CN111569613A - Device and method for eluting trace siloxane in organic silicon hydrolyzed HCl gas - Google Patents
Device and method for eluting trace siloxane in organic silicon hydrolyzed HCl gas Download PDFInfo
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- CN111569613A CN111569613A CN202010457467.4A CN202010457467A CN111569613A CN 111569613 A CN111569613 A CN 111569613A CN 202010457467 A CN202010457467 A CN 202010457467A CN 111569613 A CN111569613 A CN 111569613A
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1487—Removing organic compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1493—Selection of liquid materials for use as absorbents
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- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B7/00—Halogens; Halogen acids
- C01B7/01—Chlorine; Hydrogen chloride
- C01B7/07—Purification ; Separation
- C01B7/0706—Purification ; Separation of hydrogen chloride
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/205—Other organic compounds not covered by B01D2252/00 - B01D2252/20494
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/26—Halogens or halogen compounds
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The invention discloses a device and a method for eluting trace siloxane in organic silicon hydrolyzed HCl gas. The method comprises the following steps: 1) the siloxane-containing HCl gas enters from the bottom of the absorption tower and is in countercurrent contact with an absorbent, and the absorbent comprises at least one high-cyclic siloxane and/or at least one linear siloxane; 2) the HCl gas is ejected out of the absorption tower and then sent to a post demister to obtain qualified HCl gas; 3) and (3) supplementing a fresh absorbent from an inlet of the top of the absorption tower, and delivering the absorbent in the absorption tower and the liquid collected by the rear demister to an organic silicon hydrolysis system for regeneration treatment after being converged. The device provided by the invention does not need to be specially additionally provided with refrigeration equipment, is simple and energy-saving, and the elution method provided by the invention has strong absorption selectivity, greatly improves the stability of a chloromethane synthesis system, and relieves or eliminates the problem of equipment blockage.
Description
Technical Field
The invention relates to an organic silicon hydrolysis technology, in particular to a device and a method for eluting trace siloxane in organic silicon hydrolysis HCl gas.
Background
With the continuous progress and development of the technology of the organosilicon industry, the original chlorosilane constant boiling concentrated acid hydrolysis process is gradually replaced by an advanced concentrated acid hydrolysis process. However, the problem of HCl gas carrying oil is another difficult problem which troubles the production of enterprises. If concentrated acid is used for hydrolyzing HCl in the production of synthesizing chloromethane by a liquid phase method, trace siloxane contained in the gas is subjected to crosslinking and curing under the combined action of high temperature and a catalyst to form white solid slag. The existence of the solid directly causes the reduction of the catalytic activity, and the blockage of system equipment is caused when the catalytic activity is serious, so that the stability and the long-period operation of the system are restricted, and the problems of long shutdown cleaning time, high operation and maintenance cost and the like exist.
Although there are reports about related technologies for removing trace siloxane existing in hydrolyzed HCl gas throughout China and abroad, there is no mature and effective method, and currently, the feasible and widely adopted method is as follows:
1. gas-liquid entrainment heterogeneous separation technology
Currently, the industry uses a large number of mechanical separation methods to trap siloxane droplets in hydrolyzed HCl gas. A high-precision wire mesh demister or coalescer with critical separation particle size of 1-5 mu m and demisting efficiency of more than 99.5% is arranged in the process device, the content of liquid siloxane in the separated gas is less than 10ppm, and siloxane in the form of liquid drops in HCl gas is thoroughly separated.
2. Gas homogeneous phase separation technology
The organic silicon hydrolysate belongs to VOC (volatile organic compounds) and is relatively complex in components, wherein the mass content of volatile components (normal-temperature saturated vapor pressure P is more than or equal to 133.32Pa), D3 (hexamethylcyclotrisiloxane, the same below) and D4 (octamethylcyclotetrasiloxane, the same below) is about 21-25%, and the VOC in the hydrolyzed HCl gas is siloxane gas.
For siloxanes present in the gaseous state, the methods commonly used and available in industry are: a cryocondensation/freezing technique; b liquid (low temperature concentrated hydrochloric acid/hydrolysate) washing technology; c, chemical absorption technology; d porous material adsorption technology. The advantages and the disadvantages of each process scheme are as follows:
cryocondensation/freezing techniques: incomplete separation and high energy consumption. By adopting a low-temperature condensation/refrigeration technology, the oil content of the gas phase is reduced by 15-20%, and the energy consumption is increased by about 50%.
