CN1357601A - Method and apparatus for treating mixed gas containing dilute reactant - Google Patents
Method and apparatus for treating mixed gas containing dilute reactant Download PDFInfo
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- CN1357601A CN1357601A CN 00134819 CN00134819A CN1357601A CN 1357601 A CN1357601 A CN 1357601A CN 00134819 CN00134819 CN 00134819 CN 00134819 A CN00134819 A CN 00134819A CN 1357601 A CN1357601 A CN 1357601A
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- 238000000034 method Methods 0.000 title claims abstract description 47
- 239000000376 reactant Substances 0.000 title claims abstract description 39
- 239000007788 liquid Substances 0.000 claims abstract description 56
- 238000010521 absorption reaction Methods 0.000 claims abstract description 55
- 230000003197 catalytic effect Effects 0.000 claims abstract description 30
- 239000011541 reaction mixture Substances 0.000 claims abstract description 15
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 claims description 84
- 238000006555 catalytic reaction Methods 0.000 claims description 78
- 239000006096 absorbing agent Substances 0.000 claims description 38
- 230000008569 process Effects 0.000 claims description 22
- 238000006243 chemical reaction Methods 0.000 claims description 19
- 238000009833 condensation Methods 0.000 claims description 11
- 230000005494 condensation Effects 0.000 claims description 11
- 238000000605 extraction Methods 0.000 claims description 11
- 241000521257 Hydrops Species 0.000 claims description 9
- 206010030113 Oedema Diseases 0.000 claims description 9
- 239000000945 filler Substances 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 7
- 238000010992 reflux Methods 0.000 claims description 6
- 241000282326 Felis catus Species 0.000 claims description 5
- 229910021536 Zeolite Inorganic materials 0.000 claims description 4
- 239000010457 zeolite Substances 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 3
- 230000000694 effects Effects 0.000 abstract description 10
- 239000007789 gas Substances 0.000 description 65
- YNQLUTRBYVCPMQ-UHFFFAOYSA-N Ethylbenzene Chemical compound CCC1=CC=CC=C1 YNQLUTRBYVCPMQ-UHFFFAOYSA-N 0.000 description 48
- 230000009102 absorption Effects 0.000 description 41
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 17
- 239000003054 catalyst Substances 0.000 description 16
- 238000004821 distillation Methods 0.000 description 15
- 239000005977 Ethylene Substances 0.000 description 11
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- 238000005516 engineering process Methods 0.000 description 5
- 238000002309 gasification Methods 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 239000007787 solid Substances 0.000 description 4
- 239000007921 spray Substances 0.000 description 4
- 238000004140 cleaning Methods 0.000 description 3
- 230000006872 improvement Effects 0.000 description 3
- 238000005086 pumping Methods 0.000 description 3
- 150000001336 alkenes Chemical class 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 230000005587 bubbling Effects 0.000 description 2
- 238000004939 coking Methods 0.000 description 2
- 230000009849 deactivation Effects 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000011068 loading method Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- 231100000572 poisoning Toxicity 0.000 description 2
- 230000000607 poisoning effect Effects 0.000 description 2
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- 208000036829 Device dislocation Diseases 0.000 description 1
- 230000002152 alkylating effect Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- SYWDWCWQXBUCOP-UHFFFAOYSA-N benzene;ethene Chemical compound C=C.C1=CC=CC=C1 SYWDWCWQXBUCOP-UHFFFAOYSA-N 0.000 description 1
- 238000003442 catalytic alkylation reaction Methods 0.000 description 1
- 230000008859 change Effects 0.000 description 1
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- 239000008246 gaseous mixture Substances 0.000 description 1
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- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical compound S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
Abstract
The present invention treat mixed gas containing dilute reactant by means of catalytic absorption method with outer circulation inside a catalytic absorption tower. The tower includes one catalytic absorption section, one tail gas condensator, one optional liquid trap, one fraction extracting section and one reboiler and features its outer circulator, preferably including one fixed bed reactor, to return partial liquid reaction mixture from the bottom of the catalytic absorption section into the tower via the top of the catalystic absorption section. The present invention is simple, reliable, flexible, high in treating effect and low in power consumption.
