CN1762567A - A regenerated catalyst flue gas stripper - Google Patents
A regenerated catalyst flue gas stripper Download PDFInfo
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- CN1762567A CN1762567A CN 200410083890 CN200410083890A CN1762567A CN 1762567 A CN1762567 A CN 1762567A CN 200410083890 CN200410083890 CN 200410083890 CN 200410083890 A CN200410083890 A CN 200410083890A CN 1762567 A CN1762567 A CN 1762567A
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- flue gas
- stripping
- inner sleeve
- stripper
- heat
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- 239000003054 catalyst Substances 0.000 title claims abstract description 75
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 title claims description 54
- 239000003546 flue gas Substances 0.000 title claims description 54
- 230000008676 import Effects 0.000 claims description 3
- 238000001816 cooling Methods 0.000 abstract description 3
- 238000000926 separation method Methods 0.000 abstract 2
- 238000012546 transfer Methods 0.000 description 19
- 239000007789 gas Substances 0.000 description 12
- 238000000034 method Methods 0.000 description 9
- 238000004523 catalytic cracking Methods 0.000 description 7
- 230000008569 process Effects 0.000 description 7
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 7
- 239000003795 chemical substances by application Substances 0.000 description 6
- 230000001172 regenerating effect Effects 0.000 description 5
- 238000011069 regeneration method Methods 0.000 description 5
- 230000008859 change Effects 0.000 description 3
- 238000005336 cracking Methods 0.000 description 3
- 238000007872 degassing Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 238000005243 fluidization Methods 0.000 description 3
- 239000007788 liquid Substances 0.000 description 3
- 239000012492 regenerant Substances 0.000 description 3
- 230000009286 beneficial effect Effects 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 229910052571 earthenware Inorganic materials 0.000 description 2
- 230000008929 regeneration Effects 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 101000643890 Homo sapiens Ubiquitin carboxyl-terminal hydrolase 5 Proteins 0.000 description 1
- 102100021017 Ubiquitin carboxyl-terminal hydrolase 5 Human genes 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000000571 coke Substances 0.000 description 1
- 230000002860 competitive effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 238000012938 design process Methods 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000006073 displacement reaction Methods 0.000 description 1
- 235000012489 doughnuts Nutrition 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 239000003517 fume Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 230000036961 partial effect Effects 0.000 description 1
- 238000011056 performance test Methods 0.000 description 1
- 239000003209 petroleum derivative Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
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Abstract
he regenerated catalyst gas stripper comprises: arranging regenerated catalyst lead-in tube (1) and stripping medium lead-off tube (7) on top of the stripper and regenerated inclined tube (5) on bottom of the stripper; fixing and connecting the bottom separation plate (9) with medium distributor (4) on top and stripper cylinder and catalyst outlet pipe (10); arranging the inner sleeve (6b) on top of distributor (4) with the top end of inner sleeve (6a) in inner sleeve (6b) lower than inner sleeve (6b) and the bottom end passing distributor (4) and separation plate (9) to form outlet pipe (10); arranging stripping medium distributor (3) in catalyst outlet pipe (10 under the heat tube (8) with lead-in and lead-out ends for heat medium outside the stripper and other part in stripper. This product has dual-function both for stripping and cooling.
Description
Technical field
The invention belongs to the petroleum hydrocarbon catalyticing conversioning equipment, more particularly, is a kind of stripper that removes flue gas that regenerated catalyst is carried secretly.
Background technology
In catalytic cracking unit,, have partial fume and be reproduced catalyst and be carried in the riser reactor along with circulating of catalyst.According to the literature, this part flue gas accounts for 1～3% of catalyst circulation amount.This part flue gas is behind riser, settler, follow dry gas to enter rich gas compressor at last, the load of rich gas compressor is increased, influence the disposal ability and the energy consumption of device, so should before regenerated catalyst enters riser reactor, this part flue gas be removed.