Liquid washing technology: isothermal washing does not have gas purification capacity, and low-temperature washing process has high energy consumption and low absorption efficiency. The low-temperature concentrated hydrochloric acid is used as a washing agent, and the siloxane cannot be removed because the hydrochloric acid cannot dissolve the siloxane. When the hydrolysate is used for washing, the absorbent and the hydrolysate in the system have basically the same composition and small driving force in the mass transfer process, so that the siloxane gas is weak in dissolving and absorbing effect and only a small amount of oil drops in the gas can be trapped.
Chemical absorption technology: the reaction speed is slow, the reaction requires long residence time, the reaction volume of equipment is required to be large, the crystallization of reactants can cause the blockage of the equipment, and the purification capability is poor.
The microporous material adsorption technology comprises the following steps: low adsorption capacity, poor selectivity, short service life, and difficult disposal of the regeneration gas. The adsorption materials commonly used at present comprise modified silica gel, activated carbon, molecular sieves, activated alumina and the like, and the adsorbent is generally regenerated by high-temperature desorption.
Therefore, no matter which scheme is adopted, the effect of removing the gaseous siloxane in the HCl gas is not obvious, and the feasibility of removing trace siloxane from the HCl gas is not realized in industry.
Disclosure of Invention
The invention aims to provide an HCl deoiling device and method using at least one high-cyclic siloxane and/or at least one linear siloxane as an absorbent, and finally, the content of siloxane in HCl gas is reduced to be below 250ppm through selecting the absorbent and developing a matched process scheme and equipment, so that various problems restricting the operation of the conventional stable system are solved, and the operation efficiency of the system is improved.
In order to achieve the above purpose, the invention is realized by the following technical scheme:
on one hand, the invention provides an elution device for trace siloxane in organosilicon hydrolysis HCl gas, which comprises an absorption tower, an absorbent circulating pump and a rear demister, wherein the top of the absorption tower is connected to a gas inlet of the rear demister through a pipeline, the bottom of the absorption tower is provided with a hydrolysis HCl gas inlet, and the absorbent circulating pump is circularly connected with the absorption tower.
Compared with the prior art, the invention has the beneficial effects that: compared with the existing condensing/freezing scheme and the scheme of low-temperature hydrochloric acid and hydrolysate washing, the special additional refrigeration equipment is not needed, and the energy is saved by more than 85 percent when the same oil removal efficiency is achieved.
Furthermore, the absorption tower is connected to the organic silicon hydrolysis system after being converged into the same pipeline with a trapping liquid outlet of the rear demister through a tower kettle liquid level control valve.
Furthermore, the top of the absorption tower is provided with an absorbent inlet, and the absorbent inlet is provided with an absorbent inlet flow meter.
On the other hand, the invention provides an elution method of trace siloxane in organic silicon hydrolyzed HCl gas, which comprises the following steps:
1) leading out siloxane-containing HCl gas from an organosilicon hydrolysis system, entering from the bottom of an absorption tower, and carrying out countercurrent contact with an absorbent in the absorption tower, wherein the absorbent contains at least one high-cyclic siloxane and/or at least one linear siloxane;
2) the HCl gas is ejected out of the absorption tower and then sent to a post demister, and siloxane liquid drops carried in the HCl gas are separated by the post demister to obtain qualified HCl gas;
3) and continuously supplementing a fresh absorbent from an inlet at the top of the absorption tower, and when the sum c of the concentrations of volatile components D3 and D4 in the absorbent in the absorption tower is more than 5%, converging the absorbent in the absorption tower with liquid captured by a rear demister through a tower kettle liquid level control valve, and then sending the liquid to an organosilicon hydrolysis system for regeneration treatment.
Compared with the prior art, the invention has the beneficial effects that:
in the invention, a physical absorption method is adopted to absorb trace siloxane in HCl gas, the absorbent contains at least one high-cyclic siloxane and/or at least one linear siloxane, the aim of completely mutual dissolution with the siloxane in the HCl gas is realized, the content of the silicon oxygen in the purified chlorinated gas is less than 250ppm, the stability of a chloromethane synthesis system is greatly improved, the problem of equipment blockage is relieved or eliminated, the operation period of the equipment can be prolonged by more than 2 times, and the maintenance and cleaning cost is reduced by about 50%.
Further, the absorbent is obtained by rectifying and separating organic silicon hydrolysate or DMC.
Further, the boiling point t of the absorbentb＞210℃。
Further, the viscosity [ mu ] of the absorbent is 5 to 50 mPas.
