CN115608104A - System and method for separating water vapor and tobacco tar and recovering viscosity reducer - Google Patents
System and method for separating water vapor and tobacco tar and recovering viscosity reducer Download PDFInfo
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- CN115608104A CN115608104A CN202211608807.4A CN202211608807A CN115608104A CN 115608104 A CN115608104 A CN 115608104A CN 202211608807 A CN202211608807 A CN 202211608807A CN 115608104 A CN115608104 A CN 115608104A
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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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
- B01D53/0438—Cooling or heating systems
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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
- B01D53/32—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 electrical effects other than those provided for in group B01D61/00
- B01D53/323—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 electrical effects other than those provided for in group B01D61/00 by electrostatic effects or by high-voltage electric fields
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C—MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
- B03C3/00—Separating dispersed particles from gases or vapour, e.g. air, by electrostatic effect
- B03C3/017—Combinations of electrostatic separation with other processes, not otherwise provided for
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/102—Carbon
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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Abstract
The invention discloses a system and a method for separating water vapor smoke oil and recovering a viscosity reducer. The method sequentially removes macromolecules in the flue gas through pretreatment, organic micromolecules are adsorbed, carbon is desorbed, decoloration and deodorization, and the recovered viscosity reducer is obtained and can be directly used for production, so that the production cost of enterprises is greatly reduced, and the common fault of the industry with unqualified flue gas emission in the production process is relieved; the method solves the problems of environmental pollution, human health injury, low recovery rate and incapability of direct use caused by overlarge smoke; the viscosity reducer obtained by the treatment of the invention has better effect than the original viscosity reducer, the recovery amount accounts for more than 85% of the production addition amount, and the treated residual gas reaches the environmental protection discharge standard.
Description
Technical Field
The invention relates to the field of water vapor smoke oil treatment, in particular to a system and a method for separating water vapor smoke oil and recovering a viscosity reducer.
Background
The PVC glove industry has been in the past for over thirty years, and PVC gloves themselves are non-toxic and harmless. However, the PVC material itself generates chlorine, vinyl chloride, dioxin and other gases after high temperature treatment, which are all toxic substances. If there is a long-term emission of pungent odor, it is highly likely that the exhaust gas purification treatment of the plant is not up to standard. And the plasticizer and the stabilizer added in the production process of the PVC gloves can not reach the quality standard and can also emit unpleasant odor, and the PVC gloves are mixed with PVC and heated to generate poisonous gases such as acetylene, hydrogen chloride, vinyl chloride, sulfuric acid and the like, so that the gloves can cause damage to bodies after being inhaled for a long time.
At present, more than 30 PVC glove manufacturers exist in China, and more than 2000 PVC glove production lines are produced. Because a large amount of smoke with main contents of raw materials of gloves such as viscosity reducers, DOTP and the like can be generated at high temperature in the production process, the phenomena of overlarge smoke, serious environmental pollution, damage to the health of workers and great waste of the production cost of enterprises commonly exist in a glove production workshop.
At present, most manufacturers adopt a method that after being collected by a smoke collection device, the smoke is sent to a cooling device through a gas pipeline, the temperature of the smoke is reduced to a temperature suitable for being processed by electrostatic oil fume purification equipment through a heat exchange mode, the cooled smoke enters the oil fume purification equipment, and oil components such as a viscosity reducer and the like in the smoke are changed into liquid oil under the action of high-voltage static electricity to be recovered. But the method has the disadvantages that the smoke treatment is not thorough, only large particles such as engine oil, DOTP and the like with low content in the smoke can be treated, the small particle viscosity reducer with the highest content in the smoke hardly has any effect, the emission standard required by PM2.5 cannot be met, and the environment is seriously polluted; the second disadvantage is that the oil recovery rate is low and the oil can not be directly recycled to reduce the production cost of enterprises.
Disclosure of Invention
The invention provides a system and a method for separating water vapor and smoke oil and recovering a viscosity reducer in order to make up for the defects of the prior art.
The invention is realized by the following technical scheme: a system for separating water vapor smoke oil and recovering viscosity reducer comprises a pretreatment system, an adsorption system, a desorption system, a decolorization system and a deodorization system;
the pretreatment system comprises a PVC oven area, a smoke dispersion area, a PU oven, a purification system, high-frequency high-voltage electrostatic oil mist purification equipment and an induced draft fan;
the adsorption system comprises an active carbon tower and a plurality of inclined plate type adsorption plates arranged in the active carbon tower; 721 type active carbon and calcium chloride loaded active carbon are alternately arranged on the inclined plate type adsorption plate.