In refinery catalytic cracking unit (FCC), especially in RFCC (RFCC), in recent years along with intermingled dregs ratio constantly increases, feedstock oil is more and more heavier, the burnt amount of liter in cracking reaction also constantly increases, and these coke burnings can produce a large amount of heats in regenerator.Because the catalytic cracking reaction-regeneration system is the thermal balance operation, the heat that i.e. regeneration produces will compensate the heat that the raw material cracking reaction is absorbed, if regenerative process produces superfluous heat, to destroy reaction-regeneration system thermal balance, therefore must take measures to take away a part of heat, to guarantee steadily carrying out of technological operation.It is exactly a kind of general way that external warmer is set, and it not only can take the superfluous heat in the device away, and can utilize this part heat, produces steam, thereby becomes important energy saving measure of device.External warmer is operated nimblely because the heat-obtaining amount is big, and commercial Application is very extensive.
Propose among the CN1154400A to adopt the temperature adjustment degassing tank that regenerated catalyst is handled, the used stripping medium of temperature adjustment degassing tank is a 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, thereby can cause gas-solid contact variation, steam stripping efficiency is not high, and the competitive Adsorption of dry gas is indifferent, and displacement efficiency is not high enough, 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 dry gas is diluted, can't further utilize, economic benefit is good inadequately.
CN1311060A has proposed a kind of baffle-type regenerated catalyst flue gas stripping structure that has the center deaeration pipe, this structure centre is provided with a deaeration pipe, can make the part the flue gas of desorption from deaeration pipe, discharge in advance, perforate on baffle plate simultaneously, make water vapour and catalyst form adverse current and contact, to improve its mass-transfer efficiency with cross-flow.But this structure also exists the operating flexibility difference and the problem of inconvenience is installed.The center deaeration pipe enters in order to prevent catalyst, and the general ceramic dielectric with microcellular structure that adopts will reach certain capacity, and earthenware not only will account for very big volume, and needs frequent blowback, operation and control more complicated.In device installation and operation process, earthenware easily breaks in addition, must adopt other enhancements.
CN2455355Y has proposed a kind of gas-solid loop flow regenerated catalyst steam-stripping device of flue gas.This structure is taked certain method to make to have the apparent linear speed of different fluidisations in the inner and outer ring, and fluid bed has different density between inner and outer ring thereby make, and the circulation that has produced thus between the catalyst inner and outer ring flows.Realized repeatedly contacting of catalyst and fresh stripped vapor by circulation, can obtain higher steam stripping efficiency, and this type stripper structure is also fairly simple, size is compact.
USP 5,260, disclosed a kind of stripper structure in 034 with a plurality of annulus, in this type stripper, the ring baffle of a plurality of different radiis is divided into a plurality of annular chamber that volume does not wait with stripper, and its volume reduces from inside to outside successively, at a plurality of stripping distributors of stripper lower disposed, make catalyst from inside to outside pass through each doughnut successively, finally leave stripper, realized multistage stripping in this way.The shortcoming of this structure is complex structure, is not suitable for the bigger operating mode of catalyst circulation amount especially.
Disclosed a kind of catalytic cracking external warmer among the CN2515637Y with ailhead heat-transfer pipe.In this type external warmer, the ailhead heat-transfer pipe places within the cylindrical housings, and each root ailhead heat-transfer pipe is an enclosed construction, is made up of the steam jacket of feed pipe and band ailhead, constitutes the heat transfer element with independent vapour circuit.One end of ailhead heat-transfer pipe is fixed on the end socket, and the other end is positioned in the housing, retractable.This novel external warmer not only has higher heat transfer efficiency, and has good wearability and reliability.
USP5 has introduced the external warmer of similar shell-and-tube heat exchanger pattern in 209,287, and its heat-transfer pipe is thinner, and water and steam are walked tube side, and is vertically dirty along tube wall, and the bottom is provided with fluidized wind with catalyst fluidization.This external warmer compact conformation, heat transfer area is big.Shortcoming is that the heat-transfer pipe tube wall is thinner, is easy to by catalyst worn outly, in case a heat-transfer pipe is worn out, whole external warmer lost efficacy, and changed very difficult.
