CN101920152A - Method for treating organic matters in large-capacity industrial waste gas - Google Patents
Method for treating organic matters in large-capacity industrial waste gas Download PDFInfo
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- CN101920152A CN101920152A CN2009100329465A CN200910032946A CN101920152A CN 101920152 A CN101920152 A CN 101920152A CN 2009100329465 A CN2009100329465 A CN 2009100329465A CN 200910032946 A CN200910032946 A CN 200910032946A CN 101920152 A CN101920152 A CN 101920152A
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Abstract
The invention relates to a method for treating organic matters in large-capacity industrial waste gas, mainly solving the problems of large capacity, difficult treatment and difficult energy recovery of the large-capacity industrial waste gas in the prior art. Industrial tail gas is treated by washing and does work by expanding; the gas after doing work enters an adsorption bed for carrying out adsorption treatment and desorption treatment, the gas subjected to desorption is carried out catalytic combustion under the existence of a catalyst, and the combusted industrial waste gas is treated by alkali washing to remove a halogen containing compound contained in the tail gas, therefore, the invention better solves the problems and can be used for treating waste gas generated by industrial production.
Description
Technical field
The present invention relates to organic method in a kind of processing industrial waste gas, particularly handle organic concentration at 20-999mg/m
3Industrial waste gas.
Background technology
The organic pollution particularly generation of volatile organic matter mainly is discharging in PETROLEUM PROCESSING, chemical products production, the coal process and volatilization of organic chemical industry's product application process etc.The volatile organic matter great majority are that virose, part also has carcinogenicity, under solar radiation, organic matter combines with oxynitrides in the atmosphere and forms photochemical fog, can be detrimental to health and biological growth, the halogenated hydrocarbon organic matter also can destroy ozone layer in the atmosphere, and the environment of human living is on the hazard.Processing to organic exhaust gas, some mature technique have been developed at present, the principle of handling generally is control and reduces using and develop harmless alternative materials, control discharge amount of exhaust gas, the organic matter of discharging being recycled or carried out harmless treatment of harmful raw material that processing method commonly used has firing method, absorption process, absorption method, membrane separation process etc.
Directly firing method is to carry out under high temperature (800-1200 ℃), is fit to handle organic concentration height (〉=2000mg/m
3), gas that combustion heat value is high, can cause that secondary pollution needs handle the smog that discharges thereby its shortcoming discharges black smoke when to be organic compound combustion incomplete, therefore need to add excessive air.For solving secondary pollution, people have developed the catalyst that catalytic combustion is used simultaneously, adopt this kind catalyst after, organic gas can carry out smokeless combustion under lower temperature (300 ℃) condition, generally can not cause secondary pollution.
Absorption process is the method for organic matter dissolving, collection being utilized by certain solvent.The degree of purification of organic exhaust gas is high more, and it is also just big more to absorb the amount of using solvent, and expense is also high more.Usually absorption process adopts water as solvent, because most of organic matter is slightly soluble in water, so absorption process solvent sprinkle density must not be lower than a certain setting value usually.Contain organic big water gaging and need be further processed and to discharge, so the method produces a large amount of water pollutions.Absorption method is to use adsorbent (active carbon, molecular sieve, silica gel etc.) that organic matter is carried out adsorption treatment, and will adsorb the method that concentrated organic matter is recycled.Compare with absorption process, characteristics such as clearance height, the energy consumption that absorption method has organic exhaust gas is low, adsorbent can repeat regeneration, widely applicable, but this method adopts the method for steam regeneration more at present, also will produce the pollution of secondary water.
Waste gas in many suitability for industrialized production contains lower organic concentration (20～999mg/m
3), though these organic matter content are low, toxicity big (easily carcinogenic), smell is big, national environmental standard is more and more harsher to the concentration requirement of its discharging, and therefore, it is that problem is concerned about in the environmental protection aspect that organic matter low-concentration industrial waste gas under the atm number is effectively handled always.In order to guarantee that continuous control enters content of organics in the industrial waste gas of atmosphere, and make the production operation expense reach minimum, the method that adopts usually is the said method integrated mode at present.As the processing method that adopts absorption to combine with catalytic combustion, because catalytic combustion adopts noble metal (Pt and Pd) substantially with catalyst, running cost is higher, for reducing running cost, with absorption method organic gas in the waste gas is carried out enrichment, the processing of then desorption gas being burnt increases the treating capacity of organic gas in the unit gas.