Preferably, the calcium chloride-loaded activated carbon is lignin activated carbon.
The invention also provides a method for separating the water vapor smoke oil and recovering the viscosity reducer by using the system for separating the water vapor smoke oil and recovering the viscosity reducer, which comprises the following steps:
the method comprises the following steps: preprocessing to remove macromolecules in the smoke; the method comprises the following steps of classifying, collecting and purifying high-temperature oil fume waste gas with different temperatures at the outlet of a PVC oven zone, a smoke dispersion zone and a PU oven of a PVC glove production line, conveying the waste gas into a purification system through a gas transmission pipeline, cooling through a stainless steel multi-surface pipe, filtering macromolecular substances in the smoke under the action of high-voltage static electricity through high-frequency high-voltage electrostatic oil mist purification equipment, and exhausting the smoke to an adsorption system through an induced draft fan;
step two: small molecule adsorption; the pretreated flue gas enters an activated carbon tower, a PLC controls a pneumatic butterfly valve to control air inflow and adsorption time, and cyclic adsorption is carried out, wherein the adsorption time of each group is 22-24 hours;
step three: carbon desorption; after reaching the adsorption time, heating the mixture by using air of a heat exchanger and flushing nitrogen into the mixture for desorption, wherein the desorption time of each group is 5 to 6 hours, and then performing electrostatic and cooling treatment on the mixture and then feeding the mixture into a decoloring tank;
step four: decoloring; heating the desorbed liquid oil to 82-85 deg.C by heat exchanger, adding 0.1% decolorizing agent, stirring for 2-2.5 hr, standing for 1-1.5 hr, and deodorizing the supernatant in deodorizing tank;
step five: deodorizing; cooling the decolorized liquid oil to 34-36 ℃ by a cooler, pumping the decolorized liquid oil into a deodorization tank, stirring the decolorized liquid oil for 1-1.5 hours, and pumping the decolorized liquid oil into a temporary storage tank, wherein the addition amount of a deodorizing agent is 0.5%;
step six: temporarily storing; and sealing and storing the deodorized tobacco tar.
Preferably, the carbon adsorption temperature in the second step is 35-36 ℃.
Preferably, before the pretreated flue gas enters the activated carbon tower in the second step, the activated carbon in the activated carbon tower is subjected to reaming modification.
Preferably, the reaming modification method in the second step comprises the following steps: firstly, 2M HNO is sprayed by a spray head 3 Spraying the solution on the surface of the activated carbon, heating the activated carbon tower to 500-600 ℃, heating at a rate of 1-2 ℃/min, then quickly heating to a modification temperature of 900-950 ℃, modifying for 60-100min, heating at a rate of 20 ℃/min, keeping the activated carbon in a carbon dioxide atmosphere in the modification process, and cooling to room temperature after the carbon dioxide flow is 2L/min.
Preferably, in order to prevent carbonization of the calcium chloride-loaded activated carbon, the activated carbon is subjected to pore-expanding modification, and then the adsorption plate loaded with the calcium chloride-loaded activated carbon is arranged in the activated carbon tower.
Preferably, the desorption temperature in the third step is 155-160 ℃.
Preferably, in the fourth step, the decolorizing agent is any one of ethanol to ethanolamine to amide ratio of 4.
Preferably, in the fifth step, the deodorizing agent is selected from caustic soda, water and cobalt phthalocyanine of 1.
Compared with the prior art, the invention has the advantages that:
1. the viscosity reducer recovered by the method can be directly used for production, so that the production cost of enterprises is greatly reduced, and the common fault of the industry with unqualified smoke emission in the production process is relieved; the method solves the problems of environmental pollution, human health injury, low recovery rate and incapability of direct use caused by excessive smoke;
2. the tobacco tar treated by the method is a viscosity reducer, the viscosity reducing effect is better than that of the original viscosity reducer, the recovery amount accounts for more than 85% of the production addition amount, and the treated residual gas reaches the environmental-friendly discharge standard.
Drawings
The invention is further described below with reference to the accompanying drawings.
FIG. 1 is a process flow diagram of the present invention;
FIG. 2 is a flow diagram of carbon adsorption according to the present invention;
fig. 3 is a desorption flow chart of the present invention.
Detailed Description
The technical solution of the present invention is further illustrated by the following examples.