Description
The present invention relates to a kind of processing and contain the novel method of mixed gas of rare reactant and used equipment thereof.Or rather, the present invention relates to gas-liquid-solid three-phase catalysis absorption novel method and the equipment thereof that a kind of catalysis absorption process with the band outer circulation is handled the mixed gas that contains rare reactant.
In many industrial sectors and environmental protection field, often there are the needs that the mixed gas that contains rare reactant carried out versatility and/or the processing of purification property.For example contained rare ethene (the generally about 5-20% of content) in the dry gas of petrochemical industry refinery discharge there is the value of comprehensive utilization, can makes important chemical material ethylbenzene by making itself and benzene carry out alkylation.And for example main pollutent comprises harmful nitrogen oxide compound (NOx) and the oxysulfide (SOx) that contains in the coal firing boiler chimney tail gas of fuel-burning power plant in the modern city, its content is generally less than 1%, removing of they become a vital task in the atmosphere environmental protection, and this also can collect after making itself and other material react, generate harmless even useful material.
The rare reactant that contains in said mixed gas and the chemical reaction of other material can be realized with catalysis absorption process and/or catalytic distillation process, for example submitting to by Beijing Institute of Clothing Tech, still chat in the undocumented Chinese patent application 99124797.3 and a kind of method and apparatus for preparing ethylbenzene by benzene and the alkylation of oil refinery dry gas catalytic distillation process, wherein make oil refinery dry gas and benzene charging go into tower from the bottom and the top of catalytic distillation tower respectively, make it to flow in opposite directions and react at catalytic distillation zone, product is fractionation by distillation simultaneously, obtains conversion of ethylene and ethylbenzene selectivity preferably.
In Chinese patent application 97117321.4 by No.2 Chemical Plant, Yanhua Petrochemical Corp., Ltd., Beijing and Beijing Institute of Clothing Tech's co-applications, a kind of technology of using bubbling bed catalysis absorption process alkylation to prepare ethylbenzene is disclosed, gaseous ethylene or contain the gas of ethene such as oil refinery dry gas and liquid phenenyl enter catalyst bed by the reactor bottom bubbling wherein, carry out gas-liquid-solid phase reaction, the operational condition of controlling reactor is operated it under the gasification stagnation point near benzene.This technology is a catalysis absorption technique in essence.
Handling in the process of the mixed gas that contains rare reactant with catalytic distillation process or catalysis absorption process, the contriver finds the defective that they still exist some further to overcome separately, and this is because pending mixed gas only contains rare reactant thereby very big these characteristics of gas flux by tower cause:
For catalytic distillation process, one side is very big by the flux of the mixed gas of catalytic distillation section, and liquid flux is subjected to the restriction of two factors and be difficult to corresponding increase: the first is subjected to the restriction of the ratio of feeding liquid/solid/liquid/gas reactions thing amount, and the adjusting leeway of the inlet amount of liquid reactants is little; It two is if be increased in the flux of liquid in the catalytic distillation section by the quantity of reflux that increases overhead condensation liquid, then can corresponding requirements increase the steam output of tower still and the condensation number of cat head, cause the remarkable increase of energy consumption, the temperature that catalyzer bore that also causes simultaneously being equipped with in the catalytic distillation section raises, and this is unfavorable for controlling favourable reaction conditions.Therefore liquid flux is difficult to be increased to the degree that the big flux with mixed gas adapts in the tower, and it is fully wetting that this just makes the filler that is equipped with in the catalytic distillation section and catalyzer be difficult to by liquid, thereby some just is exposed in the mixed gas.This phenomenon makes the gas-liquid mass transferring function of filler and catalyzer and the response function of catalyzer can effectively not give full play to, but also be easy to cause polymers matter (if the words that exist) simultaneously and, cause the poisoning or the coking and deactivation on catalyst activity surface in the lip-deep oligomerisation of activity of such catalysts.This directly causes the transformation efficiency of gas reactant and selectivity of product to be difficult to reach gratifying degree, and catalyst life shortens.
