CN101402018B - Method and device for removing acid in tail gas from reaction for producing 2-butyl acetate - Google Patents
Method and device for removing acid in tail gas from reaction for producing 2-butyl acetate Download PDFInfo
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- CN101402018B CN101402018B CN2008100317872A CN200810031787A CN101402018B CN 101402018 B CN101402018 B CN 101402018B CN 2008100317872 A CN2008100317872 A CN 2008100317872A CN 200810031787 A CN200810031787 A CN 200810031787A CN 101402018 B CN101402018 B CN 101402018B
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- butyl acetate
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- 238000000034 method Methods 0.000 title claims abstract description 41
- 239000002253 acid Substances 0.000 title claims abstract description 26
- DCKVNWZUADLDEH-UHFFFAOYSA-N sec-butyl acetate Chemical compound CCC(C)OC(C)=O DCKVNWZUADLDEH-UHFFFAOYSA-N 0.000 title claims abstract description 19
- GQKZRWSUJHVIPE-UHFFFAOYSA-N sec-amyl acetate Natural products CCCC(C)OC(C)=O GQKZRWSUJHVIPE-UHFFFAOYSA-N 0.000 title claims description 15
- 238000006243 chemical reaction Methods 0.000 title claims description 10
- QTBSBXVTEAMEQO-UHFFFAOYSA-N Acetic acid Chemical compound CC(O)=O QTBSBXVTEAMEQO-UHFFFAOYSA-N 0.000 claims abstract description 141
- 239000007789 gas Substances 0.000 claims abstract description 75
- 239000003513 alkali Substances 0.000 claims abstract description 25
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- 239000002904 solvent Substances 0.000 claims abstract description 11
- VXNZUUAINFGPBY-UHFFFAOYSA-N 1-Butene Chemical compound CCC=C VXNZUUAINFGPBY-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000002994 raw material Substances 0.000 claims abstract description 5
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- 238000003860 storage Methods 0.000 claims description 8
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- 238000005260 corrosion Methods 0.000 abstract description 8
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- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 abstract 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 20
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- XEEYBQQBJWHFJM-UHFFFAOYSA-N Iron Chemical compound [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 2
- VQTUBCCKSQIDNK-UHFFFAOYSA-N Isobutene Chemical compound CC(C)=C VQTUBCCKSQIDNK-UHFFFAOYSA-N 0.000 description 2
- UEEJHVSXFDXPFK-UHFFFAOYSA-N N-dimethylaminoethanol Chemical compound CN(C)CCO UEEJHVSXFDXPFK-UHFFFAOYSA-N 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
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- 239000005977 Ethylene Substances 0.000 description 1
- 241000220317 Rosa Species 0.000 description 1
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- IAQRGUVFOMOMEM-UHFFFAOYSA-N butene Natural products CC=CC IAQRGUVFOMOMEM-UHFFFAOYSA-N 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
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- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention relates to a method and a device for effectively removing acid in tail gas during the process of preparation of alcohol sec-butyl acetate by utilization of liquefied petroleum gas to be mixed with n-butene in c_4 olefin and react with an acetic acid. The method takes an alkali solution as a solvent to remove the acetic acid in released tail gas in an extracting tower during the process of production of the alcohol sec-butyl acetate by adoption of the n-butene in the liquefied petroleum gas as a raw material; the liquefied petroleum gas after removal of the acetic acid is sent into a gas-liquid settling tank again, and enters into a torch pipe network system after separation of an alkali solution; and a tail gas system of the whole device is isolated from an external device through a liquid seal which is arranged on the gas-liquid settling tank. The method and the device guarantee that the tail gas after deacidification can safely enter into a gas holder and a torch system which do not resist acetic acid corrosion, save the trouble of needing to match a newly-built torch system which resists acetic acid corrosion and the gross investment of the newly-built device.
Description
Technical field
The present invention relates to n-butene and acetic acid reaction in a kind of mixed c 4 alkene that make use of liquefied petroleum gas and prepare in the 2-butyl acetate process method and the device thereof of acid in the effective elimination tail gas.
