CN105001185A - Maleic anhydride tail gas treatment equipment and maleic anhydride tail gas treatment process - Google Patents
Maleic anhydride tail gas treatment equipment and maleic anhydride tail gas treatment process Download PDFInfo
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- C07D307/00—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom
- C07D307/02—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings
- C07D307/34—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
- C07D307/56—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
- C07D307/60—Two oxygen atoms, e.g. succinic anhydride
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
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- B—PERFORMING OPERATIONS; TRANSPORTING
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- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
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Abstract
The invention relates to maleic anhydride tail gas treatment equipment, which comprises an air compressor, a maleic anhydride reactor, a gas cooler, a maleic anhydride absorption tower, a burning furnace, a maleic anhydride desorption tower, a lean oil flash evaporation tower, a tail gas washing tower, a gas flow distributor, a moisturizing device, a tail gas deacidification device and a gas-liquid separator, wherein the devices are connected through pipelines, the gas flow distributor comprises an inlet and at least three outlets, the inlet is connected with the tail gas outlet of the maleic anhydride absorption tower, the first outlet is connected with the moisturizing device, the second outlet is connected with the burning furnace, and the third outlet is connected with the tail gas washing tower. The present invention further provides a tail gas treatment process using the treating equipment. Compared with the equipment and the process in the prior art, the equipment and the process of the present invention have the following characteristics that n-butane, maleic anhydride and the maleic anhydride absorption solvent in the tail gas are reused at a maximum. In addition, the condenser with a condensate discharge port is used and the acid organic compounds in the tail gas are eluted by a lot of water vapor carried by the tail gas so as to reduce the equipment investment cost and the produced waste acid water.
Description
Technical field
The present invention relates to a kind of n butane oxidation legal system cis-butenedioic anhydride tail gas treatment process, particularly relate to a kind of cis-butenedioic anhydride tail gas deacidification equipment and a kind of cis-butenedioic anhydride tail gas treatment process.
Background technology
Cis-butenedioic anhydride is the third-largest acid anhydrides being only second to aceticanhydride and phthalic anhydride in the world, is widely used in the aspects such as synthetic resins, coating, agricultural chemicals, lubricating oil additive, medicine, paper treating agent, foodstuff additive and stablizer, has extremely wide application prospect.Owing to structure existing many features, cis-butenedioic anhydride has very strong reactivity worth, unsaturated polyester resin (UPR), Synolac etc. can be synthesized, it is again preparation 1, the raw material of the serial organic chemistry such as 4-butyleneglycol (BDO), tetrahydrofuran (THF) (THF) and fine chemicals is one of important chemical intermediate.2013, China Maleic Anhydrite throughput reached 172.9 ten thousand tons/year, and expecting cis-butenedioic anhydride annual output in 2015 will more than 1,800,000 ton.
Divide with raw material, the production method of cis-butenedioic anhydride mainly contains benzene method and normal butane method.China's maleic anhydride production is based on benzene method, but normal butane method has, and environmental pollution is little, carbon atom utilization ratio is high, raw material sources are extensive and the advantage such as cheap, in addition the environmental problem that China's purified petroleum benzin price is surging and increasingly serious in recent years, so normal butane method is extensively concerned.Along with China is in the operation of building normal butane method maleic anhydride unit, normal butane method cis-butenedioic anhydride is just entering the fast-developing phase.
The reaction of selective oxidation of n-butane cis-butenedioic anhydride is carried out in fixed bed cis-butenedioic anhydride reactor or fluidized-bed cis-butenedioic anhydride reactor, and catalyzer is vpo catalyst, and oxygenant is generally cheap air, also can be oxygen-rich air or pure oxygen.Normal butane and air react and are converted into cis-butenedioic anhydride in cis-butenedioic anhydride reactor, and transformation efficiency is generally 82% ~ 90%, and corresponding selection is 55% ~ 72%.After cooling, be sent to maleic anhydride absorption tower from cis-butenedioic anhydride reactor out reaction gas, reaction gas and the reverse contact mass transfer of cis-butenedioic anhydride absorption agent in maleic anhydride absorption tower, absorption agent is generally bialkyl ortho phthalate class, naphthenic acid esters class or its mixed solvent.In maleic anhydride absorption tower operating process, often produce one ton of cis-butenedioic anhydride, tower top tail gas will because of the cis-butenedioic anhydride absorption agent of gas entrainment loss 4kg (for dibutyl phthalate DBP), and when solvent consumption raises extremely in process of production, have and the highest daily consumption of solvent occurs even more than 2 tons, economic daily consumption increases unit up to ten thousand.The typical case of maleic anhydride absorption tower tower top tail gas forms as shown in table 1 below.Current most industry process this part tail gas is directly sent to incinerator burn, the heat of generation for the production of steam, then emptying.