Furthermore, the flow rate V of the siloxane-containing HCl gas to the absorption tower is 4000Nm3/h。
Furthermore, the temperature T in the absorption tower is-15-5 ℃, and the pressure P is-0.2 MPa.
Further, the circulation amount Q of the absorbent is 10-15 m3And h, the absorbent consumption S is 40-300 kg/h.
Drawings
FIG. 1 is a schematic diagram of a process for eluting trace siloxane in an organosilicon hydrolysis HCl gas according to an embodiment of the present invention.
FIG. 2 is a VOC content determination test apparatus.
Detailed Description
In order to make the technical solution of the present invention better understood by those skilled in the art, the following detailed description of the present invention will be made with reference to the accompanying drawings.
Referring to fig. 1, an embodiment of the present invention provides an apparatus for eluting a trace amount of siloxane in an organosilicon hydrolysis HCl gas, including an absorption tower 1, an absorbent circulation pump 2 and a rear demister 3, wherein the top of the absorption tower 1 is connected to a gas inlet of the rear demister 3 through a pipeline, a hydrolysis HCl gas inlet is formed at the bottom of the absorption tower 1, the hydrolysis HCl gas inlet is connected to an organosilicon hydrolysis system, and the absorbent circulation pump 2 is connected to the absorption tower 1 in a circulation manner.
The absorption tower 1 is connected to an organic silicon hydrolysis system after converging into the same pipeline with the catching liquid outlet of the rear demister 3 through a tower kettle liquid level control valve 4, the gas outlet of the rear demister 3 is connected to a methyl chloride synthesis system, and the tower kettle liquid level control valve 4 is matched with a liquid level self-control instrument.
The top of the absorption tower 1 is provided with an absorbent inlet, the absorbent inlet is provided with an absorbent tower inlet flow meter 5, and the absorption tower is provided with a liquid level meter (not shown in the figure).
On the other hand, the embodiment of the invention provides a method for eluting trace siloxane in organic silicon hydrolyzed HCl gas, which comprises the following steps:
1) the siloxane-containing HCl gas G1 is introduced from the organosilicon hydrolysis system, enters from the bottom of the absorption tower 1, and is in countercurrent contact with an absorbent in the absorption tower 1, wherein the absorbent contains at least one high-cyclic siloxane and/or at least one linear siloxane.
2) The HCl gas is sent to a rear demister 3 after coming out from the top of the absorption tower 1, siloxane liquid drops carried in the HCl gas are separated by the rear demister 3 to obtain qualified HCl gas G2, and the qualified HCl gas G2 can be led to a methyl chloride synthesis system to be used for synthesizing methyl chloride;
3) and continuously supplementing a fresh absorbent from an inlet at the top of the absorption tower, and when the sum c of the concentrations of volatile components D3 and D4 in the absorbent in the absorption tower is more than 5%, converging the absorbent in the absorption tower with liquid captured by a rear demister through a tower kettle liquid level control valve, and then sending the liquid to an organosilicon hydrolysis system for regeneration treatment. And a fresh absorbent is supplemented, so that a good absorption effect of the absorbent is ensured, and the concentration of the absorbent at the bottom of the tower is controlled by controlling the liquid level of the tower kettle of the absorption tower.
Furthermore, the absorbent is obtained by rectifying and separating organosilicon hydrolysate or DMC (dimethyl cyclosiloxane mixture), and is worth mentioning that the organosilicon hydrolysate is a mixture comprising cyclosiloxane and linear siloxane, DMC can be obtained by primary rectification, and high cyclosiloxane can be obtained by further rectifying DMC, that is, the absorbent and organosilicon hydrolysis HCl gas have the same source, so that the absorbent and volatile components D3 and D4 in HCl gas have good intersolubility and good absorption effect. In general, the high-cyclosiloxane refers to a cyclosiloxane composed of five rings and more than five rings, and the high-cyclosiloxane obtained by rectifying and separating an organosilicon hydrolysate or DMC (dimethylcyclosiloxane mixture) is a siloxane mixture mainly comprising D5 (decamethylcyclopentasiloxane), D6 (decadimethylcyclohexasiloxane), D7 (decatetramethylcycloheptasiloxane), and possibly accompanied by trace amounts of D3 (hexamethylcyclotrisiloxane) and D4 (octamethylcyclotetrasiloxane). Table 1 shows the specific components of the absorbent in one embodiment of the present invention:
TABLE 1 absorbent Components
| Absorbent composition | D3 | D4 | D5 | D6 | D7 | PDMS |
| Mass fraction wi | 0.0005％ | 0.00％ | 76.20％ | 22.61％ | 0.97％ | 0.22％ |
Boiling point t of absorbentbThe temperature is higher than 210 ℃, the viscosity mu of the absorbent is 5-50 mPa & s, and the gas phase partial pressure P of the absorbent is less than 5 Pa.