Background technology
Acetic acid is one of important Organic Chemicals, and it is the raw material of synthetic various low-grade fatty acid esters, acetate fiber and plastics etc.It is a colourless transparent liquid, and excitant acid smell flavor is arranged, ability intense stimulus people's nose, larynx and respiratory system, contaminated environment; And it is inflammable, flash-point is 43 ℃, and its steam and air can form explosive mist, meets naked light, high temperature can cause combustion explosion; It is again the very strong organic acid of a kind of corrosivity, and the common iron and steel or even the anti-corrosion stainless steel capital are had very strong corrosiveness.
In petroleum refining or petroleum refining process, the liquefied petroleum gas of a certain amount of include mixed alkene of by-product.At present,, remove to produce the blending component of MEK, high-knock rating gasoline to the application of liquefied petroleum gas, or directly act as a fuel burn outside, secondary butyl ester is another new product that n-butene and acetic acid reaction obtained in these mixed c 4 alkene.This industrial production device can produce some gas of releasing that contain acetic acid in process of production, abbreviates acid tail gas here as.Its main source has: 1. raw material acetic acid tank and process units contain the breather valve discharging of sour intermediate storage tank; Acetic acid discharging when 2. containing pump and the heat exchanger failover maintenance of acetic acid material; A large amount of liquefied gas were carried the discharging that contains acetic gas secretly when 3. tower, reactor were jumped because of the superpressure safety valve opens; 4. install the discharging that contains acetic gas when shutting down purges in a large number.
The harmfulness of acetic acid has determined these the acid tail gas that contain acetic acid in acetic acid material device is arranged should take harmless treatment to discharge again.
Chinese patent CN1099381A discloses the method for ethene, propylene, butylene and lower fatty acid prepared in reaction low-grade fatty acid ester, and another Chinese patent CN1085652C also discloses the method for propylene, isobutene, butene-1 and butene-2 and the secondary butyl ester of lower fatty acid prepared in reaction organic acid isopropyl ester, organic acid isobutyl ester and organic acid.But above-mentioned patent is only all only introduced the production technology of low-grade fatty acid ester, process units in the production process is comprised the processing method of harmful acid tail gas that acetic acid tank produces is not but all mentioned.Other documents and materials have been mentioned following 3 kinds of methods that remove sour gas.
First kind is the size of utilizing each molecular weight of material in the gaseous mixture, and the physics mode that adopts transformation absorption or film to separate is separated sour gas from gaseous mixture.For example, from natural gas, removing the sour gas carbon dioxide promptly is to adopt this method.
Second kind is to use physical solvent from feeding gas, to remove sour gas; Generate a kind of compound of intermediate state through a large amount of sour gas and solvent reaction; When containing the solvent reclamation of intermediate state compound, make sour gas focused on the release of again again and recycle again.For example, the cracking gas of ethylene cracker and catalytic cracking unit adopts pure amine solvent to remove sour gas such as wherein hydrogen sulfide and carbon dioxide in ammonia absorber and adopts this method exactly.This respect has many patented technologies, like patent " 89103780.2 " a kind of " reclaiming improving one's methods of sour gas " is provided, and is the alkanolamine aqueous solution importing absorption sour gas with alkanolamine and regeneration; Patent " 90105652.9 " provides a kind of " method of purification of acidic gas ", is the mixed solvent that adopts tertiary amine and di-tertiary amine radical derivative and specific materials such as ester class to form, acidic components in the absorbing and removing air-flow; Patent " 92100440.0 " provides a kind of " from gaseous mixture, thoroughly removing the method for sour gas ", comprises with the regeneration of solvent absorption and solvent slop, contains dimethylethanolamine (DMEA) aqueous mixture and a kind of co-catalyst in the solvent.
The third is to adopt the water-soluble characteristic of acetic acid and remove.For example, in large-scale acetic acid tank district, to the sour gas that breather valve on the storage tank is discharged, according to acetic acid characteristics soluble in water, the employing tower internals is that the absorption tower water of filler absorbs processing, reaches and controls useless purpose.
