlet pipeline. Introducing water from the horizontal tube of deaeration pipe lower end steams Gas or air, its flow velocity should guarantee to enter above-mentioned earthenware, covering metal silk screen the common metal pipe or The catalyst fines of metallic mesh tube can be blowed to degassing tower top bed layered material face, with avoid into The fine powder that enters gathers the obstruction deaeration pipe.
Advantage of the present invention is as follows:
1, adopts stripper provided by the invention and degas method, can effectively remove regenerated catalyst In flue gas.
2, because most of steam encircles baffle plate in directly flowing to from the outer shroud baffle plate, then from interior ring gear Plate below enters deaeration pipe, steam in stripper with time of contact of high-temperature regenerated catalyst very Short, thus the hydrothermal deactivation of regenerated catalyst avoided.
3, owing to removed the gas in the catalyst, increase the density of catalyst, improved catalyst The motive force of circulation.
The following examples will give further instruction to method provided by the invention, but not thereby limiting the invention.
Embodiment
Testing used medium-sized stripper internal diameter is 150 millimeters, and height overall is 3.0 meters, and the internal diameter of stripper tangential inlet pipeline is 75 millimeters, 30 millimeters of deaeration pipe internal diameters in the stripper are established three groups of inner and outer rings baffle plates in the stripper, 300 millimeters of baffle spacings, the perforate of outer shroud baffle plate, its percent opening are 5%.Regenerator beds fluidizing agent is an air, and empty bed linear gas velocity is 0.6 meter per second; The stripping medium of stripper is a nitrogen, and the void tower linear gas velocity that stripping medium total amount is amounted to into stripper is 0.2 meter per second.Catalyst quality flow rate in the stripper is about 90 kilogram-meters
-2Second
-1The gas that stripper porch catalyst carries is air, oxygen concentration wherein is 21%, because the purging metathesis of nitrogen, the oxygen concentration in the stripper descends gradually, determines the relative degassing efficiency of stripper according to the oxygen concentration in the stripper lower part outlet place gas.The result shows: in above-mentioned test range, stripper outlet oxygen concentration has reduced 80%, and the relative degassing efficiency that also is stripper is 80%.
Adopt the method for hydrogen spike to record: the stripping medium more than 80% enters deaeration pipe, upwards flows and leaves bed fast, and its mean residence time was less than 5 seconds.All the other flow downward with catalyst less than 20% stripping medium, leave stripper.
Claims (14)
1, a kind of regenerated catalyst stripper, it is characterized in that this tower is a upright cylinder, comprise: (1), be positioned at the deaeration pipe on the longitudinal axis, (2), the horizontal tube that links to each other with the deaeration pipe lower end, (3), be fixed on interior ring baffle plate on the deaeration pipe, (4), be fixed on the outer shroud baffle plate of the inner surface of cylinder, (5), annular steam pipe in the following side space of outer shroud baffle plate, that have some apertures, (6), the steam inlet tube that links to each other with annular steam pipe, (7), the gas vent on top, the catalyst tangential inlet on (8), top.
2,, it is characterized in that the height of described cylinder and its diameter ratio are 5～20: 1 according to the stripper of claim 1.
3, according to the stripper of claim 1, it is characterized in that the equal diameters of described deaeration pipe diameter and horizontal tube, be 2～20% of drum diameter.
4, according to the stripper of claim 1, it is characterized in that described in the ring baffle plate form by the inclined-plane on top and the skirt cover of bottom, the front view on inclined-plane is trapezoidal, vertical view is an annulus, the external diameter of annulus and the diameter ratio of cylinder are 0.4～0.7: 1; The front view of skirt cover is a rectangle, and vertical view is circle, and this diameter of a circle equates with the external diameter of annulus.
5,, it is characterized in that described deaeration pipe part below interior ring baffle plate is mushy earthenware, has some apertures and cover the common metal pipe of woven wire or the pipe that woven wire is rolled into according to the stripper of claim 1.
6, according to the stripper of claim 1, it is characterized in that described outer shroud baffle plate is made up of the inclined-plane on top and the skirt cover of bottom, all have some apertures on inclined-plane and the skirt cover, the front view on inclined-plane is trapezoidal, vertical view is an annulus, and the external diameter of annulus and the diameter ratio of cylinder are 0.4～0.7: 1; The front view of skirt cover is a rectangle, and vertical view is circle, and this diameter of a circle equates with the external diameter of annulus.
7, according to the stripper of claim 1, it is characterized in that described in ring baffle plate and outer shroud baffle plate vertically keep at a certain distance away and be staggered.
8, according to the stripper of claim 1, it is characterized in that the stripper bottom is the regenerated catalyst outlet, this outlet links to each other with the catalyst transport pipeline by changeover portion.
9, a kind of method of regenerated catalyst stripping, it is characterized in that regenerated catalyst enters in the tower from the stripper upper tangential, steam enters annular steam pipe through inlet tube, pass the aperture on the outer shroud baffle plate, carry out adverse current with regenerated catalyst, cross-flow contacts, steam is replaced the flue gas that regenerated catalyst carries rapidly, the regenerated catalyst that removes behind the flue gas goes out tower at the bottom of tower, flue gas of deviating from and excessive water steam enter deaeration pipe, under effect, bring out tower from cat head from the steam of horizontal tube or air.