For the catalysis absorption process, same, very big by the mixed gas flux of catalysis absorber portion, and liquid flux is subjected to the restriction of the ratio of feeding liquid/solid/liquid/gas reactions thing amount, the adjusting leeway of the inlet amount of liquid reactants not quite makes the liquid spraying amount be difficult to corresponding increase.It is fully wetting that this just makes the filler that is equipped with in the catalysis absorber portion and catalyzer be difficult to by liquid, thereby some just is exposed in the mixed gas.Equally, this phenomenon makes that the gas-liquid mass transferring function on filler and the catalyzer and the response function of catalyzer can not effectively be given full play to, but also be easy to cause polymers matter (if the words that exist) simultaneously and, cause the poisoning or the coking and deactivation on catalyst activity surface in the lip-deep oligomerisation of activity of such catalysts.This directly causes the transformation efficiency of gas reactant and product selectivity to reduce, and catalyst life shortens.
In addition, owing to only contain the less gas reactant in the mixed gas, and the rare gas element composition that is in the great majority also will pass through catalytic distillation tower or catalysis absorption tower, be in the tower gas throughput than handling in the general tower that does not contain or lack the gas-liquid reaction system that contains rare gas element big several times even tens times of gas throughput, and the also corresponding to a certain extent increase of respective liquid flux, if will ensure that pressure drop is not excessive in the tower, must guarantee that then catalytic distillation section or catalysis absorber portion in the tower reach certain voidage, also be that the loaded catalyst in the bed is restricted.If catalyst activity is not high especially or catalyzer is not in optimal working temp, often be difficult to then guarantee that the gaseous reactant that all absorptions are dissolved in the liquid phase can react completely, this has also restricted the raising of the transformation efficiency of gaseous reactant to a certain extent, even causes the partial loss of gaseous reactant.
In order to address the above problem, the inventor is from being started with by this reaction system of the ethylbenzene by alkylating low-density ethylene benzene and the oil refinery dry gas, studied the rule that the mixed gas that contains rare reactant and a kind of liquid reactants carry out gas-liquid-solid phase reaction in great detail, catalysis absorption technique and equipment thereof mixed gas, the band outer circulation that a kind of processing contains rare reactant have been proposed on this basis, solved better above-mentioned, handle the problem that exists in the process of the mixed gas that contains rare reactant with catalytic distillation process or catalysis absorption process at present.
See also narration in the Chinese patent application of submitting to by Beijing Institute of Clothing Tech 99124797.3 about carry out relevant progress that alkylation prepares ethylbenzene by the rare ethene that contains in benzene and the oil refinery dry gas, and related content is incorporated in the present patent application specification sheets in this statement.
Accompanying drawing 1 be one by the generalized flowsheet synoptic diagram of catalysis absorption technique of the present invention, the band outer circulation.
By of the present invention, with the rare second that makes with the catalytic absorption technology of outer circulation in benzene and the oil refinery dry gas It is to inhale in the catalysis with outer circulation as shown in Figure 1 that alkene carries out the process that alkylation prepares ethylbenzene Carry out in the receipts tower. The catalytic absorption tower comprises that a catalytic absorption section and a tail gas condensing reflux Device, and the hydrops groove, stripping section and the tower reactor reboiler that insert in case of necessity, the catalytic absorption section In filler and catalyst are housed, it is characterized in that it comprises that also a cover is used at the bottom of the catalytic absorption section The liquid reaction mixture of section returns the external circulating device at catalytic absorption section top. Pressing side of the present invention In the operation of method, the operating parameter of adjusting tower, even reaction temperature is 140-200 ℃, pressure is (1.5-3.0) * and MPa, liquid reactant is excessive generally speaking, the liquid/gas reactant molar ratio Be 2: 1-12: 1, use a kind of HY-BE type beta-zeolite catalyst, make most of benzene, product Ethylbenzene and heavier accessory substance remain liquid state in tower, the ethene in the dry gas and other composition keep Be gaseous state; Pending benzene charging and the dry gas that contains rare ethene respectively from the top of catalytic absorption section and Charging under the bottom, the catalytic absorption section of flowing through opposite to each other makes it the filler-urge in being loaded on this section Change on the agent bed and contact, mass transfer, catalytic alkylation reaction take place to absorb and generate product ethylbenzene; Bag Contain the tail gas of benzene of the inert component in the dry gas, a small amount of unreacted ethene and gasification through the tail of cat head The gas condenser condensation collects and returns the benzene condensation of gasification in the tower; And comprised major part The liquid reaction mixture of benzene, product ethylbenzene and heavier accessory substance moves to the tower bottom; Its feature exists In, take out the partially liq mixture from catalytic absorption section bottom and return through said external circulating device pumping To the top of catalytic absorption tower, spray with the benzene charging and to enter in the catalytic absorption section, and remaining fluid The optional stripping section concentrate that arranges through the tower bottom of attitude product mixtures mainly contains ethylbenzene from the tower reactor extraction Product liquid.
