CN115608104B - System and method for separating water vapor and tobacco tar and recycling viscosity reducer - Google Patents
System and method for separating water vapor and tobacco tar and recycling viscosity reducer Download PDFInfo
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- CN115608104B CN115608104B CN202211608807.4A CN202211608807A CN115608104B CN 115608104 B CN115608104 B CN 115608104B CN 202211608807 A CN202211608807 A CN 202211608807A CN 115608104 B CN115608104 B CN 115608104B
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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 a water vapor tobacco tar recovery viscosity reducer. The invention sequentially removes macromolecules in the flue gas through pretreatment, organic micromolecule adsorption, carbon desorption, decoloration and deodorization to obtain the recovered viscosity reducer, and the viscosity reducer can be directly used for production, thereby greatly reducing the production cost of enterprises and relieving the general industrial diseases of unqualified flue gas emission in the production process; the method solves the problems of environmental pollution caused by overlarge smoke, human health injury, lower recovery rate and incapability of direct use; 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 additive amount, and the treated residual gas reaches the environmental protection emission standard.
Description
Technical Field
The invention relates to the field of water vapor tobacco tar treatment, in particular to a system and a method for separating a water vapor tobacco tar recovery viscosity reducer.
Background
The PVC glove industry has been a history of over thirty years, and the PVC glove itself is nontoxic and harmless. However, the PVC material itself can generate gases such as chlorine, chloroethylene, dioxin and the like after high temperature treatment, and the gases are toxic substances. If the pungent odor is emitted for a long period of time, there is a high possibility that the exhaust gas purification treatment of the plant does not reach the standard. And the quality of the plasticizer and the stabilizer added in the production process of the PVC glove does not reach the standard, and the plasticizer and the stabilizer can volatilize unpleasant odor, and the plasticizer and the stabilizer are mixed with PVC to generate toxic gases such as acetylene, hydrogen chloride, chloroethylene, sulfuric acid and the like after heating treatment, so that the body is damaged after long-term inhalation.
At present, more than 30 PVC glove manufacturers and more than 2000 production lines exist in China. Because a large amount of smog with main contents of viscosity reducer, DOTP and other glove raw materials can be generated at high temperature in the production process, the phenomena of overlarge smog, serious environmental pollution, harm to the health of workers and great waste of the production cost of enterprises generally exist in glove production workshops.
At present, most manufacturers adopt the smoke collecting device to collect the smoke, send the smoke to the cooling device through the gas pipeline, enable the temperature of the smoke to be reduced to a temperature suitable for being processed by the electrostatic smoke purifying equipment through a heat exchange mode, enable the cooled smoke to enter the smoke purifying equipment, and enable oil components such as viscosity reducers in the smoke to be changed into liquid oil to be recovered under the action of high-voltage static electricity. However, the method has the defects that firstly, the smoke treatment is not thorough, only large particles such as engine oil, DOTP and the like with lower content in the smoke can be treated, hardly any effect is achieved on the small particle viscosity reducer with highest content in the smoke, the emission standard required by PM2.5 can not be met, and the environment is seriously polluted; the second disadvantage is that the recovery rate of oil is low and the oil cannot be directly recycled so as 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 the defects of the prior art.
The invention is realized by the following technical scheme: a system for separating vapor and tobacco tar recovery viscosity reducer comprises a pretreatment system, an adsorption system, a desorption system, a decoloring system and a deodorizing system;
the pretreatment system comprises a PVC oven area, a smoke dispersing 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 activated carbon tower and a plurality of inclined plate type adsorption plates arranged in the activated carbon tower; 721 type activated carbon and activated carbon loaded with calcium chloride are alternately arranged on the inclined plate type adsorption plate.
Preferably, the activated carbon loaded with calcium chloride is lignin activated carbon.