Introduced a kind of unit pipes group header type external warmer among the CN1045644A, it is made up of housing and some heat transfer unit pipe groups, the slightly larger in diameter of heat-transfer pipe, and each unit pipes group comprises many heat-transfer pipes, pool together by upper header and lower collecting box, draw housing from top then.This external warmer characteristics are that catalyst fluidization is in good condition, and each unit pipes group respectively has valve control, opening and closing voluntarily, and a unit pipes group is out of order, and does not influence the use of whole heat collector.Shortcoming is that the heat-transfer pipe between upper header, the lower collecting box at high temperature nonvolatil distortion takes place easily and influences its service life.
Although aspect flue gas stripping and the catalyst cooling a lot of patented technologies are being arranged, the catalytic cracking regenerant flue gas stripping device with catalyst refrigerating function does not appear in the newspapers as yet.
Summary of the invention
The purpose of this invention is to provide a kind of catalytic cracking regenerant flue gas stripping device that has the catalyst refrigerating function concurrently, not only make regenerative agent remove the flue gas that it is carried secretly as much as possible, but also can reduce the heat-obtaining load of external warmer.
Flue gas stripping device provided by the present invention mainly comprises with lower member: regenerated catalyst ingress pipe 1, flue gas stripping device cylindrical shell 2, stripping dielectric distribution device 3 and 4, regenerator sloped tube 5, different inner sleeve 6a and 6b, stripping medium delivery line 7, heat removing tube 8, bottom baffles 9 and the catalyst outlet pipes 10 of diameter; Wherein, regenerated catalyst ingress pipe 1 and stripping medium delivery line 7 are arranged at the top of this flue gas stripping device respectively, and regenerator sloped tube 5 is arranged at the bottom of this flue gas stripping device; Stripper bottom baffles 9 is fixedlyed connected with stripper cylindrical shell and catalyst outlet pipe 10; Stripping dielectric distribution device 4 is positioned at the top of bottom baffles 9, inner sleeve 6b is arranged at the top of stripping dielectric distribution device 4, and the upper end of inner sleeve 6a that is arranged at inner sleeve 6b inside is low than the upper end of inner sleeve 6b, and stripping dielectric distribution device 4 is passed in its lower end and bottom baffles 9 forms catalyst outlet pipes 10; The stripping dielectric distribution device 3 that is arranged at catalyst outlet pipe 10 inside is positioned at the below of heat removing tube; The heat-obtaining medium of heat removing tube 8 imports end and derives end and is arranged at this flue gas stripping device outside, and remainder is positioned at flue gas stripping device inside.
Compared with prior art, beneficial effect of the present invention is mainly reflected in following aspect:
1.FCC device adopts the catalytic cracking regenerant flue gas stripping device of catalyst refrigerating function of the present invention, not only can solve the problem that regenerative agent is carried flue gas secretly, and, therefore can reduce the heat-obtaining load of external warmer to a certain extent because the present invention has the function of catalyst cooling.
2. utilize provided by the present inventionly have the regenerative agent stripper of catalyst refrigerating function, by rational technology Calculation, in the design process of FCC reaction-regeneration system, can cancel conventional external warmer, substitute with stripper provided by the present invention the double action that makes this stripper reach the steam stripping regeneration agent simultaneously and take out superfluous heat.
3. the present invention makes catalyst circuitous flowing in stripper, thereby has realized repeatedly contacting of water vapour and catalyst by adopting two different inner sleeves of diameter, has played the steam stripped effect of multistage, has improved steam stripping efficiency greatly; Simultaneously, in circuitous the flowing of catalyst, also realized with heat removing tube in the heat exchange of the heat-obtaining medium that flows, make the water that flows in the heat removing tube become water vapour.