The acid tail gas that first and second kinds of above-mentioned technology all do not include acetic acid material device removes; Though being first water, the third technology just removes the acid that contains in the acid gas as solvent; But it is to the sour gas of acetic acid tank top breather valve trace continuous, that evenly discharge, does not also relate to the processing method that ester plant contains sour tail gas.This technology adopts water treatment to contain the tail gas of acetic acid; Though can remove the acid that contains in the sour tail gas; But there is following problem in this technology: 1. be to adopt big water gaging to absorb acid, produced a large amount of sour sewage that contains in the process, sewage efflux processing; Both sank money, influenced economic benefit, again contaminated environment, influence social benefit.2. the tower treatment process of charge in adopting, its flow process and control system are complicated, and operating cost is high.3. expensive corrosion resisting stainless steel material all need be used like its tower body, inner-tower filling material etc. in the position that contacts with acetic aid medium; Cause when containing the acid gas discharging in a large number and needing to handle when considering also on device shutting down and the pressure vessel that safety valve opens to jump, the specification of equipment, pipeline will very big, and the investment of device is also just very big.4. with the absorption tower technology of filler as inner member, can not the adaptive device shutting down and pressure vessel on safety valve open when jumping, contain the pressure drop requirement of acid gas discharging in a large number.Otherwise the specification of equipment size will be very big with investment.
About containing the removal methods of sour tail gas in the 2-butyl acetate preparation section, also there is not the pertinent literature report at present.In the normal productive process, to build the investment of gas holder-flare system of acid corrosion-resistant very big for the 2-butyl acetate matched with devices separately.Often these gases after harmless treatment being discharged into existing gas holder-flare system handles.In 4 kinds of above-mentioned main acid tail gas, 1., 2. the plant sour gas comes amount not quite and more steady, and the 3., the acid tolerance of 4. planting is very big, the discharging duration is longer.Especially 3. plant sour gas and also have emergentness, and carry volume instantaneous expansion after the liquefied petroleum gas pressure release that contains acetic acid, about 250～300 times of the volumetric expansions after the gasification secretly.The flash-point of liquefied gas, boiling point are very low, and all below 0 ℃, explosive range is 1.5～11.7% (bodies), and this designing requirement to the subsequent treatment system is very high.Therefore; With the optimized design that newly-increased investment economizes most, the operation expense is minimum, three waste discharge is minimum; Utilize existing gas holder, flare system to handle these sour gas; Making the gas of discharging meet environmental sanitation and safety requirements, is to be the major issue that the 2-butyl acetate device of raw material will solve with the liquefied petroleum gas.
Summary of the invention
The acid gas of the corrosivity that the objective of the invention is to produce in the Dichlorodiphenyl Acetate Zhong Ding ester apparatus production process gets into gas holder, the flare system of existing not anti-acetic acid corrosion again through reasonably in advance after the depickling, thus the gross investment of minimizing new device.
The object of the invention can be realized through following technical measures: this method is to utilize the acid-base neutralization principle to come efficiently to remove the acetic acid in the acid liquefied petroleum gas.Selecting mass percent concentration is that 3～10% sodium hydroxide solution is as the solvent that removes sour gas in the Zhong Ding ester apparatus production process; Send into extracting tower top gravity flow and descend; Washing removes the acetic acid in the liquefied gas; Deviate from the liquefied petroleum gas of acetic acid and send into a gas-liquid settling tank again, get into the torch pipe network system again after isolating buck.
It is the internal circulating load with the required sodium hydroxide solution of variations in temperature control depickling that the present invention further improves; Said internal circulating load with the required sodium hydroxide solution of variations in temperature control depickling; Be meant that safety valve opens jumping, contain in a large number under the situation that acid gas releases; When temperature reaches setting value, strengthen the output quantity of alkali lye.
In satisfying the scope that allows the use concentration of lye, the alkali lye of tower bottom constantly is circulated in the extracting tower top entering tower and recycles.
Be realizing that said method, the present invention provide removes 2-butyl acetate and prepares the device that contains sour tail gas in the process.Comprise an extracting tower and gas-liquid settling tank; This extracting tower is that the relative direction of same axis is provided with overlapped and keeps the retaining of a determining deviation to pull in reactive site; Extracting tower bottom alkali lye is transported to the extracting tower top through pump; Baffle plate and horizontal direction angle are 15 °, and baffle plate upper edge place has a strip through-hole short slightly with baffle edge.