Patent CN1679999A adopts special-purpose rotation adsorbent equipment to carry out adsorption treatment, then the organic matter enriched gas is burnt.The rotation adsorbent equipment is combined closely a plurality of adsorbent beds, has reduced the absorption pipeline.But owing to adopted whirligig, moving part of appliance maintenance requirement improves.And to the organic gas combustion of enrichment, the heat that utilize to produce carries out desorb, reduces system capacity consumption greatly, carries out the desorb of adsorbent equipment but patent adopts blower fan to promote regeneration hot gas, has correspondingly increased system power consumption and equipment investment again.
Patent CN1883761A has proposed absorption, desorption under a kind of static state, carries out the method for enriched gas catalytic combustion again.This method has solved the production problem of continuous adsorption and desorb, does not adopt moving equipment, greatly reduces the expense that movable sealing produces.When carrying out the adsorbent equipment desorption, adopt the method identical with patent CN1679999A, both with 200 ℃ of hot gas behind the catalytic combustion as the desorb source of the gas, owing to reason falls in pipeline pressure, the method need increase resistant to elevated temperatures blower fan and increase the pipeline pressure head.
Said method is in handling atm number during organic gas, compare with traditional treatment method, demonstrate some advantages, but in the desorb after absorption concentrates, all adopt the hot gas after the gas combustion processing of enrichment as desorption gas, though the heat energy that has effectively utilized burning to produce to a certain extent, but with regard to the entire process system, increased the gas flow of handling, compared with adopting external hot gas, the gas flow of unit volume sorbent treatment is suitable in the absorption-desorption process.Not only increase auxiliary equipment quantity, also increased the processing load of organic waste gas treatment system, finally make system's complicated operating process, the operating cost height also increases system's construction cost.
Summary of the invention
Purpose of the present invention just provides organic method in a kind of processing industrial waste gas, can carry out the absorption of industrial waste gas continuously, the new method of desorption and catalytic combustion, adopt the method can make the unit volume adsorbent equipment handle the more industrial waste gas of atm number, pressurization industrial waste gas energy is further recycled, organic gas in the also abundant simultaneously purified industrial waste gas, do not produce secondary pollution, also the organic gas burning being produced heat fully recycles, the cleaning system flow process is simplified more, device quantity reduces, construction cost reduces, the operation and maintenance expense reduces, and has also saved energy simultaneously.
The inventive method comprises the steps:
A, the waste gas pressurization that commercial plant is produced are also carried out carrying out washing treatment;
B, the waste gas of carrying out washing treatment further after the heating, is entered the work done of one-level decompressor, the gas that one-level expands after the acting further heats in heat exchanger, carries out expansion working then in the compound expansion machine;
Gas after c, the compound expansion work done enters adsorbent bed and carries out adsorption treatment, and the mode that absorption adopts multistage adsorption zone to hocket is introduced stripping gas adsorbent bed is carried out desorb, adopts adsorption and desorption successively, the implementation procedure continued operation;
Gas after d, the desorb carries out catalytic combustion in the presence of catalyst, get burning industrial waste gas, the calory burning that catalytic combustion produces carries out heat recovery and utilizes by fully exchanging with combustion reactor, decompressor inlet gas heat, and the organic matter enriched gas after the desorb is further heated;
The burning industrial waste gas of e, the abundant heat exchange of process is handled through alkali cleaning, removes the halogen contained compound that contains in the waste gas.
Among the step a, washing step adopts the method for at least one step washing, and washing or caustic washing method are adopted in washing, can coagulate sour vapour and water to remove the corrosivity that exists in the waste gas;
Among the step b, the temperature that enters decompressor 16a or 25a is between 120～450 ℃, and is more excellent in 200～250 ℃.
Outlet Gas Temperature is 160～170 ℃ behind the described one-level expansion working, and exit gas pressure is controlled at 2～10atm.
Described gas further heats, and enters compound expansion machine 16b or 25b temperature at 170～200 ℃,
More excellent temperature is at 180～190 ℃, and Outlet Gas Temperature is at 20～30 ℃ after compound expansion machine 16b or the 25b work done, and pressure is 1～2atm.