The invention also provides a method for separating the water vapor tobacco tar recovery viscosity reducer by using the system for separating the water vapor tobacco tar recovery viscosity reducer, which comprises the following steps:
step one: pretreating to remove macromolecules in the flue gas; the method comprises the steps that high-temperature oil smoke waste gas with different temperatures at a PVC oven area, a smoke dispersing area and a PU oven outlet of a PVC glove production line is classified, collected and purified, the waste gas is conveyed into a purification system through a gas conveying pipeline, is subjected to cooling treatment through a stainless steel multi-surface pipe, passes through high-frequency high-voltage electrostatic oil mist purification equipment, filters macromolecular substances in the smoke under the action of high-voltage static electricity, and is then exhausted to an adsorption system through an induced draft fan;
step two: small molecule adsorption; the pretreated flue gas enters an activated carbon tower, the air inflow and the adsorption time are controlled by a PLC (programmable logic controller) control pneumatic butterfly valve, and the flue gas is circularly adsorbed, wherein each group of adsorption time is 22-24 hours;
step three: carbon desorption; heating the air by a heat exchanger and flushing nitrogen to desorb after reaching the adsorption time, wherein each group of desorption time is 5-6 hours, and then entering a decolorizing tank after static electricity and cooling treatment;
step four: decoloring; heating the desorbed liquid oil to 82-85 ℃ through a heat exchanger, entering a decolorizing tank, wherein the adding amount of a decolorizing agent is 0.1%, stirring the liquid oil in the decolorizing tank for 2-2.5 hours, standing the liquid oil for 1-1.5 hours, and then pumping the supernatant into a deodorizing tank for deodorizing;
step five: deodorizing; cooling the decolorized liquid oil to 34-36 ℃ through a cooler, pumping the decolorized liquid oil into a deodorizing tank, stirring for 1-1.5 hours, and pumping the decolorized liquid oil into a temporary storage tank, wherein the addition amount of the deodorizing agent is 0.5%;
step six: temporary storage; sealing and storing the deodorized tobacco tar.
Preferably, the carbon adsorption temperature in the second step is 35-36 ℃.
Preferably, 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.
Preferably, the reaming modification method in the second step comprises the following steps: the HNO of 2M is firstly sprayed through a spray header 3 Spraying the solution on the surface of the activated carbon, heating the activated carbon tower to 500-600 ℃ at a heating rate of 1-2 ℃/min, then rapidly heating to a modification temperature of 900-950 ℃, carrying out modification treatment for 60-100min at a heating rate of 20 ℃/min, enabling the activated carbon to be always in carbon dioxide atmosphere in the modification process, and cooling to room temperature at a carbon dioxide flow rate of 2L/min.
Preferably, in order to prevent carbonization of the activated carbon loaded with calcium chloride, the activated carbon is subjected to pore-enlarging modification, and then the adsorption plate loaded with the activated carbon loaded with calcium chloride is arranged in the activated carbon tower.
Preferably, the desorption temperature in the third step is 155-160 ℃.
Preferably, in the fourth step, the decoloring agent is any one of ethanol, ethanolamine, amide and ethylenediamine, wherein the ratio of ethanol to the amide is 4:3:5, and the ratio of the amide to isopropyl palmitate is 5:1:4:1.
Preferably, in the fifth step, the deodorant is caustic soda, water and cobalt phthalocyanine are respectively 1:8:0.05.
Compared with the prior art, the invention has the following advantages:
1. the viscosity reducer recovered by the invention can be directly used for production, so that the production cost of enterprises is greatly reduced, and the common industrial problem of unqualified smoke emission in the production process is relieved; the method solves the problems of environmental pollution caused by overlarge smoke, human health injury, lower recovery rate and incapability of direct use;
2. the tobacco tar treated by the method is used as a viscosity reducer, the viscosity reduction effect is better than that of the original viscosity reducer, the recovery amount accounts for more than 85% of the production additive amount, and the treated residual gas reaches the environmental protection emission 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 carbon adsorption flow chart of the present invention;
fig. 3 is a desorption flow chart of the present invention.
Detailed Description
The technical scheme of the invention is further described below by examples.