Table 1 typical normal butane legal system maleic anhydride process maleic anhydride absorption tower tower top tail gas forms
Can find that the tail gas that cis-butenedioic anhydride absorption operation produces has following characteristics by table 1: (1) tail is large-minded, the tail gas of the maleic anhydride production device generation of cis-butenedioic anhydride annual production 20000 tons is up to about 80000kg/h; (2) the unreacted normal butane still containing 0.61% (massfraction, lower same) in tail gas, accounts for total hydrocarbon charging 17%; (3) the cis-butenedioic anhydride lyosorption DBP still containing 0.01% in tail gas, accounts for 30% of solvent total losses amount; (4) a large amount of water vapour is contained in tail gas; (5) in tail gas, oxygen content still accounts for 15.46%, can serve as oxygenant.Therefore, for the maleic anhydride production technology that cis-butenedioic anhydride product cost about 50% is expense of raw materials, if this part tail gas is directly burnt, not only can reduce the utilization ratio of raw material normal butane, strengthen the loss amount of cis-butenedioic anhydride lyosorption, increase maleic anhydride production cost, but also the load of incinerator can be increased, produce a large amount of greenhouse gases, to environment.
In order to more reasonably process this part tail gas, many patent documentations (such as US 3899516, US3904652, US 4222945, US 4342699, US 5011945) provide a kind of circulation of tail gas utilize method, but these technology generally use pure oxygen or oxygen-enriched stream, the commercial run making oxygenant from use air is significantly different, and exhaust gas processing device is complicated, cost of investment is large, and income is not high, and for the production equipment operated, these exhaust gas circulation process are difficult to undergo technological transformation to it.Also patent documentation (as US 4231943 etc.) report is had to use air to do the circulation of tail gas technology of oxygenant in addition, but be limited to the intrinsic thinking of typical industrial processes, this process feeds oxygen concentration is lower, concentration of n-butane is very high, its transformation efficiency is 20% ~ 40%, but the waste that high concentration of n-butane charging and discharging easily cause normal butane is larger, in addition in actual production process a large amount of rare gas element (as N
2or Ar) can accumulate gradually, need constantly to shift out from tail gas.In order to overcome these defects, US 4231943 proposes to use absorbent charcoal adsorber to carry out unreacted normal butane in adsorption selection tail gas, then desorb normal butane under suitable operational condition, but device complicated operation, and vent gas treatment amount is very large, causes processing costs very high.
Compare above patent, patent documentation US 6040460 proposes a kind of realistic plan, only by partial tail gas after extracting tower depickling directly and air mixed enter cis-butenedioic anhydride reactor, and Conser exhaust gas circulation process successful operation corresponding with it for many years, its concrete operations are 40% cyclically utilizing maleic anhydride absorption tower being absorbed tail gas after cis-butenedioic anhydride, rest part is directly sent to incinerator and burns, 40% tail gas is sloughed after organic acid through extracting tower and is sent into air compressor two sections of entrances, mix with from air compressor one section outlet fresh air, then gas mixture and normal butane are mixed into cis-butenedioic anhydride reactor reaction by a certain percentage.This exhaust gas circulation process can make full use of maleic anhydride absorption tower tail gas pressure, and reduces compressor shaft power to reach energy-conservation object.But because tail gas is large-minded, but also with acidity, which results in extracting tower equipment comparatively large and need protection against corrosion, the introducing of extra de-acidying agent water simultaneously creates a large amount of acid waste water, and the not treated direct burning of the tail gas of 60%, both cause a large amount of unreacted normal butane in tail gas to be still underutilized, and also cause tail gas owing to carrying caused solvent loss secretly.Therefore, cis-butenedioic anhydride circulation of tail gas technology also has very large room for promotion.
Summary of the invention
The invention discloses a kind of cis-butenedioic anhydride tail gas treatment device and technique thereof, this technique can improve n butane oxidation yield, reduces cis-butenedioic anhydride lyosorption consumption, reduces the quantity discharged of depickling waste water.