A reaction tower that can the reactive site of acid-base neutralization and the storage tank that stores alkali lye be united two into one, top is reactive site, the alkali lye that absorbs behind the acetic acid is stored in the extracting tower bottom.
In the embodiment of the invention, specification φ 600 * 4000/ φ 1600 * 6000 of preferred extracting tower.The reactive site of the undergauge on top is provided with at the overlapped 50～100mm of the relative direction of same axis; And keep 4～8 herringbones retaining of a determining deviation to pull, have a strip through-hole that wide a 3～6mm, length and baffle edge are lacked slightly apart from panel edges 30～50mm place along the alkali lye flow direction above it.
The present invention has established bar-shaped trough newly on baffle plate, make when alkali lye flows on each piece baffle plate, can form 2 road alkaline streams below the baffle plate, and with the alkali lye distribution comparison of existing structure form baffle plate, the chance that alkali lye contacts with sour gas has increased nearly one times.
Described gas-liquid settling tank is the storage tank that has certain water seal height, specification φ 1500 * 9000.It not only is used for the sedimentation separation extracting tower and comes the buck in the gas, keeps apart but also will install other device that links to each other with flare system, to guarantee the safe operation of this device.
The pump that makes the alkali lye circulation in the said extracting tower comprises a temperature sensor by the control of control system in this control system, and the control system is according to the output quantity of the height control pump of the temperature that records.
The bottom is to open when jumping according to safety valve in the device production process, and acid-base neutralization reacts the required storage storage tank of excess base liquid measure slightly during with the containing acid gas and release of maximum.
Technical scheme of the present invention is reasonable, adopts the baffle arrangement of mutual cross modal, and its pressure drop is little, guaranteed that the device safety valve opens the demand that the big flux of gas is released when purging of jumping or stop work suddenly, and it is simple in structure, and processing and manufacturing is easily invested very little; This has guaranteed to contain in the sour gas removing of acetic acid material; The caustic alkali that adopts can all remove the acetic acid in the tail gas of releasing; Guaranteed that the tail gas after the depickling can get into gas holder, the flare system of not anti-acetic acid corrosion safely; Saved the flare system that needs supporting newly-built anti-acetic acid to corrode; Except that extracting tower top reactive site uses the corrosion resistant stainless steel material; Systems such as whole extracting tower bottom storage tank, gas-liquid sedimentation separation jar and the NaOH solution circulating pump of this tail gas depickling contrive equipment all adopt common straightcarbon steel, thereby have practiced thrift the gross investment of new device greatly; This invention adopts temperature control system to control the vary in size operation of pump of exhaust gas processing device two, and the energy consumption of device is low, has reduced production cost of products.
Description of drawings
Fig. 1 is the partial structurtes sketch map on extracting tower top;
Fig. 2 is the structural representation of baffle plate in the extracting tower;
Fig. 3 is a process chart of the present invention.
The specific embodiment:
With reference to Fig. 1,2,3, specification φ 600 * 4000/ φ 1600 * 6000 of extracting tower [1].The reactive site of the undergauge on top is provided with at the overlapped 50～100mm of the relative direction of same axis (being 75mm in the present embodiment); And keep 5 herringbones retaining of a determining deviation to pull [10], locate to have wide a 3～6mm (being 5mm in the present embodiment), long strip through-hole [11] of lacking slightly apart from panel edges 30～50mm (being 40mm in the present embodiment) with baffle edge along the alkali lye flow direction above it.The pump of one big, little two different flows, specifications and models 65FF-35, little pump 6m
3/ h, big pump 12m
3/ h.Have only little pump to move continuously under the normal condition; But safety valve occurring opens when jumping; The heat release meeting of a large amount of acid and alkali reaction makes and is located at the variation of the thermometer measure signal on the herringbone baffle plate in the extracting tower; This signal drives big pump through the control system that is provided with and moves simultaneously, and the alkali lye that q.s is provided is to accomplish deacidification.