Example 1
A system for separating vapor and tobacco tar recovery viscosity reducer comprises a pretreatment system, an adsorption system, a desorption system, a decoloring system and a deodorizing system;
the pretreatment system comprises a PVC oven area, a smoke dispersing 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 activated carbon tower and a plurality of inclined plate type adsorption plates arranged in the activated carbon tower; the inclined plate type adsorption plates are adsorption plates respectively provided with active carbon and loaded with calcium chloride active carbon, and the two inclined plate type adsorption plates are arranged at intervals.
In this example, the activated carbon loaded with calcium chloride was lignin activated carbon.
Example 2
A method for separating a water vapor tobacco tar recovery viscosity reducer, comprising the following steps:
step one: pretreating to remove macromolecules in the flue gas; the PVC oven area, the scattered cigarette area of PVC gloves production line, the different temperature high temperature oil smoke waste gas of PU oven export are classified and are collected and purified, and the waste gas that volatilizees from PVC gloves production line is carried clean system through gas-supply pipeline in, earlier through unobstructed and little stainless steel multiaspect pipe cooling treatment of resistance, rethread high frequency high voltage static formula oil mist clarification plant, under the effect of high voltage static, the macromolecular class in the filtering flue gas, then by draught fan convulsions to adsorption system.
Step two: small molecule adsorption; the pretreated flue gas (the temperature is 35-36 ℃) enters into an active carbon tower, the number of active carbon towers is 18, each 3 active carbon towers is a group, the air inflow and the adsorption time are controlled by a PLC (programmable logic controller) control pneumatic butterfly valve, the cyclic adsorption is carried out, and the adsorption time of each group is 22-24 hours; as the workshops are generally 16-18 production lines, the workshop area reaches about 1 ten thousand square meters, and practice proves that the adsorption tank adopts the inclined plate type adsorption plate, the recovery oil efficiency is highest, and the effect is best.
Because of the existence of unbalanced and unsaturated molecular attraction or chemical bond on the solid surface of the active carbon, when the solid surface is contacted with gas, gas molecules can be attracted, so that the gas molecules are concentrated and kept on the solid surface, organic waste gas molecules are adsorbed in micropores in the active carbon, the organic waste gas has good adsorption effect on waste gas of benzene, alcohol, ketone, ester, gasoline and other organic solvents, pollutants are adsorbed, and the waste gas enters a dust exhaust system of equipment after passing through a filter, so that the purified gas is discharged up to the standard at high altitude.
Step three: carbon desorption; and after the adsorption time is reached, heating the air by a heat exchanger, flushing nitrogen for desorption, wherein the desorption time of each group is 5-6 hours, and then, carrying out static electricity and cooling treatment and then, entering a decolorizing tank.
The high-temperature carbonization is to make a part of organic matters adsorbed on the activated carbon boil, vaporize and desorb, and a part of organic matters undergo decomposition reaction to generate micromolecular hydrocarbon to be desorbed, and the residual components are remained in the pores of the activated carbon to form the fixed carbon. At this stage, the temperature will reach 155-160 ℃, typically under an evacuated 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 micropores of the activated carbon, so that the adsorption performance of the activated carbon is recovered, and the activation stage is the key of the whole regeneration process.
Step four: decoloring; heating the desorbed liquid oil to 82-85 ℃ by a heat exchanger, entering a decoloring tank, adding 0.1% of decoloring agent, stirring for 2-2.5 hours in the decoloring tank, standing for 1-1.5 hours, and then pumping the supernatant into a deodorizing tank for deodorizing.
The decoloring agent adopts two formulas of ethanol, ethanolamine, amide (4:3:5) or ethylenediamine, amide and isopropyl palmitate (5:1:4:1), and has ideal effect.
Step five: deodorizing; cooling the decolorized liquid oil to 34-36 ℃ by a cooler, pumping the decolorized liquid oil into a deodorizing tank, stirring for 1-1.5 hours, pumping the decolorized liquid oil into a temporary storage tank, wherein the addition amount of a deodorizing agent is 0.5%, and the deodorizing agent is caustic soda, water and cobalt phthalocyanine are 1:8:0.05.