The present invention for the taked technical scheme that achieves the above object is:
A kind of cis-butenedioic anhydride exhaust gas processing device, comprise the air compressor, cis-butenedioic anhydride reactor, gas cooler, maleic anhydride absorption tower, incinerator, cis-butenedioic anhydride desorption tower, oil-poor flashing tower, tail gas washing tower, gas flow divider, humidifying device, tail gas depickling device, the gas-liquid separator that are connected by pipeline, described gas flow divider comprises import and at least three outlets, its import is connected to the offgas outlet of maleic anhydride absorption tower, its first outlet is connected to humidifying device, second outlet is connected to incinerator, and the 3rd outlet is connected to tail gas washing tower.
In the present invention, by gas flow divider, maleic anhydride absorption tower tail gas is divided into washing, circulation, burning three strands of air-flows, farthest can reclaims the normal butane in tail gas and cis-butenedioic anhydride lyosorption, reduce production cost.
As preferably, the offgas outlet of described tail gas washing tower is connected to incinerator, discharged to air after fully burning.
As preferably, described cis-butenedioic anhydride reactor is the one in fixed bed cis-butenedioic anhydride reactor, fluidized-bed cis-butenedioic anhydride reactor, circulating fluidized bed cis-butenedioic anhydride reactor, is preferably fixed bed cis-butenedioic anhydride reactor.
As preferably, described tail gas depickling device is the condenser being provided with condensate discharge mouth.
As preferably, described tail gas washing tower is dynamic wave scrubbing tower.
In order to obtain better technique effect, the present invention additionally provides a kind of tail gas treatment process using aforesaid device simultaneously, comprises the following steps:
(1) Feedstock treating: fresh air and recycled offgas are mixed into air compressor through the second mixing tank.Cis-butenedioic anhydride reactor feed air-flow is mixed to form by a certain percentage from air compressor air-flow out and normal butane.
(2) react: feed stream is introduced cis-butenedioic anhydride reactor, normal butane wherein reacts and generates cis-butenedioic anhydride under the effect of catalyzer.
(3) absorption and desorption: reclaim heat through gas cooler cooling from cis-butenedioic anhydride reactor reaction gas out, at the bottom of tower, maleic anhydride absorption tower is introduced after cooling, contact with the solvent counter current entered from maleic anhydride absorption tower top and carry out mass transfer, reclaim cis-butenedioic anhydride wherein, the rich oil containing cis-butenedioic anhydride at the bottom of tower is sent to cis-butenedioic anhydride desorption tower solution sucking-off cis-butenedioic anhydride, crude maleic anhydride product side line output.Oil-poorly at the bottom of cis-butenedioic anhydride desorption tower tower be sent to oil-poor flashing tower, reclaim further oil-poor in the cis-butenedioic anhydride that comprises.
(4) vent gas treatment: maleic anhydride absorption tower tail gas is divided into portion washes, component loops through gas flow divider, part burns three strands of air-flows, and wherein portion washes air-flow converges with cis-butenedioic anhydride desorption tower tail gas, oil-poor flashing tower tail gas and enters tail gas washing tower; Component loops air-flow with mend humectant be thoroughly mixed to form mixed flow in humidifying device, mend the amount of humectant and determined by recycled offgas content, to guarantee all organic acids in tail gas of dissolution.Mixed flow enters the condensation of tail gas depickling device and forms liquid phase stream and vapor phase stream subsequently, wherein mend humectant and water vapor preferential condensation when mixed flow condensation, mend in humectant and water to guarantee that the organic acid that subsequent condensation is got off and acid anhydrides etc. are dissolved in, with after through condensate discharge mouth discharge out-of-bounds, vapor phase stream is mixed into air compressor with fresh air and recycles after gas-liquid separation; Part burns airflow feeding toward incinerator, and in air-flow, normal butane, carbon monoxide and other organism and oxygen Thorough combustion, after off-gas recovery heat, enter air.
The transformation efficiency that cis-butenedioic anhydride reacts, selectivity and yield depend on catalyzer and reaction conditions, especially cis-butenedioic anhydride reactor feed composition, temperature, pressure and air speed.In order to obtain better technique effect, further improving and optimized choice has been made to reaction conditions.