4. in the FCC process, adopt the present invention can reduce the operating temperature of regenerative agent stripper, avoid catalyst hydrothermal deactivation at high temperature.
5. equipment flue gas Srteam Stripping effect provided by the present invention is good, and heat-obtaining is flexible, operation is reliable.
Description of drawings
Fig. 1 is the structural representation of flue gas stripping device provided by the present invention.
Fig. 2 be stripper shown in Figure 1 along A-A to profile.
Fig. 3 is the structural representation of heat removing tube of the present invention.
Fig. 4 is the structural representation of the disclosed ailhead heat removing tube of CN2515637Y.
The specific embodiment
Further specify regenerative agent flue gas stripping device provided by the present invention below in conjunction with accompanying drawing, but therefore the present invention is not subjected to any restriction.
As shown in Figure 1, the regenerated catalyst ingress pipe 1 that links to each other with regenerator is positioned at the top of this stripper, and fixedlys connected with the cylindrical shell 2 of stripper.Stripping medium delivery line 7 also is positioned at the top of this stripper, and fixedlys connected with the cylindrical shell 2 of stripper.Regenerated catalyst ingress pipe 1 and stripping medium delivery line 7 preferably are positioned at the both sides, top of this stripper.
Regenerator sloped tube 5 is positioned at the bottom of this flue gas stripping device, and it is fixedly connected with flue gas stripping device and be connected, and makes catalyst behind the stripping be able to be delivered to reactive moieties by this regenerator sloped tube and recycles.
The bottom of stripper is provided with dividing plate 9, this bottom baffles is fixedlyed connected with stripper cylindrical shell and catalyst outlet pipe 10, the catalyst of finishing stripping and heat transfer process in the flue gas stripping device can only be delivered to reactive moieties through regenerator sloped tube 5 and recycle then by 10 outputs of catalyst outlet pipe.
Stripping dielectric distribution device 4 is positioned at the top of bottom baffles 9, and this stripping dielectric distribution device not directly is arranged on the bottom baffles, needs to leave the space that certain being used to installed and overhauled according to common designing requirement.Inner sleeve 6b is arranged at the top of stripping dielectric distribution device 4, and the vertical range suggestion of its lower end to stripping dielectric distribution device 4 upper surfaces is not less than 5 centimetres, preferably is not less than 10 centimetres.And the upper end of inner sleeve 6a that is arranged at inner sleeve 6b inside is low than the upper end of inner sleeve 6b.Be arranged at the inner sleeve 6b and the inner sleeve 6a of stripper inside, the difference in height of the two upper end preferably is not less than 10 centimetres, preferably is not less than 20 centimetres.The height of inner sleeve 6b and inner sleeve 6a should be suitable with the height of this stripper inner catalyst bed.The best coaxial setting of inner sleeve 6b and inner sleeve 6a, and inner sleeve 6b and inner sleeve 6a be preferably designed as circular cylinder body, but the cylindrical shell of other shape, for example, hexagon, octagon or dodecagonal cylindrical shell etc. also can reach effect of the present invention.The lower end of inner sleeve 6a is catalyst outlet pipe 10 after passing stripping dielectric distribution device 4 and bottom baffles 9.Stripping dielectric distribution device 3 is arranged at catalyst outlet pipe 10 inside, but is positioned at the below of the heat removing tube that is arranged at inner sleeve 6a inside.
The present invention is as depicted in figs. 1 and 2 I, II and three districts of III by above-mentioned inner sleeve 6a and 6b are set with the effective stripping spatial division in the stripper in stripper, make the catalyst that enters in the stripper this three districts that flow through successively.Concrete catalyst stream flowing mode is referring to this flue gas stripping device workflow part.Effective stripping of the present invention space is meant and is positioned at the above stripping space that beds occupied of bottom baffles in the flue gas stripping device.