Step six: temporary storage; sealing and storing the deodorized tobacco tar.
Example 3
When the activated carbon is desorbed, residual components are remained in the pores of the activated carbon to form fixed carbon, and micropores of the activated carbon need to be cleaned to restore the adsorption performance for recycling the activated carbon.
The difference between this example and example 2 is that the activated carbon in the activated carbon tower is subjected to hole expansion modification before the pretreated flue gas enters the activated carbon tower in step two.
However, in the experimental process of pore expansion modification, after the activated carbon is modified by carbon dioxide, the specific surface area of the mesopore of the activated carbon is obviously increased, so that the specific surface area of the activated carbon is obviously reduced, and the adsorption capacity of small organic molecules is reduced. It is therefore also necessary to control the specific surface area of the activated carbon.
The specific surface area of the activated carbon is controlled by adopting nitric acid spraying in the embodiment, and the specific operation is as follows:
first, 2M HNO is sprayed through a spray header 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 temperature raising rate is 1-2 ℃/min, then the temperature is quickly raised to 900-950 ℃, the modification treatment time is 60-100min, the temperature raising rate is 20 ℃/min, the activated carbon is always in carbon dioxide atmosphere in the modification process, the carbon dioxide flow is 2L/min, and then the temperature is reduced to room temperature.
Due to HNO 3 The strong oxidizing property of the activated carbon damages the microporous structure of the activated carbon, so that partial microporous wall collapses to form transition holes, the surface area and the pore volume are reduced, the activated carbon is subjected to secondary activation through high-temperature heat treatment, more micropores are formed in the surface functional group decomposition process, and partial micropores are ablated into mesopores, so that the number of micropores is not reduced sharply under the condition that the mesopore content is obviously increased, the pore structure of the activated carbon tends to be developed, and the surface area and the pore volume are increased.
The modification of the carbon dioxide can open the partially blocked holes of the active carbon, so that the connectivity of the active carbon hole structure is improved, and the cleaning capability is obviously improved. The activated carbon after hole enlarging 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 the second step, the inclined plate type adsorption plates are adsorption plates in which activated carbon and activated carbon loaded with calcium chloride are respectively arranged, and the two inclined plate type adsorption plates are arranged at intervals. The purpose is to recover the water and oil.
In order to prevent carbonization of the activated carbon loaded with calcium chloride, the activated carbon is subjected to pore-enlarging modification, and then the adsorption plate loaded with the activated carbon is arranged in the activated carbon tower. The activated carbon loaded with calcium chloride is lignin activated carbon, the lignin activated carbon is used for absorbing water vapor, and the absorbed water vapor is conveyed into a water storage device through a condensing pipe connected with the bottom of the inclined plate type absorbing plate for subsequent water treatment. After the adsorption is finished, the condensing tube is closed.
One of the most important preconditions of the above three embodiments is that the glove oven must be particularly well sealed and must be maintained at a negative pressure, otherwise, smoke will be caused to fly directly into the workshop, affecting the recovery rate of tobacco tar.
The foregoing describes embodiments of the present invention and is not intended to limit the scope of the invention so that further modifications and variations on the basis of the technical solutions will be apparent to those skilled in the art and remain within the scope of the invention.