As preferably, the shunting volume accounting (accounting for the ratio of tail gas cumulative volume) of described maleic anhydride absorption tower tail gas is: component loops air-flow accounts for 10 ~ 50%, portion washes air-flow accounts for 0 ~ 40%, part is burned air-flow and accounted for 10 ~ 90%.Namely, in the tail gas that above-mentioned maleic anhydride absorption tower ejects, 10% ~ 50% enters the whole normal butane of described tail gas washing tower reuse and oxygen as recycled offgas, 0 ~ 40% enters described tail gas purification tower recycling design and part normal butane as cleaning of off-gas, and rest part is sent to incinerator and burns recovery heat.Show after deliberation, the distribution of aforementioned proportion can farthest unreacted normal butane and cis-butenedioic anhydride lyosorption in reuse tail gas, and does not affect existing maleic anhydride production index, and therefore, the present invention adopts aforementioned proportion to the distribution of tail gas.
As preferably, interpolation and the mixing of described benefit humectant complete in humidifying device, described benefit humectant and cis-butenedioic anhydride, dissolve each other, with normal butane indissoluble along acid, fumaric acid, acetic acid, vinylformic acid.
As preferably, described benefit humectant is de-salted water, in described maleic anhydride absorption tower, absorption agent used is one in bialkyl ortho phthalate class, hexahydrobenzene dioctyl phthalate dialkyl esters or its mixed solvent, be preferably dibutyl phthalate or hexahydrobenzene dibutyl carboxylic acid, the washing composition in described tail gas washing tower is identical with the absorption agent in maleic anhydride absorption tower.
As preferably, the washing composition temperature in described tail gas washing tower is 10 ~ 50 DEG C, and the catalyzer used in described cis-butenedioic anhydride reactor is vanadium composite phosphorus oxide catalyzer (vpo catalyst).
Why the present invention selects part circulation of tail gas, is that under suitable anaerobic conditions, the selectivity in reaction can improve, and the anaerobic environment that the introducing of suitable recycled offgas causes can improve selectivity thus cause yield to improve because find through experiment.And too much recycled offgas enters the process of reacting again and can reduce butanes conversion too much thus reduce yield, and then production intensity declines greatly, therefore, must enter incinerator by partial tail gas, and partial tail gas enters reaction process again as recycled offgas.
Compared with prior art, the present invention takes tail gas component loops, portion washes, part is burned, under the prerequisite not affecting existing industrial production index, and normal butane and cis-butenedioic anhydride lyosorption in reuse tail gas to greatest extent.Invention increases tail gas portion washes technique, not only reclaimed product cis-butenedioic anhydride in tail gas by tail gas washing tower, and reclaimed cis-butenedioic anhydride lyosorption in tail gas, so greatly reduce maleic anhydride absorption tower solvent-oil ratio.In addition, the tail gas depickling device that the present invention adopts is not board-like maleic anhydride absorption tower of the prior art or filler maleic anhydride absorption tower, but with the condenser of condensate discharge mouth, the Acidic organic matter in tail gas by a large amount of water vapour wash-outs of carrying in tail gas, the spent acid water yield that reduces facility investment expense and produce.
Accompanying drawing explanation
Fig. 1 is the process flow sheet of traditional not hot tail gas circulation.
Fig. 2 is the process flow sheet of conventional belt circulation of tail gas.
Fig. 3 is present invention process schema.
Embodiment
Below in conjunction with accompanying drawing and concrete case study on implementation, the invention will be further described.
Implement operating mode 1: the process flow sheet taking Fig. 1, Fig. 1 as traditional not hot tail gas circulation, air 1 mixes with normal butane 4 through air compressor 2; Mixing raw material gas 5 enters cis-butenedioic anhydride reactor 6 and reacts, and reaction conditions is: 420 DEG C, 0.19MPa, 1560h
-1; Maleic anhydride absorption tower 10 is entered through gas cooler 8 cooling from cis-butenedioic anhydride reactor 6 reaction gas 7 out, in maleic anhydride absorption tower 10, in reaction gas, product cis-butenedioic anhydride is absorbed, maleic anhydride absorption tower tower top tail gas 11 is sent to incinerator 14, and rich solution 12 at the bottom of maleic anhydride absorption tower tower is sent to cis-butenedioic anhydride desorption tower 15 desorb; The thick anhydride product 18 of cis-butenedioic anhydride desorption tower 15 side line output, cis-butenedioic anhydride desorption tower tower base solvent 17 is sent to oil-poor flashing tower 19 further cis-butenedioic anhydride in recycling design, and oil-poor flashing tower overhead gas 20 and cis-butenedioic anhydride desorption tower tower top tail gas 16 converge and enters tail gas washing tower 23 and reclaim the cis-butenedioic anhydride that tail gas carries further; Tail gas washing tower overhead gas 24 emptying, tail gas washing tower tower base solvent 25 is sent to maleic anhydride absorption tower 10 and absorbs cis-butenedioic anhydride.