Gas among the step c, after the compound expansion work done enters adsorbent bed 14 or 24 and contacts with adsorbent and carry out adsorption treatment, and the multistage adsorption zone adsorption and desorption that hockets, implementation procedure continued operation are adopted in absorption.Desorption gas can be the portion of hot gas behind the one-level expansion working, also can shunt a part of gas after the compound expansion work done and heat, as stripping gas.Adopting this strand desorption gas successively each adsorbent bed 14 or 24 to be carried out desorb handles; When carrying out adsorption operations, adsorbent bed 14 is adsorbent beds, when carrying out the desorb operation, the desorption gas that former adsorbent bed 14 becomes in desorb bed (following 14 also can be described as adsorbent bed or the desorb bed) desorption process directly comes from industrial waste gas, significantly reduce each binding domain gas treatment amount like this, increase the adsorption system disposal ability.
After passing through the desorption gas (containing the enrichment organic matter) of adsorbent bed 14 and partly the gas of process adsorbent bed 14 not mixing, enter into catalytic combustion reactor 17 or 27 imports, control both flows and make the organic concentration in mixing back be lower than 25% of organic component explosion limit in mass all the time.
Described adsorbent is one or more in wooden activated carbon, coal-based activated carbon, activated carbon fiber, silica gel, aluminium oxide or the molecular sieve, and described adsorbent is formed the adsorbent bed of single or multiple lift.Each adsorbent bed is imported and exported the open and close valve that all is provided with chain interaction, by the DCS control system, at the different time valve in open and close absorption pipeline and desorption tube road according to this, has realized the continued operation of adsorption and desorption, cooling.
Hot nitrogen or thermal purification gas that desorption gas adopts thermal technology's industry waste gas place of water steam and blower fan to carry have reduced adsorbent bed quantity and blower fan quantity.When needing to cool off after the desorb of adsorbent bed high temperature, by the control valve action, close the hot gas that enters the desorb bed, make it directly enter into catalytic combustion reactor 17 or 27 preceding preheaters, carry out catalytic combustion then.
In the steps d, gas temperature rises to 400～500 ℃ behind the catalytic combustion, and gas enters into and carries out heat exchange in heat exchanger 13E or the 23f, finally makes the waste gas outlet temperature that enters into combustion reactor guarantee that at 250～350 ℃, more excellent temperature is at 300～320 ℃.Described catalyst is the VOCat450 type catalyst that BASF AG produces, and is to be carrier with the cordierite, aluminium oxide or SiO
2Composite oxides are as the Pt/Pd noble metal catalyst of coating.
Among the step e, the halogen compounds that catalytic combustion after-purification gas contains is further handled by caustic wash tower 12 or 22 modes of carrying out at least one step alkali liquid washing, reduces environmental pollution, and the conventional method alkali cleaning is adopted in alkali cleaning.
Of the present invention owing to adopt such scheme, have following advantage: the present invention adopts multistage heating expansion working, can press the kinetic energy of industrial waste gas to make full use of on heat energy, the band of low grade heat energy in the commercial plant and catalytic combustion generation, reduce the process units energy consumption; The present invention and existing direct burning purification techniques are relatively, owing to adopted absorption to concentrate means and new hot waste gas renovation process, guaranteeing under the constant prerequisite of adsorbent bed quantity, compare with other desorption method, by attached illustrated in figures 1 and 2, the present invention extracts one gas out and directly uses as desorption gas from gas to be adsorbed, the gas treatment amount that makes each adsorbent bed pass through reduces, the corresponding treating capacity that improves reaction system, the adsorbent bed pressure drop reduces, and has reduced system failure rate.Simultaneously follow-up catalytic combustion is handled tolerance and is reduced to direct burning treating capacity 10%-30% in mass, corresponding combustion reaction catalyst amount also reduces directly burning treating capacity 10%-30% in mass, the investment for trnasforming urban land of saving the industrial waste gas processing unit widely thus.Regeneration is no longer used with water vapour in the adsorption system, also reduces the water yield of secondary pollution; The present invention adopts the open and close program of the chain interaction of DCS control, has realized purifier continuous adsorption, desorb and cooling down operation, has guaranteed to enter the stability of catalytic combustion reactor organic concentration.And adopt purified waste gas carrying out washing treatment again, eliminated the atmosphere pollution that contains halogen compounds; The catalytic combustion employing is a carrier with the cordierite among the present invention, aluminium oxide or SiO
2Composite oxides can be suitable for containing the organic gas purification of halogen compounds as the Pt/Pd noble metal catalyst of coating; Because the present invention has considered big industrial waste gas organic matter simultaneously and has purified and the energy utilization, makes full use of the detergent power of limited device, both can make the atm number organic exhaust gas reach environmental requirement, can energy savings, reduce and build and operating cost, therefore, be particularly suitable for the device capacity expansion revamping.