Example 1
A system for separating water vapor smoke oil and recovering viscosity reducer comprises a pretreatment system, an adsorption system, a desorption system, a decolorization system and a deodorization system;
the pretreatment system comprises a PVC oven area, a smoke dispersion area, a PU oven, a purification system, high-frequency high-voltage electrostatic oil mist purification equipment and an induced draft fan;
the adsorption system comprises an active carbon tower and a plurality of inclined plate type adsorption plates arranged in the active carbon tower; the inclined plate type adsorption plates are respectively provided with activated carbon and calcium chloride loaded activated carbon, and the two inclined plate type adsorption plates are arranged at intervals.
In this embodiment, the calcium chloride-loaded activated carbon is lignin activated carbon.
Example 2
A method for separating water vapor and smoke oil to recover viscosity reducer comprises the following steps:
the method comprises the following steps: pretreating to remove macromolecules in the smoke; PVC oven district of PVC gloves production line, scattered cigarette district, the different temperature high temperature oil smoke waste gas of PU oven export carries out the classified collection and purifies, the waste gas that volatilizees out on the PVC gloves production line carries purification system through gas transmission pipeline in, earlier through unobstructed and the little stainless steel multi-face pipe cooling of resistance and handle, rethread high-frequency high voltage electrostatic oil mist clarification plant, under high-voltage static's effect, the macromolecule class in the filtering flue gas, then convulsions to adsorption system by the draught fan again.
Step two: small molecule adsorption; the pretreated flue gas (the temperature is 35-36 ℃) enters an activated carbon tower, the total number of the activated carbon towers is 18, each activated carbon tower is a group, the PLC controls a pneumatic butterfly valve to control the air inflow and the adsorption time, the adsorption is carried out in a circulating way, and the adsorption time of each group is 22-24 hours; as 16-18 production lines are commonly used in a workshop, the area of the workshop reaches about 1 ten thousand square meters, and practice proves that the adsorption tank adopts an inclined plate type adsorption plate, so that the oil recovery efficiency is highest, and the effect is best.
Owing to unbalanced and unsaturated molecular attraction or chemical force on the solid surface of active carbon, when the solid surface contacts with gas, the gas molecules are attracted and concentrated and maintained on the solid surface to adsorb organic waste gas molecules in the micropores inside the active carbon, so that the pollutant is adsorbed, and the waste gas is filtered in a filter and fed into dust exhaust system for exhausting purified gas.
Step three: carbon desorption; and after reaching the adsorption time, heating by using air of a heat exchanger and charging nitrogen for desorption, wherein the desorption time of each group is 5-6 hours, and then performing electrostatic and cooling treatment and entering a decoloring tank.
The high-temperature carbonization is to boil and vaporize a part of organic matters adsorbed on the activated carbon, a part of the organic matters are subjected to decomposition reaction to generate micromolecular hydrocarbon to be desorbed, and residual components are left in pores of the activated carbon to form 'fixed carbon'. At this stage, the temperature will reach 155-160 ℃, generally under vacuum or inert atmosphere, in order to avoid oxidation of the activated carbon. In the next activation stage, nitrogen is introduced into the activated carbon tower to clean the activated carbon micropores and restore the adsorption performance, and the activation stage is the key of the whole regeneration process.
Step four: decoloring; heating the desorbed liquid oil to 82-85 deg.C by heat exchanger, adding 0.1% decolorizer, stirring in the decolorization tank for 2-2.5 hr, standing for 1-1.5 hr, and deodorizing the supernatant in a deodorizing tank.
The decolorant adopts two formulas of ethanol, ethanolamine, amide (4.
Step five: deodorizing; cooling the decolorized liquid oil to 34-36 ℃ through a cooler, pumping the decolorized liquid oil into a deodorization tank, stirring the decolorized liquid oil for 1-1.5 hours, pumping the decolorized liquid oil into a temporary storage tank, wherein the addition of a deodorizing agent is 0.5%, and the deodorizing agent is selected from caustic soda, water, poly-cobalt phthalocyanine and the ratio of 1.05.
Step six: temporarily storing; and sealing and storing the deodorized tobacco tar.
Example 3
When the activated carbon is desorbed, residual components are left in the pores of the activated carbon to form fixed carbon, and in order to recycle the activated carbon, micropores of the activated carbon need to be cleaned so as to recover the adsorption performance.
The difference between the embodiment and the embodiment 2 is that before the pretreated flue gas enters the activated carbon tower in the step two, the activated carbon in the activated carbon tower is subjected to reaming modification.
However, in the experimental process of pore expansion modification, it is found that after the carbon dioxide is used for modifying the activated carbon, the specific surface area of the mesopores in the activated carbon is obviously increased, so that the specific surface area of the activated carbon is obviously reduced, and the adsorption capacity of organic small molecules is reduced. It is also necessary to control the specific surface area of the activated carbon.