Claims (8)
1. A method for separating water vapor and tobacco tar and recovering viscosity reducer is characterized by comprising the following steps:
comprises a pretreatment system, an adsorption system, a desorption system, a decoloring system and a deodorization system;
the pretreatment system comprises a PVC oven area, a smoke dispersing 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 activated carbon tower and a plurality of inclined plate type adsorption plates arranged in the activated carbon tower; activated carbon and activated carbon loaded with calcium chloride are alternately arranged on the inclined plate type adsorption plate;
the activated carbon loaded with calcium chloride is lignin activated carbon;
the recovery method of the system for separating the water vapor tobacco tar recovery viscosity reducer comprises the following steps:
step one: pretreating to remove macromolecules in the flue gas; the method comprises the steps that high-temperature oil smoke waste gas with different temperatures at a PVC oven area, a smoke dispersing area and a PU oven outlet of a PVC glove production line is classified, collected and purified, the waste gas is conveyed into a purification system through a gas conveying pipeline, is subjected to cooling treatment through a stainless steel multi-surface pipe, passes through high-frequency high-voltage electrostatic oil mist purification equipment, filters macromolecular substances in the smoke under the action of high-voltage static electricity, and is then exhausted to an adsorption system through an induced draft fan;
step two: small molecule adsorption; the pretreated flue gas enters an activated carbon tower, the air inflow and the adsorption time are controlled by a PLC (programmable logic controller) control pneumatic butterfly valve, and the flue gas is circularly adsorbed, wherein each group of adsorption time is 22-24 hours;
step three: carbon desorption; heating the air by a heat exchanger and flushing nitrogen to desorb after reaching the adsorption time, wherein each group of desorption time is 5-6 hours, and then entering a decolorizing tank after static electricity and cooling treatment;
step four: decoloring; heating the desorbed liquid oil to 82-85 ℃ through a heat exchanger, entering a decolorizing tank, wherein the adding amount of a decolorizing agent is 0.1%, stirring the liquid oil in the decolorizing tank for 2-2.5 hours, standing the liquid oil for 1-1.5 hours, and then pumping the supernatant into a deodorizing tank for deodorizing;
step five: deodorizing; cooling the decolorized liquid oil to 34-36 ℃ through a cooler, pumping the decolorized liquid oil into a deodorizing tank, stirring for 1-1.5 hours, and pumping the decolorized liquid oil into a temporary storage tank, wherein the addition amount of the deodorizing agent is 0.5%;
step six: temporary storage; sealing and storing the deodorized tobacco tar.
2. The method for separating a water vapor tobacco tar recovery viscosity reducer according to claim 1, wherein the carbon adsorption temperature in the second step is 35-36 ℃.
3. The method for separating water vapor and tobacco tar recovery viscosity reducer according to claim 1, wherein in the second step, the activated carbon in the activated carbon tower is subjected to hole expansion modification before the pretreated flue gas enters the activated carbon tower.
4. The method for separating water vapor tobacco tar recovery viscosity reducer of claim 3, wherein the reaming modification method in the second step is as follows: the HNO of 2M is firstly sprayed through a spray header 3 Spraying the solution on the surface of the activated carbon, heating the activated carbon tower to 500-600 ℃ at a heating rate of 1-2 ℃/min, then rapidly heating the activated carbon tower to a modification temperature of 900-950 ℃ for modification treatment time of 60-100min at a heating rate of 20 ℃/min, and starting the modification process of the activated carbonFinally, the mixture is placed in a carbon dioxide atmosphere, the flow rate of the carbon dioxide is 2L/min, and then the mixture is cooled to room temperature.
5. The method for separating water vapor and tobacco tar recovery viscosity reducer according to claim 3, wherein in the second step, in order to prevent carbonization of the activated carbon loaded with calcium chloride, after hole expansion modification of the activated carbon, an adsorption plate loaded with calcium chloride is disposed in the activated carbon tower.
6. The method for separating vapor tobacco tar recovery viscosity reducer of claim 1, wherein the desorption temperature in the third step is 155-160 ℃.
7. The method for separating water vapor tobacco tar recovery viscosity reducer according to claim 1, wherein the decolorizing agent in the fourth step is any one of ethanol, ethanolamine, amide and isopropyl palmitate in the ratio of 4:3:5 or ethanol, ethylenediamine, amide and isopropyl palmitate in the ratio of 5:1:4:1.
8. The method for separating water vapor tobacco tar recovery viscosity reducer according to claim 3, wherein the deodorizing agent in the fifth step is caustic soda and water and cobalt phthalocyanine are respectively 1:8:0.05.
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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 |
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| 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 |
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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 |
| 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 |
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| CN115608104A (en) | 2023-01-17 |
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