Description of drawings
One of Fig. 1 schematic flow sheet of the present invention
Two of Fig. 2 schematic flow sheet of the present invention
The specific embodiment
Below in conjunction with drawings and Examples invention is described in detail, embodiment does not produce any restriction to the present invention.Purified treatment with oxidation industrial waste gas in terephthalic acid (TPA) (PTA) production in this example is that example illustrates.Its flow process as depicted in figs. 1 and 2.
The PTA oxidation gaseous effluent is main consists of nitrogen, oxygen, carbon dioxide, carbon monoxide, methyl acetate, benzene, paraxylene, toluene, Celfume, acetic acid and water etc., and it is about 10atm at the production system operating pressure usually, and temperature is about 110 ℃.Organic matter benzene, paraxylene, toluene, Celfume concentration are respectively at 20～100mg/m in the waste gas
3, all belong to poisonous carcinogenic substance, easily human body is caused very big injury, need handle.
As shown in Figure 1, at first the waste gas 111 that oxidation is produced is through high pressure scrubber washing 11, remove wherein most of acetic acid and water, enter into heat exchanger 13a heating temperature raising then, industrial waste gas after the heating enters the work done of one-level decompressor 16a adiabatic expansion, the gas pressure of finishing after the one-level decompressor does work reaches 2～10atm, temperature is about 160～170 ℃, from then on shunt one hot fluid in the gas as stripping gas, remaining most of hot waste gas is by secondary heat exchanger 13b, and 13c heats to 200～250 ℃, enters the acting of compound expansion machine 16b adiabatic expansion then, the gas pressure that expands after doing work is 1～2atm, 20～30 ℃ of temperature.This strand gas of finishing the compound expansion work done is evenly distributed in 6 adsorbent beds 14, the import and export of adsorbent bed are provided with switch valve, when this adsorbent bed during for adsorbed state, advancing cold air valve 15a opens simultaneously with the air outlet valve 15b that is connected atmosphere, oxidation gaseous effluent is carried out adsorption treatment, by the time adsorbent bed absorption reaches and passes saturating point, when organic matter comes into existence in the purifying exhaust air, stop absorption, begin to enter desorption state, close 15a this moment, and 15b opens 15c simultaneously, 15d, pressure is 2～10atm, and temperature is that the oxidation gaseous effluent about 160～170 ℃ carries out the desorption processing to adsorption bed, and the organic matter desorb under the condition of high temperature that is adsorbed on the adsorbent enters in the thermal oxide waste gas.Pressure is 2atm, temperature be about 170 ℃ heat of oxidation waste gas some directly reach desorb bed outlet by control valve, control valve 18 is adjusted and is entered the catalytic combustion reactor organic concentration, guarantee its certain hour of process below 25% desorb under explosion limit, close 15c, 15d, the desorb bed is cooled off, all pressure are 2～10atm, temperature is that the heat of oxidation waste gas about 160～170 ℃ enters heat exchanger 13e by control valve 18, makes it enter the combustion reaction actuator temperature and reaches 250～350 ℃.During driving, adopt electrical heating or high-temperature steam mode of heating, this strand gas is heated to predetermined temperature, when beginning stable operation, when catalytic combustion after-purification gas temperature reaches 400～500 ℃, can close driving heater 13d, utilize high temperature purification gas and its heat exchange in 13e.After preheater 13e is heated to 250～350 ℃, entering catalytic combustion reactor decomposes, behind this reactor internal reaction, make all organic matters be converted into carbon dioxide and water, wherein carbon monoxide also is oxidized to CO2, because catalytic combustion makes Outlet Gas Temperature reach 400～500 ℃, as mentioned above, will purify the back high-temperature gas and enter 13e heat exchanger one side, with the inlet gas heat exchange, and then with this strand high-temperature gas with advance the further heat exchange in 13a of decompressor gas, fully reclaim the heat energy that burning produces, can't burn owing to contain bromide, therefore, the burning purified gas, before entering atmosphere, after absorption is handled through alkali lye, reclaim bromide.