Implement operating mode 2: the process flow sheet taking Fig. 2, Fig. 2 as conventional belt circulation of tail gas.With operating mode 1 difference, this operating mode increases exhaust gas circulation process newly, and concrete operations flow process is that 40% of maleic anhydride absorption tower tower top tail gas 11 is recycled, and all the other are sent to incinerator 14; Component loops air-flow 29 enters tail gas extracting tower through tail gas heat exchanger heat exchange, laggard toward air compressor 2 entrance through gas-liquid separator gas-liquid separation from tail gas extracting tower gas out.The solvent that this technique deacidification uses is water, and deacidification equipment is packing tower or tray column.
Implement operating mode 3: be flow process figure of the present invention for Fig. 3, Fig. 3.Wherein cis-butenedioic anhydride desorption tower 15, the top exhaust port of oil-poor flashing tower 19 is connected with tail gas washing tower 23 through pipeline, maleic anhydride absorption tower top tail gas 11 is communicated with humidifying device 32 by gas flow divider 27 simultaneously, tail gas washing tower 23, incinerator 14, described humidifying device 32 is through pipeline communication tail gas depickling device 34, gas-liquid separator 38, the bottom of described tail gas depickling device 34 has condensate discharge mouth 35, the upper gas outlet of described gas-liquid separator 38 has the second mixing tank through pipeline communication, described second mixing tank has fresh air inlet, described second mixing tank is through pipeline communication air compressor 2, described tail gas washing tower 23 is connected with incinerator 14 through pipeline.
With operating mode 1, 2 differences, tail gas 11 is divided into component loops by this operating mode, portion washes, part burns three strands of air-flows, and tail gas component loops deacidification equipment is the condenser with condensate discharge mouth, concrete operations flow process is that maleic anhydride absorption tower tail gas 11 splits into 40% cycling stream stock by gas flow divider 27, 40% scrub stream stock, 20% burns three fluid streams such as stream stock, wherein the part of 20% is burned air-flow 28 and is sent directly to incinerator 14 burning recovery heat, the portion washes air-flow 30 of 40% and cis-butenedioic anhydride desorption tower 15, the tower top tail gas of oil-poor flashing tower 19 converges and is sent to tail gas washing tower 23 and washs, tail gas washing tower 23 is dynamic wave scrubbing tower, then deliver to incinerator 14 and burn recovery heat.All the other 40% component loops air-flows 29 fully mix in humidifying device 32 with benefit humectant 31, mixed flow 33 condensation in tail gas depickling device 34 forms liquid phase stream 36 and vapor phase stream 37, humectant and water vapor preferential condensation is mended when mixed flow 33 condensation, mend in humectant and liquid water to guarantee that the organic acid that subsequent condensation is got off and acid anhydrides etc. are dissolved in, discharge out-of-bounds through condensate discharge mouth 35 subsequently.From tail gas depickling device 34 vapor phase stream 37 out through gas-liquid separator 38 gas-liquid separation, be mixed into air compressor from gas-liquid separator gas phase 39 out with fresh air and recycle.The benefit humectant 31 that this technological process uses is de-salted waters, and deacidification equipment is the condenser with liquid discharge outlet.
For annual output of maleic anhydride up to 20,000 t technical scale, carry out analog calculation to three kinds of operating modes, partial results is as follows:
Table 2 operating mode 2 and the contrast of operating mode 3 deacidification effect
Raw material consumption amount under the different operating mode of table 3
In addition, in order to study further and optimize reaction, for the equipment implementing operating mode 3, applicant has also carried out following different embodiment.
By finding out in above embodiment, operating mode 2 and operating mode 3 acid treatment effect basically identical, all can meet the acidproof requirement of air compressor.The present invention's (operating mode 3) is compared with exhaust gas circulation process (operating mode 2) advanced at present, annual cis-butenedioic anhydride lyosorption loss amount reduces 48 tons, normal butane consumption decreases 40 tons, wastewater flow rate decreases 2008 tons, and the investment of operating mode 3 deacidification equipment is fewer than operating mode 2 in addition.Therefore, the present invention is more with the obvious advantage than traditional technology.