Fig. 2 be the A-A of stripper shown in Figure 1 to profile, wherein, shown in heat removing tube 8 vertically and equably be arranged in the stripper. Inner sleeve 6a and 6b are divided into as shown in the figure I, II and three districts of III with this stripper.For the long-pending ratio in the effective cross section in described three districts, the preferred I of the present invention: II: III=0.3-3: 0.3-3: 1, further preferred I: II: III=0.4-2.5: 0.4-2.5: 1.
The heat-obtaining medium of heat removing tube 8 of the present invention imports and derives end and is arranged at this flue gas stripping device top, and the remainder of heat removing tube is positioned at flue gas stripping device inside.Described heat removing tube preferred vertical and being arranged in the stripper equably.The quantity of heat removing tube can be one, also can be many, and for example, the 3-40 root needs the factors such as size in catalyst flow, heat-obtaining load and available space according to device to determine.Described heat removing tube is preferably formed as independently heat-obtaining medium circulation loop; Heat removing tube can adopt structure as shown in Figure 3, also can adopt other follow-on heat removing tube, and the ailhead heat removing tube disclosed in CN2515637Y is referring to Fig. 4.
Wherein, Figure 3 shows that a kind of independently heat removing tube schematic diagram in heat-obtaining medium circulation loop that forms, liquid heat-obtaining medium enters through inlet tube 1a, circular passage 3a along heat removing tube flows downward, in process of flowing, absorb the entrained heat of high-temperature regenerated catalyst in the stripper indirectly, and change gaseous state into by liquid state gradually by tube wall.The heat-obtaining medium that flows to heat removing tube bottom changes flow direction, upwards flow by the central tube 4a that is arranged at heat removing tube inside, after outlet 2a draw.
Fig. 4 is the ailhead heat removing tube disclosed in the CN2515637Y, and the difference of itself and Fig. 3 is: the enhanced heat exchange element 5a of many ailhead shapes has been fixed in the heat removing tube outside, to increase heat transfer area, to improve heat transfer efficiency.
The workflow of flue gas stripping device provided by the present invention is as follows: the regenerated catalyst from top to down that enters in this stripper through ingress pipe 1 flows, and at first enters I district as shown in the figure.The stripping medium is distributed in this stripper as far as possible equably through stripping dielectric distribution device 3 and 4, catalyst in process of flowing with the stripping medium, fully contact as steam or dry gas.The catalyst that flows to the stripper bottom changes flow direction under the acting in conjunction of stripping medium and bottom baffles, then upwards flows, enters the II district.Catalyst flows in the II district from bottom to up, to top, II district, enters the III district through inner barrel 6a upper end overflow.The catalyst that enters the III district at gravity with from the acting in conjunction of the stripping medium of stripping dielectric distribution device 3 under then flow downward, and finally discharge by catalyst outlet pipe 10 and regenerator sloped tube 5.
Catalyst contacts with heat collector 8 in being arranged at stripper in above-mentioned circuitous process of flowing, makes the entrained heat of catalyst send the heat-obtaining medium that flows in the heat removing tube to by the tube wall of heat removing tube.The heat-obtaining medium, for example, water preferably through the necessary demineralized water of handling, injects heat removing tube through the heat-obtaining medium inlet of heat removing tube 8, and the tube wall by heat removing tube absorbs the heat in this stripper, makes the heat-obtaining medium change gaseous state into by liquid state; The heat-obtaining medium of gaseous state is drawn by the top heat-obtaining media outlet of heat removing tube.Each heat removing tube of the present invention is preferably formed as independent control loop, does not influence the work of other heat removing tube when breaking down with one of them heat removing tube of box lunch.
Regenerated catalyst is circuitous in the manner described above to flow by making, and fully contacts with the stripping medium in flow process, and the flue gas that regenerated catalyst is carried secretly removes as much as possible.The regenerated flue gas that stripping medium and institute's stripping go out compiles at the top of this stripper, and draws by stripping medium delivery line 7.