Explain in more detail process of the present invention below in conjunction with accompanying drawing.
Fig. 1 is the schematic flow sheet by processing method of the present invention, its essential part be a cover only with the catalysis absorption equipment of external circulating device, comprise a catalysis absorption tower C-01, a cover external circulating device (5., C-02 and 6.) and tail gas condenser E-01 and charging accordingly and discharging pipeline.Have only the catalysis absorber portion in the C-01 of catalysis absorption tower, do not have stripping section, hydrops groove and tower still reboiler E-02.Outer circulation device can be to overlap for example pipeline system of pumping liquid, and wherein C-02 can be a straight-through pipeline, also can be arranged to fixed-bed reactor as required.In the catalysis absorber portion catalyzer is housed, catalyzer can with the random packing mixed packing, in the structured packing of also can packing into, can also adopt jet-type tray column filling.
Through the oil refinery dry gas of preliminary cleaning through 1. feeding C-01 by catalysis absorber portion below, through the benzene of preliminary cleaning through 3. feeding C-01 by the top of catalysis absorber portion.Reacted gaseous mixture goes out the benzene of a small amount of gasification after 7. discharged by cat head through item gas condenser E-01 condensation; The benzene that condensation is got off returns the top of catalysis absorber portion; Product ethylbenzene liquid by tower at the bottom of 8. extraction; Return the top of catalysis absorber portion from catalysis absorber portion bottom with most of liquid reaction mixture through the external circulating system pumping, and spray with the fresh benzene charging and to enter in the catalysis absorption tower.The concentration of contained gas reactant is decided in amount of liquid that external circulating system returns will be according to the mixed gas charging, and it generally was at least 1: 1 with 8. the ratio of product load at the bottom of tower, was preferably 2: 1 to 5: 1.
According to a preferred embodiment of the inventive method, on the basis of catalysis absorption process basic, the band outer circulation and equipment, make the C-02 in the external circulating device be designed to fixed-bed reactor, the catalyzer of wherein packing into.The loading amount of catalyzer is generally the 5-50% of catalyzer inventory among the C-02, concrete loading amount decide with the performance and the temperature of reaction of catalyzer, also promptly in fact decides with lysed in the product liquid mixture that flows to bottom the catalysis absorber portion but unreacted ethylene content.At this moment, 1. dry gas through feeding C-01 by catalysis absorber portion below, 3. benzene through sending into the top of catalysis absorber portion, extract the liquid reaction mixture of major portion out through 5. sending into postreaction the C-02 from the below of catalysis absorber portion, again through 6. delivering to catalysis absorber portion top, enter catalysis absorber portion with fresh benzene charging from this position spray at this, product by tower at the bottom of 8. extraction.Adopt the benefit of this embodiment to be, can in tower, use active lower slightly catalyzer on the one hand or use lower slightly service temperature, be beneficial to the abundant absorption mass transfer of gaseous reactant in liquid reactant, be dissolved in catalysis absorber portion bottom in the liquid reaction mixture but unreacted completely gaseous reactant can be in C-02 postreaction complete, can further improve the transformation efficiency of gaseous reactant like this, therefore improve its utilization ratio; On the other hand, because C-02 is located in the external circulating device, its design and configuration are carried out as the operation that selecting for use of the selection of structure, catalizer variety and the consumption of catalyst bed, operational condition etc. all can be independent of tower, make method and apparatus of the present invention have more handiness.
Another preferred embodiment according to the inventive method, on the basis of catalysis absorption process basic, the band outer circulation and equipment, under the catalysis absorber portion, increase a stripping section and tower still reboiler E-02, between catalysis absorber portion and stripping section, increase a hydrops groove.Can pack in the stripping section column plate or high efficiency packing.1. dry gas through feeding C-01 by stripping section, 3. benzene through entering the top of catalysis absorber portion, from the hydrops groove, extract liquid reaction mixture out, send into the top of catalysis absorber portion through external circulating system, spray with fresh benzene charging there and enter in the tower, through spissated product ethylbenzene at the bottom of the still through 8. extraction.In external circulating device, do not establish reactor C-02 this moment.