Claims (10)
1. a cis-butenedioic anhydride exhaust gas processing device, comprise the air compressor (2) connected by pipeline, cis-butenedioic anhydride reactor (6), gas cooler (8), maleic anhydride absorption tower (10), incinerator (14), cis-butenedioic anhydride desorption tower (15), oil-poor flashing tower (19), tail gas washing tower (23), gas flow divider (27), humidifying device (32), tail gas depickling device (34), gas-liquid separator (38), it is characterized in that, described gas flow divider (27) comprises import and at least three outlets, its import is connected to the offgas outlet of maleic anhydride absorption tower (10), its first outlet is connected to humidifying device (32), second outlet is connected to incinerator (14), 3rd outlet is connected to tail gas washing tower (23).
2. a kind of cis-butenedioic anhydride exhaust gas processing device according to claim 1, is characterized in that, the offgas outlet of described tail gas washing tower (23) is connected to incinerator (14).
3. a kind of cis-butenedioic anhydride exhaust gas processing device according to claim 2, is characterized in that, described cis-butenedioic anhydride reactor (6) is fixed bed cis-butenedioic anhydride reactor, one in fluidized-bed cis-butenedioic anhydride reactor, circulating fluidized bed cis-butenedioic anhydride reactor.
4. a kind of cis-butenedioic anhydride exhaust gas processing device according to claim 2, is characterized in that, described tail gas depickling device (34) is for being provided with the condenser of condensate discharge mouth.
5. a kind of cis-butenedioic anhydride exhaust gas processing device according to claim 2, is characterized in that, described tail gas washing tower (23) is dynamic wave scrubbing tower.
6. a kind of cis-butenedioic anhydride tail gas treatment process of a kind of cis-butenedioic anhydride exhaust gas processing device described in any one of claim 1 to 5, comprise the following steps: Feedstock treating, reaction, absorption and desorption, vent gas treatment, it is characterized in that, in described vent gas treatment step, maleic anhydride absorption tower tail gas (11) is divided into portion washes, component loops through gas flow divider (27), part burns three strands of air-flows, and wherein portion washes air-flow (30) converges with cis-butenedioic anhydride desorption tower tail gas (16), oil-poor flashing tower tail gas (20) and enters tail gas washing tower (23); Component loops air-flow (29) enters tail gas depickling device (34) after mixing in humidifying device (32) with benefit humectant (31); Part is burned air-flow (28) and is sent to incinerator (14).
7. a kind of cis-butenedioic anhydride tail gas treatment process according to claim 6, it is characterized in that, the shunting volume accounting of described maleic anhydride absorption tower tail gas (11) is: component loops air-flow (29) accounts for 10 ~ 50%, portion washes air-flow (30) accounts for 0 ~ 40%, partly burning air-flow (28) accounts for 10 ~ 90%.
8. a kind of cis-butenedioic anhydride tail gas treatment process according to claim 6, it is characterized in that, interpolation and the mixing of described benefit humectant (31) complete in humidifying device (32), and described benefit humectant (31) is dissolved each other, with normal butane indissoluble with cis-butenedioic anhydride, suitable acid, fumaric acid, acetic acid, vinylformic acid.
9. a kind of cis-butenedioic anhydride tail gas treatment process according to claim 8, it is characterized in that, described benefit humectant (31) is de-salted water, and in described maleic anhydride absorption tower (10), absorption agent used is one in bialkyl ortho phthalate class, hexahydrobenzene dioctyl phthalate dialkyl esters or its mixed solvent; Washing composition in described tail gas washing tower (23) is identical with the absorption agent in maleic anhydride absorption tower (10).
10. a kind of cis-butenedioic anhydride tail gas treatment process according to claim 9, it is characterized in that, washing composition temperature in described tail gas washing tower (23) is 10 ~ 50 DEG C, and the catalyzer used in described cis-butenedioic anhydride reactor (6) is vanadium composite phosphorus oxide catalyzer.