With reference to figure 3, the acetate acid tail gas that contains that the Zhong Ding ester apparatus is released and, at first the inlet [2] from extracting tower [1] top gets into, from bottom to top.Alkali lye is sent into by the inlet [4] on extracting tower [1] top through NaOH solution circulating pump [3], and gravity flow and descending is pulled [10] and contained that sour tail gas is reverse to be contacted through retaining, the acetic acid in the alkali lye absorbing and removing tail gas, and baffle plate and horizontal direction angle are 15 °.Entering extracting tower bottom recycled after alkali lye absorbed acetic acid; Tail gas is got in the gas-liquid sedimentation separation jars [7] by inlet [6] through pipeline from the outlet [5] on extracting tower [1] top after the depickling, behind dealkalize water, gets into flare system by the outlet [8] of gas-liquid sedimentation separation jar [7] again.Pump [3] has two, little pump operation under the normal condition, and big pump is subsequent use.When containing acid gas in a large number and release, the temperature of thermometer [9] can rise, and it drives subsequent use big pump through the control system and moves together, increases the internal circulating load of alkali lye, guarantees removing of acetic acid in the sour gas; When its temperature no longer rose and keeps downward trend, manual work stopped big pump.
Embodiment 1
With 30,000 tons of/year 2-butyl acetate production line vent gas treatment is example.According to above-mentioned technological process and step, the circulation of preparation 10% absorbs sodium hydroxide solution, and the tail gas that contains 99% concentration acetic acid in the running is released with the amount of 5.9t/h; The extracting tower temperature control system starts; Two NaOH solution circulating pumps of size start operation, and accident is finished dealing with after 10 minutes, and the sampling analysis concentration of lye is 5.6%; Acetic acid content after the depickling in the tail gas can not surveyed, and tail-gas quality meets the demands.
With 30,000 tons of/year 2-butyl acetate production line vent gas treatment is example.According to above-mentioned technological process and step; The circulation of preparation 10% absorbs sodium hydroxide solution, and the tail gas that contains 82ppm concentration acetic acid in the running is released with the amount of 3.9t/h, the little NaOH solution circulating pump operation of extracting tower; Accident is finished dealing with after 10 minutes; The sampling analysis concentration of lye is almost constant, and the acetic acid content after the depickling in the tail gas can not surveyed, and tail-gas quality meets the demands.
With 30,000 tons of/year 2-butyl acetate production line vent gas treatment is example.According to above-mentioned technological process and step; The circulation of preparation 10% absorbs sodium hydroxide solution, and the tail gas that contains 52ppm concentration acetic acid in the running is released with the amount of 8.5t/h, the little NaOH solution circulating pump operation of extracting tower; Accident is finished dealing with after 15 minutes; The sampling analysis concentration of lye is almost constant, and the acetic acid content after the depickling in the tail gas can not surveyed, and tail-gas quality meets the demands.
With 30,000 tons of/year 2-butyl acetate production line vent gas treatment is example.According to above-mentioned technological process and step; The circulation of preparation 10% absorbs sodium hydroxide solution, in 3 months running time, installs all acetic acid tank breather valve discharging tail gas amounts and is about 0.002t/h; The little NaOH solution circulating pump operation of extracting tower; The sampling analysis concentration of lye is 7.3% in the production process, and the acetic acid content after the depickling in the tail gas can not surveyed, and tail-gas quality meets the demands.
With 30,000 tons of/year 2-butyl acetate production line vent gas treatment is example.According to above-mentioned technological process and step, the circulation of preparation 10% absorbs sodium hydroxide solution, and device stops and purges; Two NaOH solution circulating pumps of extracting tower size move simultaneously; It is 3.3% that 9 hours post-samplings are analyzed concentration of lye, and the acetic acid content after the depickling in the tail gas is 15ppm, contains acetic acid in the tail gas.After replacing alkali lye reruned, the acetic acid content after the depickling in the tail gas can not surveyed, and tail-gas quality meets the demands.