This embodiment is specially adapted to that catalyzed reaction function among the C-01 can be given full play to but situation that the extraction degree of purity of production is had relatively high expectations.The liquid reaction mixture of collecting from catalysis absorber portion bottom through the stripping section enrichment after, lighter benzene is mainly stayed top and is turned back to cat head through external circulating system and enters the catalysis absorber portion again, and main product ethylbenzene and heavier product by still at the bottom of through 8. extraction, its concentration ratio has significant improvement during without the stripping section enrichment, and for example ethylbenzene purity can reach 70%.But consider the restriction of tower still temperature, generally be controlled at about 20%.
According to another embodiment preferred of the present invention be, on the basis of catalysis absorption process basic, the band outer circulation and equipment, both increased stripping section, reboiler E-02 and hydrops groove, in external circulating device, set up fixed bed catalytic reactor C-02 again.Concrete distributing style and technical process are seen described in last two preferred embodiments.It is insufficient and to the high situation of concentration requirement of the product ethylbenzene of extraction that this embodiment is specially adapted to the performance of catalyzed reaction function among the C-01.
Possesses outstanding advantage by Processes and apparatus of the present invention, that handle the mixed gas contain rare reactant with the catalysis absorption process of band outer circulation, for example it is a gas-liquid-solid three-phase absorption-reaction-isolating collaborative processes, carrying out gas-liquid reaction in same tower simultaneously separates with product, this simplifies and intensive technology and equipment, is adapted to especially handle wherein contain at least a mixed gas that can transform rare gaseous reactant of collection through reaction.Increase the flux of liquid reactants and increase preferred the setting as required by outer circulation, reached the reinforcement absorption process and thereby increase transformation efficiency, effectively the guard catalyst activity, suppress side reaction, energy-conservation and purposes such as flexibility of operation is big, production concentration height.
Below in conjunction with explaining the present invention in more detail by the specific embodiment of benzene and oil refinery dry gas alkylation to prepare ethylbenzene, but this does not also mean that by method and apparatus of the present invention and only is applicable to by benzene and oil refinery dry gas alkylation to prepare ethylbenzene, does not mean that the present invention is only limited to this several forms of implementation yet.Being suitable for handling the wherein at least a diluted gas reactant that contains in essence by method and apparatus of the present invention can transform the mixed gas of collecting through reaction, for example to the collection utilization of the diluted gas composition that contains in chemical industry, petrochemical industry and other industrial sector discharge tail gas, can transform through reaction or purify and remove.Those of ordinary skills can continue to make many changes and improvements according to the present patent application disclosure; comprise and handle different mixed gass and adopt different forms of implementation, but these changes and improvements do not exceed the determined scope of asking for protection of accompanying Claim book.The catalysis absorption technique of embodiment 1 band outer circulation
Adopt equipment and technical process shown in Figure 1.Before going into tower, oil refinery dry gas and benzene are all handled through preliminary cleaning.The catalysis absorption tower includes only a catalysis absorber portion C-01 and a condenser E-01, is not with reactor C-02 in the external circulating system.The tower diameter of catalysis absorption tower C-01 is φ 30mm, tower height 1.4m, interior dress φ 4 * 4 four hole HY-BE type beta-zeolite catalyst 50g (being produced by Hua Yutong side, Beijing chemical science and technology development company).Adopt and φ 4 θ ring filler mixed packings.In the C-01 that packs into behind 20: 80 the ratio machinery mixing.The tower still does not heat.The oil refinery dry gas treatment capacity is 1.75h
-1, ethylene content is 16 moles of % in the dry gas, 1. dry gas through feeding C-01 by reaction zone below, 3. benzene through feeding C-01 by the reaction zone top, tail gas behind condenser E-01 by 7. discharging, the extraction through at the bottom of of alkylate ethylbenzene 8. by tower.Benzene feed/alkene mol ratio 6, outer circulation amount are 3 times of tower still produced quantity.System pressure 2.0MPa, temperature of reaction 140-180 ℃.Device moved through 480 hours, stable operation, and respond well, the average ethylene transformation efficiency is 91.4 moles of %, average ethylbenzene selectivity is 92.4 moles of %.The catalysis absorption technique of embodiment 2 outer circulation band catalyticreactors