As shown in Figure 2, at first the waste gas 111 that oxidation is produced is through high pressure scrubber washing 21, remove wherein most of acetic acid and water, enter into heat exchanger 23a heating temperature raising then, after the heating industrial waste gas enter the work done of one-level decompressor 25a adiabatic expansion, the gas pressure of finishing after the one-level decompressor does work reaches 2～10atm, temperature is about 160～170 ℃, then by secondary heat exchanger 23b, 23c heats to more than 200 ℃, enter the acting of compound expansion machine 16b adiabatic expansion, the gas pressure after the acting of expanding is 1～2atm, and temperature is 20～30 ℃.Finish the gas of compound expansion work done and tell one gas, enter 24 blower fan superchargings, enter the 23c heating then, be used for adsorbent bed and resolve hot gas.Remaining most of gas of compound expansion work done is evenly distributed in 6 adsorbent beds 14, the import and export of adsorbent bed are provided with switch valve, when this adsorbent bed during for adsorbed state, advancing cold air valve 26d opens simultaneously with the air outlet valve 26b that is connected atmosphere, oxidation gaseous effluent is carried out adsorption treatment, by the time adsorbent bed absorption reaches and passes saturating point, when organic matter comes into existence in the purifying exhaust air, stop absorption, begin to enter desorption state, close 26d this moment, 26b opens 26c, 26a simultaneously, with the heat of oxidation waste gas adsorption bed is carried out desorption and handle, the organic matter desorb under the condition of high temperature that is adsorbed on the adsorbent enters in the thermal oxide waste gas.Pressure is 2～10atm, temperature be about 160～170 ℃ heat of oxidation waste gas some directly reach desorb bed outlet by control valve, control valve 28 is adjusted and is entered the catalytic combustion reactor organic concentration, guarantee its certain hour of process below 25% desorb under explosion limit, close 26c, 26a, the desorb bed is cooled off, all pressure are 2～10atm, temperature is that the heat of oxidation waste gas about 160～170 ℃ enters heat exchanger 23f by control valve 28, makes it enter the combustion reaction actuator temperature and reaches 250～350 ℃.During driving, adopt electrical heating or high-temperature steam mode of heating, this strand gas is heated to predetermined temperature, when beginning stable operation, when catalytic combustion after-purification gas temperature reaches 400～500 ℃, can close driving heater 23e, utilize high temperature purification gas and its heat exchange in 23f.After preheater 23f is heated to 250～350 ℃, entering catalytic combustion reactor decomposes, behind this reactor internal reaction, make all organic matters be converted into carbon dioxide and water, wherein carbon monoxide also is oxidized to CO2, because catalytic combustion makes Outlet Gas Temperature reach 400～500 ℃, as mentioned above, will purify the back high-temperature gas and enter 23f heat exchanger one side, with the inlet gas heat exchange, and then with this strand high-temperature gas with advance the further heat exchange in 23a of decompressor gas, fully reclaim the heat energy that burning produces, can't burn owing to contain bromide, therefore, the burning purified gas, before entering atmosphere, after absorption is handled through alkali lye, reclaim bromide.
Claims (8)
1. handle organic method in the atm number industrial waste gas, may further comprise the steps:
A, the waste gas pressurization that commercial plant is produced are also carried out carrying out washing treatment;
B, the waste gas of carrying out washing treatment further after the heating, is entered the work done of one-level decompressor, the gas that one-level expands after the acting further heats in heat exchanger, carries out expansion working then in the compound expansion machine;
Gas after c, the compound expansion work done enters adsorbent bed and carries out adsorption treatment, and the mode that absorption adopts multistage adsorption zone to hocket is introduced stripping gas adsorbent bed is carried out desorb, adopts adsorption and desorption successively, the implementation procedure continued operation;
Gas after d, the desorb carries out catalytic combustion in the presence of catalyst, get burning industrial waste gas, the calory burning that catalytic combustion produces carries out heat recovery and utilizes by fully exchanging with combustion reactor, decompressor inlet gas heat, and the organic matter enriched gas after the desorb is further heated;
The burning industrial waste gas of e, the abundant heat exchange of process is handled through alkali cleaning, removes the halogen contained compound that contains in the waste gas.
2. according to the method for claim 1, it is characterized in that: among the described step a, washing step adopts the method for at least one step washing, and washing or alkali cleaning are adopted in washing.
3. according to the method for claim 1, it is characterized in that: among the step b, the gas temperature that enters the one-level decompressor is between 120～450 ℃, and Outlet Gas Temperature is 160～170 ℃ behind the one-level expansion working, and exit gas pressure is controlled at 2～10atm;
Described gas 2 further heats, and enters compound expansion machine temperature at 170～200 ℃, and Outlet Gas Temperature is at 20～30 ℃ after the work done of compound expansion machine, and pressure is 1～2atm.