D3 and D4 in the hydrolysate have the lowest boiling points and the highest volatility, and D3 and D4 in the HCl gas account for about 95 percent (mass percent) of all VOCs in total, so the main components of the VOCs removed from the HCl gas are D3 and D4. The absorbent provided by the embodiment of the invention can be completely mutually soluble with volatile components D3 and D4 in HCl gas, and has the advantages of high boiling point, low volatility, good chemical stability and good absorption effect; the viscosity of the absorbent is low, and if the viscosity is too high, the power loss of the device is large, and the absorption coefficient is reduced, so that the absorption effect is influenced.
Preferably, the siloxane-containing HCl gas G1 is passed into the absorption column 1 at a flow rate V of 4000Nm3/h。
Preferably, the temperature T in the absorption tower 1 is-15 to 5 ℃, and the pressure P is-0.2 to 0.2 MPa.
PreferablyThe circulation amount Q of the absorbent is 10-15 m3And h, the absorbent consumption S is 40-300 kg/h.
Preferably, the absorption tower 1 adopts a packed tower, the air speed U of the empty tower is 0.4-0.8 m/s, and the spraying density U of liquid in the tower is 8-12 m3/m2·h-1。
In order to further test the elution effect of the method for eluting trace siloxane in the hydrolyzed HCl gas of organosilicon, the siloxane content in the HCl gas before and after elution was measured using the apparatus shown in fig. 2.
As shown in fig. 2, the VOC content test measuring device comprises a rotameter 6, a VOC absorption bottle 7 and an HCl absorption bottle 8, wherein the rotameter 6 is communicated to the VOC absorption bottle 7 through a conduit 9, the VOC absorption bottle 7 is communicated to the HCl absorption bottle 8 through a conduit 10, and the HCl absorption bottle 8 discharges tail gas through a conduit 11.
The operation specification is as follows: the HCl gas containing VOC is metered by a rotameter 6 and enters a VOC absorption bottle 7 (with the volume of 500mL) containing quantitative absorbent (250mL) through a conduit 9, and the VOC in the HCl is completely absorbed by the absorbent; unabsorbed gas enters the HCl absorption bottle 8 (500 mL capacity) through the conduit 10, HCl in the gas is completely absorbed by water, and insoluble gas is discharged through the conduit 11.
The VOC concentration in the absorption liquid before and after elution is respectively measured, the total flow of gas is measured, the VOC content omega in the HCl gas is obtained through theoretical calculation, and the calculation formula is as follows:
in the formula, 250 is the volume of the absorption liquid, mL; rhoLThe density of the absorption liquid is kg/mL; c. C1、c2Measuring the VOC mass percentage content in the absorption liquid before and after absorption by adopting a chromatograph; vGTo determine the total flow of gas through the flowmeter over a period of time, m3；ρGIs gas density, kg/m3。
Examples 1-3 below further illustrate the purification effect of the absorbent, high-cyclic siloxane, for purifying and absorbing siloxane-containing HCl gas.
Continuously supplying high-cyclosiloxane absorbent and VOC-containing HCl gas, wherein the input volume V of the VOC-containing HCl gas is 4000Nm3The operating pressure P in the absorption tower is 0.15MPa (G), the operating temperature is-5 ℃, the circulating quantity Q of the absorbent is 12m3/H, the consumption quantity S of the absorbent is 40-300 kg/H, the tower diameter DN1000, the height H of the packing layer is 5.5m, and the conjugated ring plastic random packing is 50 × 40 × 1.4.4. after the system is stabilized, the content of siloxane in HCl gas before and after elution is respectively measured by a VOC content measuring test device, and the siloxane content is shown in the table 2:
TABLE 2 comparison table of the content changes of D3, D4, D5, D6 and D7 before and after the absorption of the high-ring absorbent
High-cyclic siloxane is used as an absorbent (gas phase partial pressure is 3.6Pa), the VOC content omega in HCl gas measured before absorption is 350-500 ppm, the VOC content omega after absorption is 150-250 ppm, and the absorption rate can reach about 50%.
Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art within the scope of the present invention.