Equipment used, material, operation steps and operational condition are all described with embodiment 1 in the present embodiment, exception be in external circulating device, to comprise fixed-bed reactor, identical catalyzer in interior dress 50g and the catalysis absorption tower.Device is stable through 480 hours operations, and effect is fine, and the average ethylene transformation efficiency is 95.2 moles of %, and average ethylbenzene selectivity is 92.4 moles of %.Catalysis absorption/the distil process of embodiment 3 outer circulation band catalyticreactors
In the present embodiment, the tower diameter of catalysis absorption/distillation tower (C-01) is φ 50mm, tower height 4m, wherein stripping section high 1 meter (only adorning structured packing).Dress 1350g HY-BE type beta-zeolite catalyst in the catalysis absorber portion, catalyzer is the cylindricality particle of φ 1.5, is contained on the tower tray of jet-type member.750g catalyzer of the same race is housed in the fixed-bed reactor in the external circulating device (C-02).The dry gas treatment capacity is 1.75h
-1, ethylene content is 14-20% in the dry gas, benzene/ethylene feed mol ratio is 6-8.The outer circulation amount is 1-3 a times of tower still produced quantity, and the liquid total reflux that condensation is got off in the tail gas condenser enters in the tower, and the overhead liquid specific liquid rate is 8-12m
3/ m
2H.System pressure is 2.0MPa, and temperature of reaction is 140-180 ℃.Device turned round through 2000 hours, stable operation, and the effect excellence, the average ethylene transformation efficiency is 95.6 moles of %, average ethylbenzene selectivity is 98.6 moles of %.The catalysis absorption technique of comparative example's 1 no outer circulation
Equipment used, material, operation steps and operational condition are all described with embodiment 1 in the present embodiment, exception be not use outer circulation.At this moment, the average ethylene transformation efficiency is 95.7 moles of %, but average ethylbenzene selectivity has only 87.9 moles of %, and catalyst activity prolongs the trend of significantly decreasing in time.For example after running in 240 hours, conversion of ethylene drops to 92.8 moles of % by 98.1 moles of %, and ethylbenzene selectivity remains unchanged substantially.
Claims (11)
1. the catalysis absorption process with the band outer circulation is handled the catalysis absorption process of the mixed gas contain rare reactant, this method is carried out in a catalysis absorption tower, the catalysis absorption tower comprises a catalysis absorber portion, a tail gas condensation reflux device, with an optional hydrops groove, stripping section and tower still reboiler, filler and catalyzer are housed in the catalysis absorber portion, pending mixed gas and liquid reactant charging are respectively under the bottom of catalysis absorber portion and its top feed, the catalysis absorber portion of flowing through opposite to each other, discharge after the condensation of cat head tail gas condensation reflux device through reacted tail gas, liquid reaction mixture by tower at the bottom of discharging, it is characterized in that, extract the operative liquid reaction mixture from catalysis absorber portion bottom and turn back to top, catalysis absorption tower, and enter in the catalysis absorber portion through a cover external circulating device.
2. according to the method for claim 1, it is characterized in that the liquid reaction mixture amount of outer circulation was at least 1: 1 with ratio by the liquid reaction mixture amount of extraction in the tower.
3. according to the method for claim 2, it is characterized in that said ratio is 2: 1-5: 1.
4. according to the method for claim 3, it is characterized in that, in external circulating device, set up fixed-bed reactor, made before the liquid reaction mixture of outer circulation is entering into catalysis absorber portion top through further catalyzed reaction.
5. according to each method among the claim 1-4, it is characterized in that, also comprise hydrops groove, stripping section and a tower still reboiler that is positioned under the catalysis absorber portion in the catalysis absorption tower, at this moment, make mixed gas from the stripping section charging, divide the liquid reactions mixture to make it outer circulation from the effusive liquid reacting product of catalysis absorber portion through hydrops groove extraction unit and return catalysis absorber portion top, all the other liquid reaction mixtures enter stripping section, from tower still bottom extraction liquid reacting product.
6. according to the method for claim 5, it is characterized in that the said mixed gas that contains rare reactant is an oil refinery dry gas, liquid reactants is a benzene.