4. according to the method for claim 3, it is characterized in that: the gas temperature that enters the one-level decompressor among the step b enters compound expansion machine gas temperature at 180～190 ℃ at 200～250 ℃.
5. according to the method for claim 1, it is characterized in that: among the step c, described stripping gas is the portion of hot gas after one-level expansion or the compound expansion work done.
6. according to the method for claim 1, it is characterized in that: among the step c, the adsorbent that described adsorbent bed is selected for use is one or more in wooden activated carbon, coal-based activated carbon, activated carbon fiber, silica gel, aluminium oxide or the molecular sieve.
7. according to the method for claim 1, it is characterized in that: a part of stripping gas carries out the desorb processing by adsorbent bed to the organic adsorbent of enrichment among the step c, another part desorption gas does not directly arrive the outlet of desorb bed by adsorbent bed, with enter gas heater after stripping gas mixes, catalytic combustion carries out purified treatment then.
8. according to the method for claim 1, it is characterized in that: through the stripping gas of adsorbent bed and after partly the gas of process adsorbent bed does not mix, enter into the catalytic combustion reactor import, regulate both flows and make the organic concentration in mixing back be lower than 25% of organic component explosion limit in mass all the time.
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| CN103446881A (en) * | 2013-09-11 | 2013-12-18 | 中石化上海工程有限公司 | Method for catalytically oxidizing tail gas by using phenol-acetone device to realize energy saving and emission reduction |
| CN105289484A (en) * | 2015-04-02 | 2016-02-03 | 江苏沥泽生化科技有限公司 | Efficient adsorption activated carbon fiber cloth and preparation method thereof |
| CN105536428A (en) * | 2015-12-14 | 2016-05-04 | 北京蓝博新科环保科技有限公司 | Organic waste gas purification system and purification method |
| CN107252606A (en) * | 2017-07-03 | 2017-10-17 | 安徽国能亿盛环保科技有限公司 | A kind of industrial waste gas handling process |
| CN112122327A (en) * | 2020-08-20 | 2020-12-25 | 杨晓秋 | Prosthetic devices based on soil thermal desorption repair technique |
| CN113262580A (en) * | 2021-06-09 | 2021-08-17 | 江西理工大学 | Acetic acid recovery method for furfural production waste gas |
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| JP2001070750A (en) * | 1999-09-06 | 2001-03-21 | Taikisha Ltd | Waste gas treatment system |
| CN2537454Y (en) * | 2001-12-27 | 2003-02-26 | 中国人民解放军63971部队 | Organic waste gas purifying treatment system |
| CN2579505Y (en) * | 2002-10-31 | 2003-10-15 | 陈泽枝 | Organic waste gas purifying device |
| CN1962028A (en) * | 2006-10-26 | 2007-05-16 | 清华大学 | Method for reclaiming methylene chloride from waste gas |
| CN101284201A (en) * | 2008-06-02 | 2008-10-15 | 北京云辰天环保科技有限公司 | Organic waste gas treatment process without secondary pollution |
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| CN103446881A (en) * | 2013-09-11 | 2013-12-18 | 中石化上海工程有限公司 | Method for catalytically oxidizing tail gas by using phenol-acetone device to realize energy saving and emission reduction |
| CN103446881B (en) * | 2013-09-11 | 2015-03-25 | 中石化上海工程有限公司 | Method for catalytically oxidizing tail gas by using phenol-acetone device to realize energy saving and emission reduction |
| CN105289484A (en) * | 2015-04-02 | 2016-02-03 | 江苏沥泽生化科技有限公司 | Efficient adsorption activated carbon fiber cloth and preparation method thereof |
| CN105536428A (en) * | 2015-12-14 | 2016-05-04 | 北京蓝博新科环保科技有限公司 | Organic waste gas purification system and purification method |
| CN107252606A (en) * | 2017-07-03 | 2017-10-17 | 安徽国能亿盛环保科技有限公司 | A kind of industrial waste gas handling process |
| CN112122327A (en) * | 2020-08-20 | 2020-12-25 | 杨晓秋 | Prosthetic devices based on soil thermal desorption repair technique |
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| CN113262580A (en) * | 2021-06-09 | 2021-08-17 | 江西理工大学 | Acetic acid recovery method for furfural production waste gas |
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