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| CN108426242A (en) * | 2018-04-17 | 2018-08-21 | 上海四方锅炉集团工程成套股份有限公司 | A kind of maleic anhydride waste gas burning process and boiler system |
| CN108452639A (en) * | 2017-12-26 | 2018-08-28 | 陈卓 | The heat recovery and nmp solvent recovery method and device of a kind of lithium battery coating machine exhaust |
| CN108727313A (en) * | 2018-08-21 | 2018-11-02 | 宁波浙铁江宁化工有限公司 | The examination reaction system of cis-butenedioic anhydride |
| CN108752297A (en) * | 2018-08-21 | 2018-11-06 | 宁波浙铁江宁化工有限公司 | Cis-butenedioic anhydride tries the recovery and processing system of reactor product |
| CN108786683A (en) * | 2018-08-21 | 2018-11-13 | 宁波浙铁江宁化工有限公司 | The examination reaction unit of cis-butenedioic anhydride |
| CN111603896A (en) * | 2020-06-03 | 2020-09-01 | 中建安装集团有限公司 | Environment-friendly device and process for recovering maleic anhydride by using efficient solvent |
| CN112028863A (en) * | 2020-07-28 | 2020-12-04 | 中建安装集团有限公司 | Energy-saving device and process based on multistage condensation and two-stage absorption integrated separation of maleic anhydride |
| CN114100167A (en) * | 2021-11-26 | 2022-03-01 | 郑朝生 | Energy-saving maleic anhydride absorption deep analysis refining process |
| CN114749110A (en) * | 2022-04-18 | 2022-07-15 | 中建安装集团有限公司 | Maleic anhydride production device and method for tail gas resource utilization |
| CN115487753A (en) * | 2021-06-18 | 2022-12-20 | 济南隆凯能源科技有限公司 | Method and device for preparing acid anhydride by partial oxidation of hydrocarbon with variable-concentration feed |
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| CN107042054A (en) * | 2017-03-27 | 2017-08-15 | 南京工业大学 | Treatment method of aldehyde waste gas |
| CN108452639A (en) * | 2017-12-26 | 2018-08-28 | 陈卓 | The heat recovery and nmp solvent recovery method and device of a kind of lithium battery coating machine exhaust |
| CN108426242A (en) * | 2018-04-17 | 2018-08-21 | 上海四方锅炉集团工程成套股份有限公司 | A kind of maleic anhydride waste gas burning process and boiler system |
| CN108426242B (en) * | 2018-04-17 | 2023-11-10 | 上海四方锅炉集团工程成套股份有限公司 | Maleic anhydride waste gas incineration process and boiler system |
| CN108786683B (en) * | 2018-08-21 | 2023-10-03 | 宁波浙铁江宁化工有限公司 | Maleic anhydride test reaction device |
| CN108786683A (en) * | 2018-08-21 | 2018-11-13 | 宁波浙铁江宁化工有限公司 | The examination reaction unit of cis-butenedioic anhydride |
| CN108752297B (en) * | 2018-08-21 | 2023-10-03 | 宁波浙铁江宁化工有限公司 | Recovery processing system of maleic anhydride test reaction product |
| CN108752297A (en) * | 2018-08-21 | 2018-11-06 | 宁波浙铁江宁化工有限公司 | Cis-butenedioic anhydride tries the recovery and processing system of reactor product |
| CN108727313B (en) * | 2018-08-21 | 2023-10-31 | 宁波浙铁江宁化工有限公司 | Maleic anhydride test reaction system |
| CN108727313A (en) * | 2018-08-21 | 2018-11-02 | 宁波浙铁江宁化工有限公司 | The examination reaction system of cis-butenedioic anhydride |
| CN111603896A (en) * | 2020-06-03 | 2020-09-01 | 中建安装集团有限公司 | Environment-friendly device and process for recovering maleic anhydride by using efficient solvent |
| CN112028863A (en) * | 2020-07-28 | 2020-12-04 | 中建安装集团有限公司 | Energy-saving device and process based on multistage condensation and two-stage absorption integrated separation of maleic anhydride |
| CN115487753A (en) * | 2021-06-18 | 2022-12-20 | 济南隆凯能源科技有限公司 | Method and device for preparing acid anhydride by partial oxidation of hydrocarbon with variable-concentration feed |
| CN115487753B (en) * | 2021-06-18 | 2024-08-16 | 济南隆凯能源科技有限公司 | Method and device for preparing anhydride by hydrocarbon partial oxidation of variable-concentration feed |
| CN114100167A (en) * | 2021-11-26 | 2022-03-01 | 郑朝生 | Energy-saving maleic anhydride absorption deep analysis refining process |
| CN114749110A (en) * | 2022-04-18 | 2022-07-15 | 中建安装集团有限公司 | Maleic anhydride production device and method for tail gas resource utilization |
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