7. according to the method for claim 6, it is characterized in that the service temperature on catalysis absorption tower is 140-200 ℃, pressure is (1.5-3.0) MPa, and the liquid/gas reactant molar ratio is 2: 1-12: 1, use HY-BE type beta-zeolite type catalyzer.
8. a catalysis absorption equipment mixed gas that is used to handle contain rare reactant, the band outer circulation, it comprises a catalysis absorber portion, a tail gas condensation reflux device, filler and catalyzer are housed in the catalysis absorption tower, it is characterized in that between the top of catalysis absorber portion and bottom, also having the external circulating device that a cover is used for liquid reaction mixture is turned back to from this section bottom this section top.
9. equipment according to Claim 8 is characterized in that, disposes a fixed bed catalytic reactor in external circulating device.
10. according to Claim 8 or 9 equipment, it is characterized in that, under the catalysis absorber portion, also dispose a hydrops groove, a stripping section and a tower still reboiler.
11. the purposes of each equipment according to Claim 8-10 is used to handle the mixed gas that contains rare reactant.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 00134819 CN1192081C (en) | 2000-12-04 | 2000-12-04 | Method and apparatus for treating mixed gas containing dilute reactant |
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| Application Number | Priority Date | Filing Date | Title |
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| CN 00134819 CN1192081C (en) | 2000-12-04 | 2000-12-04 | Method and apparatus for treating mixed gas containing dilute reactant |
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| CN1357601A true CN1357601A (en) | 2002-07-10 |
| CN1192081C CN1192081C (en) | 2005-03-09 |
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| CN 00134819 Expired - Lifetime CN1192081C (en) | 2000-12-04 | 2000-12-04 | Method and apparatus for treating mixed gas containing dilute reactant |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103776040A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Method for catalytic oxidation treatment of refinery dry gas |
-
2000
- 2000-12-04 CN CN 00134819 patent/CN1192081C/en not_active Expired - Lifetime
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103776040A (en) * | 2012-10-24 | 2014-05-07 | 中国石油化工股份有限公司 | Method for catalytic oxidation treatment of refinery dry gas |
| CN103776040B (en) * | 2012-10-24 | 2015-11-18 | 中国石油化工股份有限公司 | A kind for the treatment of by catalytic oxidation of oil refinery dry gas |
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| Publication number | Publication date |
|---|---|
| CN1192081C (en) | 2005-03-09 |
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Correction item: Co-applicant Correct: Beijing Institute of Fashion Technology|Institute of Jinling Branch of China Petroleum & Chemical Corporation|Tianjin New Tianjin Technology and Development Co., Ltd.|East China University of Science and Technology|Shanghai Medicine Industry Design Institute of Sinopec Group False: Beijing Institute of Fashion Technology|China Petroleum Chemical Co Jinling Branch Number: 28 Page: The title page Volume: 18 |
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| CI01 | Correction of invention patent gazette |
Correction item: Co-applicant Correct: Beijing Institute of Fashion Technology|Institute of Jinling Branch of China Petroleum & Chemical Corporation|Tianjin New Tianjin Technology and Development Co., Ltd.|East China University of Science and Technology|Shanghai Medicine Industry Design Institute of Sinopec Group False: Beijing Institute of Fashion Technology|China Petroleum Chemical Co Jinling Branch Number: 28 Volume: 18 |
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| CI02 | Correction of invention patent application |
Correction item: Co-applicant Correct: Beijing Institute of Fashion Technology|Institute of Jinling Branch of China Petroleum & Chemical Corporation|Tianjin New Tianjin Technology and Development Co., Ltd.|East China University of Science and Technology|Shanghai Medicine Industry Design Institute of Sinopec Group False: Beijing Institute of Fashion Technology|China Petroleum Chemical Co Jinling Branch Number: 28 Page: The title page Volume: 18 |
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Free format text: CORRECT: CO-APPLICANT; FROM: BEIJING DRESS COLLEGE CHINA PETROLEUM + CHEMICAL CORPORATION JINLING BRANCH TO: BEIJING DRESS COLLEGE SINOPEC JINLING BRANCH RESEARCH INSTITUTE TIANJIN CITY XINTIANJIN SCIENCE DEVELOPMENT CO., LTD. EAST CHINA UNIVERSITY OF SCIENCE AND TECHNOLOGY SINOPEC SHANGHAI MEDICAL INDUSTRY ... |
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