In stripper of the present invention, when adopting steam as the stripping medium, the preferred 1-10kg/ ton of the consumption of its stripped vapor catalyst; The preferred 0.05-0.5m/s of stripping linear speed; Preferred 10-120kg. (the m of catalyst quality flow rate in this stripper
2.s)
-1, the preferred 0.2-4min of its catalyst mean residence time.
The following examples will give further instruction to method provided by the present invention, but therefore the present invention is not subjected to any restriction.
Embodiment
This embodiment explanation: adopting the beneficial effect that is brought behind the flue gas stripping device of the present invention on the FCC apparatus.
In disposal ability is 100 * 10
4The heavy oil catalytically cracking equipment in ton/year is transformed, and sets up flue gas stripping device of the present invention.This flue gas stripping device diameter is 2400mm, high 5650mm.The structure of this stripper as shown in Figure 1, wherein, the ratio that amass the effective cross section in I, II and three districts of III 1.5: 2: 1,10 centimetres of the vertical ranges of the lower end of inner sleeve 6b to stripping dielectric distribution device 4 upper surfaces, inner sleeve 6b and inner sleeve 6a, the difference in height of the two upper end is 20 centimetres.20 of ailhead heat removing tubes are set in this stripper altogether, and heat removing tube length 5.1m, single tube heat transfer area are 5.6m
2, total heat conduction area is 112m
2, thermic load is 1.56 * 107W.Adopt steam as the stripping medium, the linear speed 0.2m/s of stripped vapor.Through industrial performance test, regenerator dense-phase bed temperature drops to 698 ℃ by 705 ℃, and non-hydrocarbon gas content is reduced to 1.68% from original 18% in the dry gas.
Claims (10)
1, a kind of regenerated catalyst steam-stripping device of flue gas is characterized in that this flue gas stripping device mainly comprises with lower member: the inner sleeve (6a) that regenerated catalyst ingress pipe (1), flue gas stripping device cylindrical shell (2), stripping dielectric distribution device (3) and (4), regenerator sloped tube (5), diameter are different and (6b), stripping medium delivery line (7), heat removing tube (8), bottom baffles (9) and catalyst outlet pipe (10); Wherein, regenerated catalyst ingress pipe (1) and stripping medium delivery line (7) are arranged at the top of this flue gas stripping device respectively, and regenerator sloped tube (5) is arranged at the bottom of this flue gas stripping device; Stripper bottom baffles (9) is fixedlyed connected with stripper cylindrical shell and catalyst outlet pipe (10); Stripping dielectric distribution device (4) is positioned at the top of bottom baffles (9), inner sleeve (6b) is arranged at the top of stripping dielectric distribution device (4), and the upper end that is arranged at the inner inner sleeve (6a) of inner sleeve (6b) is low than the upper end of inner sleeve (6b), and stripping dielectric distribution device (4) is passed in its lower end and bottom baffles (9) forms catalyst outlet pipe (10); The stripping dielectric distribution device (3) that is arranged at catalyst outlet pipe (10) inside is positioned at the below of heat removing tube; The heat-obtaining medium of heat removing tube (8) imports end and derives end and is arranged at this flue gas stripping device outside, and remainder is positioned at flue gas stripping device inside.
2,, it is characterized in that described regenerated catalyst ingress pipe (1) and stripping medium delivery line (7) are positioned at the both sides, top of this stripper according to the flue gas stripping device of claim 1.
3,, it is characterized in that the vertical range of lower end to stripping dielectric distribution device (4) upper surface of described inner sleeve (6b) is not less than 5 centimetres according to the flue gas stripping device of claim 1.
4,, it is characterized in that the difference in height of the two upper end of described inner sleeve (6b) and inner sleeve (6a) is not less than 10 centimetres according to the flue gas stripping device of claim 1.
5,, it is characterized in that described inner sleeve (6b) and the coaxial setting of inner sleeve (6a), and they are circular cylinder body according to the flue gas stripping device of claim 1.