Claims (10)
1. The utility model provides an organic silicon hydrolysis HCl is micro siloxane elution device in gas, includes absorption tower, absorbent circulating pump and rearmounted defroster, its characterized in that, and absorption tower top pipe line connection to rearmounted defroster gas inlet, absorption tower bottom are equipped with hydrolysis HCl gas inlet, absorbent circulating pump and absorption tower circulating connection.
2. The device for eluting micro siloxane in HCl gas after organosilicon hydrolysis according to claim 1, characterized in that the absorption tower is connected to the organosilicon hydrolysis system after being merged into the same pipeline with the trapped liquid outlet of the post demister through the tower bottom level control valve.
3. The device for eluting the trace siloxane in the organosilicone hydrolysis HCl gas as claimed in claim 1 or 2, wherein an absorbent inlet is arranged at the top of the absorption tower, and an absorbent inlet flow meter is arranged at the absorbent inlet.
4. The elution method of trace siloxane in organic silicon hydrolyzed HCl gas is characterized by comprising the following steps of:
1) leading out siloxane-containing HCl gas from an organosilicon hydrolysis system, entering from the bottom of an absorption tower, and carrying out countercurrent contact with an absorbent in the absorption tower, wherein the absorbent contains at least one high-cyclic siloxane and/or at least one linear siloxane;
2) the HCl gas is ejected out of the absorption tower and then sent to a post demister, and siloxane liquid drops carried in the HCl gas are separated by the post demister to obtain qualified HCl gas;
3) and continuously supplementing a fresh absorbent from an inlet at the top of the absorption tower, and when the sum c of the concentrations of volatile components D3 and D4 in the absorbent in the absorption tower is more than 5%, converging the absorbent in the absorption tower with liquid captured by a rear demister through a tower kettle liquid level control valve, and then sending the liquid to an organosilicon hydrolysis system for regeneration treatment.
5. The method for eluting traces of siloxanes in organosilicon hydrolyzed HCl gas according to claim 4, characterized in that the absorbent is obtained by rectification separation of organosilicon hydrolyzate or DMC.
6. The method of claim 4, wherein the boiling point t of the absorbent is tb＞210℃。
7. The method for eluting trace siloxane in organosilicone hydrolyzed HCl gas according to claim 4, wherein the viscosity of the absorbent μ ═ 5 to 50mPa · s.
8. Method for eluting traces of siloxanes in organosilicon hydrolyzed HCl gas according to any of claims 4 to 7, characterized in that the siloxanes comprisingIntroducing HCl gas into the absorption tower at a flow rate V of 4000Nm3/h。
9. The method for eluting trace siloxane in organosilicone hydrolysis HCl gas as claimed in any one of claims 4 to 7, wherein the temperature T in the absorption tower is-15 to 5 ℃ and the pressure P is-0.2 to 0.2 MPa.
10. The method for eluting trace siloxane in organosilicone hydrolyzed HCl gas according to any one of claims 4 to 7, wherein the circulating amount Q of the absorbent is 10-15 m3And h, the absorbent consumption S is 40-300 kg/h.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112076529A (en) * | 2020-09-24 | 2020-12-15 | 南通星球石墨股份有限公司 | Device and method for removing siloxane in organic silicon byproduct hydrochloric acid |
| CN112441561A (en) * | 2020-11-26 | 2021-03-05 | 山东东岳有机硅材料股份有限公司 | Device and method for efficiently removing siloxane in chlorosilane hydrolysis byproduct hydrogen chloride |
| CN113559678A (en) * | 2021-07-31 | 2021-10-29 | 湖北兴瑞硅材料有限公司 | Evacuation tail gas absorption device and process for organic silicon vacuum unit |
| CN114011208A (en) * | 2021-10-22 | 2022-02-08 | 中石化石油工程技术服务有限公司 | Gasoline vapor recovery unit |
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Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112076529A (en) * | 2020-09-24 | 2020-12-15 | 南通星球石墨股份有限公司 | Device and method for removing siloxane in organic silicon byproduct hydrochloric acid |
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| CN113559678A (en) * | 2021-07-31 | 2021-10-29 | 湖北兴瑞硅材料有限公司 | Evacuation tail gas absorption device and process for organic silicon vacuum unit |
| CN113559678B (en) * | 2021-07-31 | 2023-07-25 | 湖北兴瑞硅材料有限公司 | Device and process for absorbing exhaust gas of organic silicon vacuum unit |
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| CN114011208B (en) * | 2021-10-22 | 2024-04-09 | 中石化石油工程技术服务有限公司 | Gasoline and oil gas recovery device |
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Application publication date: 20200825 |