10,, it is characterized in that described regenerated catalyst is from catalytic conversion process according to the method for claim 9.
11, according to the method for claim 10, it is characterized in that described catalytic conversion process can be a catalytic pyrolysis, also can be catalytic pyrolysis.
12,, it is characterized in that the flow velocity that regenerated catalyst tangentially enters in the stripper is 10～18 meter per seconds according to the method for claim 9.
13,, it is characterized in that the time of staying of excessive steam in stripper was less than 10 seconds according to the method for claim 9.
14,, it is characterized in that the regenerated catalyst flow velocity is 0.05～0.3 meter per second in the stripper according to the method for claim 9.
Priority Applications (10)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001033859A CN1156340C (en) | 2000-03-03 | 2000-03-03 | Regenerated catalyst stripping tower and method for stripping regenerated catalyst |
| JP2001563200A JP4326742B2 (en) | 2000-03-03 | 2001-02-26 | Stripper and stripping method for removing flue gas carried by regenerated catalyst |
| AU2001237204A AU2001237204A1 (en) | 2000-03-03 | 2001-02-26 | The stripping column and method for stripping smoke entrapped by regenerative catalyst |
| PCT/CN2001/000145 WO2001064307A1 (en) | 2000-03-03 | 2001-02-26 | The stripping column and method for stripping smoke entrapped by regenerative catalyst |
| CA002400500A CA2400500C (en) | 2000-03-03 | 2001-02-26 | A stripper and a stripping process for removing the flue gas carried by regenerated catalyst |
| US09/795,496 US6723292B2 (en) | 2000-03-03 | 2001-03-01 | Stripper and a stripping process for removing the flue gas carried by regenerated catalyst |
| MYPI20010947A MY128827A (en) | 2000-03-03 | 2001-03-01 | A stripper and a stripping process for removing the flue gas carried by regenerated catalyst |
| NO20024057A NO330759B1 (en) | 2000-03-03 | 2002-08-26 | A stripper and stripping process for removing exhaust gases are contained in a regenerated catalyst |
| FI20021549A FI121989B (en) | 2000-03-03 | 2002-08-30 | Stripper and stripping procedure for the removal of flue gas transported by regenerated catalytic converter |
| US10/767,361 US6939823B2 (en) | 2000-03-03 | 2004-01-29 | Stripper and a stripping process for removing the flue gas carried by regenerated catalyst |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB001033859A CN1156340C (en) | 2000-03-03 | 2000-03-03 | Regenerated catalyst stripping tower and method for stripping regenerated catalyst |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1311060A true CN1311060A (en) | 2001-09-05 |
| CN1156340C CN1156340C (en) | 2004-07-07 |
Family
ID=4576944
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB001033859A Expired - Lifetime CN1156340C (en) | 2000-03-03 | 2000-03-03 | Regenerated catalyst stripping tower and method for stripping regenerated catalyst |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1156340C (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101605597B (en) * | 2006-12-21 | 2013-06-19 | 环球油品有限责任公司 | Screenless moving bed reactor |
| CN104128016A (en) * | 2014-07-02 | 2014-11-05 | 洛阳智达石化工程有限公司 | Coaxial type sedimentation regenerator |
| CN104946305A (en) * | 2014-10-09 | 2015-09-30 | 石宝珍 | Catalytic cracking reaction method |
| CN112156761A (en) * | 2020-04-09 | 2021-01-01 | 北京中航泰达环保科技股份有限公司 | Novel active carbon regeneration device |
| CN113769429A (en) * | 2021-10-14 | 2021-12-10 | 华峰集团上海工程有限公司 | Solvent recovery and deashing device and process for PPC slurry |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104212475B (en) * | 2014-08-27 | 2016-01-13 | 洛阳智达石化工程有限公司 | A kind of stripping component seal coupling device |
-
2000
- 2000-03-03 CN CNB001033859A patent/CN1156340C/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101605597B (en) * | 2006-12-21 | 2013-06-19 | 环球油品有限责任公司 | Screenless moving bed reactor |
| CN104128016A (en) * | 2014-07-02 | 2014-11-05 | 洛阳智达石化工程有限公司 | Coaxial type sedimentation regenerator |
| CN104128016B (en) * | 2014-07-02 | 2015-10-21 | 洛阳智达石化工程有限公司 | Coaxial type sedimentation-regenerator |
| CN104946305A (en) * | 2014-10-09 | 2015-09-30 | 石宝珍 | Catalytic cracking reaction method |
| CN112156761A (en) * | 2020-04-09 | 2021-01-01 | 北京中航泰达环保科技股份有限公司 | Novel active carbon regeneration device |
| CN113769429A (en) * | 2021-10-14 | 2021-12-10 | 华峰集团上海工程有限公司 | Solvent recovery and deashing device and process for PPC slurry |
Also Published As
| Publication number | Publication date |
|---|---|
| CN1156340C (en) | 2004-07-07 |
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Applicant after: China Petrochemical Group Corp. Co-applicant after: Sinopec Research Institute of Petroleum Processing Applicant before: China Petrochemical Group Corp. Co-applicant before: Chinese petrochemical industry Research Institute of Petro-Chemical Engineering of group company |
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Granted publication date: 20040707 |