6, according to the flue gas stripping device of claim 1, it is characterized in that 3-40 root heat removing tube is set in the described stripper, described heat removing tube vertically and equably is distributed in the stripper.
7,, it is characterized in that described heat removing tube is the ailhead heat removing tube according to the flue gas stripping device of claim 6.
8, according to the flue gas stripping device of claim 1, it is characterized in that described inner sleeve (6a) and (6b) be I, II and three districts of III, and the long-pending ratio in the effective cross section in described three districts is I: II: III=0.3-3: 0.3-3: 1 the effective stripping spatial division in this stripper.
9,, it is characterized in that the long-pending ratio in effective cross section in described three districts is I: II: III=0.4-2.5: 0.4-2.5: 1 according to the flue gas stripping device of claim 8.
10,, it is characterized in that described heat removing tube is for having the heat removing tube of independent closed circuit separately according to the flue gas stripping device of claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100838903A CN100337735C (en) | 2004-10-22 | 2004-10-22 | Regenerated catalyst steam-stripping device of flue gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100838903A CN100337735C (en) | 2004-10-22 | 2004-10-22 | Regenerated catalyst steam-stripping device of flue gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN1762567A true CN1762567A (en) | 2006-04-26 |
| CN100337735C CN100337735C (en) | 2007-09-19 |
Family
ID=36747016
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CNB2004100838903A Expired - Lifetime CN100337735C (en) | 2004-10-22 | 2004-10-22 | Regenerated catalyst steam-stripping device of flue gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN100337735C (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100464830C (en) * | 2006-07-26 | 2009-03-04 | 中国石油大学(北京) | Combined catalyst stripper |
| WO2020078411A1 (en) * | 2018-10-17 | 2020-04-23 | 中国石油化工股份有限公司 | Gas replacement method and device, and hydrogenation method for nitro compound |
| RU2805504C2 (en) * | 2018-10-17 | 2023-10-18 | Чайна Петролиум & Кемикал Корпорейшн | Method of gas replacement, apparatus for gas replacement and method of carrying out the nitro compound hydrogenation reaction |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5260034A (en) * | 1992-04-24 | 1993-11-09 | Shell Oil Company | Stage catalyst concentric annular stripper |
| CN2455355Y (en) * | 2000-11-10 | 2001-10-24 | 石油大学(北京) | High performance reproduced catalyst stripping apparatus |
| CN2515637Y (en) * | 2001-11-28 | 2002-10-09 | 中国石化工程建设公司 | External heat-transfer apparatus |
-
2004
- 2004-10-22 CN CNB2004100838903A patent/CN100337735C/en not_active Expired - Lifetime
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN100464830C (en) * | 2006-07-26 | 2009-03-04 | 中国石油大学(北京) | Combined catalyst stripper |
| WO2020078411A1 (en) * | 2018-10-17 | 2020-04-23 | 中国石油化工股份有限公司 | Gas replacement method and device, and hydrogenation method for nitro compound |
| JP2022512758A (en) * | 2018-10-17 | 2022-02-07 | 中国石油化工股▲ふん▼有限公司 | Hydrogenation reaction process of nitro compounds, and hydrogenation reaction equipment |
| RU2805504C2 (en) * | 2018-10-17 | 2023-10-18 | Чайна Петролиум & Кемикал Корпорейшн | Method of gas replacement, apparatus for gas replacement and method of carrying out the nitro compound hydrogenation reaction |
| JP7434307B2 (en) | 2018-10-17 | 2024-02-20 | 中国石油化工股▲ふん▼有限公司 | Nitro compound hydrogenation reaction process and hydrogenation reaction equipment |
| US12116331B2 (en) | 2018-10-17 | 2024-10-15 | China Petroleum & Chemical Corporation | Gas replacement process, gas replacement apparatus, and nitro compound hydrogenation reaction process |
Also Published As
| Publication number | Publication date |
|---|---|
| CN100337735C (en) | 2007-09-19 |
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