Claims (6)
1. one kind removes 2-butyl acetate and prepares the method that contains sour tail gas in the process; Comprise that using mass percent concentration is that 3～10% sodium hydroxide solution is solvent; In extracting tower; Remove with the acetic acid in to be raw material release in producing the 2-butyl acetate process tail gas of the n-butene in the liquefied petroleum gas; Deviate from the liquefied petroleum gas of acetic acid and send into a gas-liquid settling tank again, get into the torch pipe network system again after isolating buck, the exhaust system of whole device is isolated with outer device through the fluid-tight that the gas-liquid settling tank is provided with.
2. the 2-butyl acetate that removes according to claim 1 prepares the method that contains sour tail gas in the process; It is characterized in that internal circulating load with the required sodium hydroxide solution of variations in temperature control depickling; Said internal circulating load with the required sodium hydroxide solution of variations in temperature control depickling is meant that safety valve opens jumping, contains in a large number under the situation that acid gas releases; When temperature reaches setting value, strengthen the output quantity of alkali lye.
3. implement the device of claim 1 or 2 said methods; Comprise an extracting tower and gas-liquid settling tank; This extracting tower is that the relative direction of same axis is provided with overlapped and keeps the retaining of a determining deviation to pull in reactive site; Extracting tower bottom sodium hydroxide solution is transported to the extracting tower top through pump, it is characterized in that said baffle plate and horizontal direction angle are 15 °, and baffle plate upper edge place has a strip through-hole short slightly with baffle edge.
4. device according to claim 3 is characterized in that described extracting tower is the reaction tower that the reactive site of acid-base neutralization and the storage tank that stores alkali lye are united two into one, and top is reactive site, and the alkali lye that absorbs behind the acetic acid is stored in the extracting tower bottom.
5. device according to claim 4, the specification that it is characterized in that described extracting tower are φ 600 * 4000/ φ 1600 * 6000; The reactive site of the undergauge on top is provided with at the overlapped 50～100mm of the relative direction of same axis; And keep 4～8 herringbones retaining of a determining deviation to pull, have a strip through-hole that wide a 3～6mm, length and baffle edge are lacked slightly apart from panel edges 30～50mm place along the alkali lye flow direction above the baffle plate.
6. device according to claim 3 is characterized in that described gas-liquid settling tank is to have the certain altitude water seal is attached thereto other device with isolation storage tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100317872A CN101402018B (en) | 2008-07-16 | 2008-07-16 | Method and device for removing acid in tail gas from reaction for producing 2-butyl acetate |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008100317872A CN101402018B (en) | 2008-07-16 | 2008-07-16 | Method and device for removing acid in tail gas from reaction for producing 2-butyl acetate |
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| CN101402018A CN101402018A (en) | 2009-04-08 |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2487971Y (en) * | 2001-06-04 | 2002-04-24 | 沈福昌 | Tail gas treating absorbing tower |
| JP2003260302A (en) * | 2002-03-11 | 2003-09-16 | Mitsubishi Electric Corp | Method and device for recovering organic solvent |
| JP2007054774A (en) * | 2005-08-26 | 2007-03-08 | Saitama Prefecture | Apparatus for treating voc and cartridge for apparatus for treating voc |
| CN2888249Y (en) * | 2006-03-10 | 2007-04-11 | 西安长庆科技工程有限责任公司 | Multifunctional tank with functions of flash evaporation, liquid separation and water seal for combustible gas emptying |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN2487971Y (en) * | 2001-06-04 | 2002-04-24 | 沈福昌 | Tail gas treating absorbing tower |
| JP2003260302A (en) * | 2002-03-11 | 2003-09-16 | Mitsubishi Electric Corp | Method and device for recovering organic solvent |
| JP2007054774A (en) * | 2005-08-26 | 2007-03-08 | Saitama Prefecture | Apparatus for treating voc and cartridge for apparatus for treating voc |
| CN2888249Y (en) * | 2006-03-10 | 2007-04-11 | 西安长庆科技工程有限责任公司 | Multifunctional tank with functions of flash evaporation, liquid separation and water seal for combustible gas emptying |
Non-Patent Citations (1)
| Title |
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| 魏玺群等.变压吸附法回收醋酸尾气工艺.《低温与特气》.2002,(第01期), * |
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