In this embodiment, the specific surface area of the activated carbon is controlled by spraying nitric acid, and the specific operations are as follows:
firstly, 2M HNO is sprayed by a spray head 3 The solution is sprayed on the surface of the activated carbon, then the temperature of the activated carbon tower is raised to 500-600 ℃, the heating rate is 1-2 ℃/min, then the temperature is rapidly raised to 900-950 ℃ of modification temperature, the modification treatment time is 60-100min, the heating rate is 20 ℃/min, the activated carbon is always in the carbon dioxide atmosphere in the modification process, the carbon dioxide flow is 2L/min, and then the temperature is lowered to the room temperature.
Due to HNO 3 The strong oxidizing property destroys the microporous structure of the activated carbon, so that partial microporous pore wall is collapsed to form transition pores, the surface area and the pore volume are both reduced, the activated carbon is subjected to secondary activation through high-temperature heat treatment, on one hand, more micropores are formed in the decomposition process of surface functional groups, on the other hand, partial micropores are ablated into mesopores, so that the number of the micropores is not rapidly reduced, on the contrary, the pore structure of the activated carbon tends to be more developed, and the surface area and the pore volume are more developed under the condition that the mesopore content is obviously increasedThe product increases.
Because the modification of the carbon dioxide can open part of originally blocked holes in the activated carbon, the structural connectivity of the activated carbon holes is improved, and the cleaning capability is obviously improved. The active carbon after reaming modification can be reused, and the cleaning effect can reach more than 98%.
Example 4
The difference between this example and example 2 is that in step two, the inclined plate type adsorption plates are adsorption plates on which activated carbon and calcium chloride-loaded activated carbon are respectively arranged, and the two inclined plate type adsorption plates are arranged at intervals. The purpose is to recover water and oil separately.
In order to prevent the calcium chloride-loaded activated carbon from carbonizing, the adsorption plate loaded with the calcium chloride-loaded activated carbon is arranged in the activated carbon tower after the activated carbon is subjected to reaming modification. The calcium chloride-loaded activated carbon is lignin activated carbon, water vapor is adsorbed by the lignin activated carbon, and the adsorbed water vapor is conveyed into a water storage device through a condensing pipe connected to the bottom of the inclined plate type adsorption plate for subsequent water treatment. And after the adsorption is finished, closing the condensing pipe.
The most important prerequisite for the above three embodiments is that the glove oven must be particularly airtight, and the negative pressure must be maintained in the oven, otherwise the smoke will be directly scattered into the workshop, and the recovery rate of the tobacco tar will be affected.
While particular embodiments of the present invention have been described, it will be understood that the scope of the invention is not limited thereto, and that various modifications and changes in light thereof will be suggested to persons skilled in the art and are to be included within the spirit and purview of this invention.
Claims (10)
1. The utility model provides a system for viscosity reducer is retrieved to separation steam tobacco tar which characterized in that: comprises a pretreatment system, an adsorption system, a desorption system, a decoloration system and a deodorization system;
the pretreatment system comprises a PVC oven area, a smoke dispersion area, a PU oven, a purification system, high-frequency high-voltage electrostatic oil mist purification equipment and an induced draft fan;
the adsorption system comprises an active carbon tower and a plurality of inclined plate type adsorption plates arranged in the active carbon tower; the inclined plate type adsorption plate is alternately provided with active carbon and active carbon loaded with calcium chloride.
2. The system for separating water vapor smoke oil recovery viscosity reducer according to claim 1, wherein the activated carbon loaded with calcium chloride is lignin activated carbon.
3. A method for recovering the viscosity reducer based on the system for separating the water vapor and the smoke oil according to any one of the claims 1 to 2, which is characterized by comprising the following steps:
the method comprises the following steps: preprocessing to remove macromolecules in the smoke; the method comprises the following steps of classifying, collecting and purifying high-temperature oil fume and waste gas with different temperatures at the outlets of a PVC oven zone, a smoke dispersing zone and a PU oven of a PVC glove production line, conveying the waste gas into a purification system through a gas transmission pipeline, cooling through a stainless steel multi-surface pipe, filtering macromolecular substances in the smoke under the action of high-voltage static electricity through high-frequency high-voltage electrostatic oil mist purification equipment, and then exhausting the smoke to an adsorption system through an induced draft fan;
step two: small molecule adsorption; the pretreated flue gas enters an activated carbon tower, a PLC controls a pneumatic butterfly valve to control air inflow and adsorption time, and cyclic adsorption is carried out, wherein the adsorption time of each group is 22-24 hours;
step three: carbon desorption; heating by air through a heat exchanger and charging nitrogen for desorption after reaching the adsorption time, wherein the desorption time of each group is 5-6 hours, and then performing electrostatic and cooling treatment and then entering a decolorizing tank;
step four: decoloring; heating the desorbed liquid oil to 82-85 deg.C by heat exchanger, adding 0.1% decolorizing agent, stirring for 2-2.5 hr, standing for 1-1.5 hr, and deodorizing the supernatant in deodorizing tank;
step five: deodorizing; cooling the decolorized liquid oil to 34-36 ℃ by a cooler, pumping the decolorized liquid oil into a deodorization tank, stirring the decolorized liquid oil for 1-1.5 hours, and pumping the decolorized liquid oil into a temporary storage tank, wherein the addition amount of a deodorizing agent is 0.5%;
step six: temporarily storing; sealing and storing the deodorized tobacco tar.
4. A recovery process according to claim 3, characterized in that the carbon adsorption temperature in step two is 35-36 ℃.
5. The recycling method according to claim 3, wherein in the second step, before the pretreated flue gas enters the activated carbon tower, the activated carbon in the activated carbon tower is subjected to hole expansion modification.
6. The recycling method according to claim 5, wherein the reaming modification method in the second step is as follows: firstly, 2M HNO is sprayed by a spray head 3 The solution is sprayed on the surface of the activated carbon, then the temperature of the activated carbon tower is raised to 500-600 ℃, the heating rate is 1-2 ℃/min, then the temperature is rapidly raised to 900-950 ℃ of modification temperature, the modification treatment time is 60-100min, the heating rate is 20 ℃/min, the activated carbon is always in the carbon dioxide atmosphere in the modification process, the carbon dioxide flow is 2L/min, and then the temperature is lowered to the room temperature.
7. The recycling method according to claim 5, wherein in the second step, in order to prevent carbonization of the calcium chloride-loaded activated carbon, after the pore-expanding modification is performed on the activated carbon, the adsorption plate loaded with the calcium chloride-loaded activated carbon is arranged in the activated carbon tower.
8. The recovery process according to claim 3, wherein the desorption temperature in the third step is 155-160 ℃.
9. The recovery method according to claim 3, wherein the decoloring agent in the fourth step is any one of ethanolamine-amide (4).
10. The recycling method according to claim 3, characterized in that the deodorizing agent in the fifth step is selected from the group consisting of caustic soda, cobalt phthalocyanine 1.
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| CN101885486A (en) * | 2010-07-05 | 2010-11-17 | 南京林业大学 | Technology for producing acid granular activated carbon by air activation method |
| CN103434063A (en) * | 2013-08-30 | 2013-12-11 | 淄博英科医疗制品有限公司 | Two-hand mould PVC (polyvinyl chloride) glove production equipment |
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| CN113041719A (en) * | 2021-03-22 | 2021-06-29 | 蓝帆医疗股份有限公司 | Organic solvent absorption method and device for tail gas of PVC glove production process |
| CN214715530U (en) * | 2021-03-22 | 2021-11-16 | 蓝帆医疗股份有限公司 | Organic solvent absorption equipment for PVC glove production process tail gas |
| CN115382344A (en) * | 2022-07-21 | 2022-11-25 | 宁夏宁杰橡胶再生资源循环利用科技有限公司 | Rubber flue gas treatment system |
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2022
- 2022-12-15 CN CN202211608807.4A patent/CN115608104B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101885486A (en) * | 2010-07-05 | 2010-11-17 | 南京林业大学 | Technology for producing acid granular activated carbon by air activation method |
| CN103434063A (en) * | 2013-08-30 | 2013-12-11 | 淄博英科医疗制品有限公司 | Two-hand mould PVC (polyvinyl chloride) glove production equipment |
| CN110461766A (en) * | 2017-04-06 | 2019-11-15 | Ipr控股有限公司 | The method for preparing active carbon |
| CN108043216A (en) * | 2017-11-12 | 2018-05-18 | 江苏瑞尔隆鼎实业有限公司 | A kind of paint exhaust treatment device and method |
| CN113041719A (en) * | 2021-03-22 | 2021-06-29 | 蓝帆医疗股份有限公司 | Organic solvent absorption method and device for tail gas of PVC glove production process |
| CN214715530U (en) * | 2021-03-22 | 2021-11-16 | 蓝帆医疗股份有限公司 | Organic solvent absorption equipment for PVC glove production process tail gas |
| CN115382344A (en) * | 2022-07-21 | 2022-11-25 | 宁夏宁杰橡胶再生资源循环利用科技有限公司 | Rubber flue gas treatment system |
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