CN102908874A - Method for comprehensive treatment of waste gases - Google Patents
Method for comprehensive treatment of waste gases Download PDFInfo
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- CN102908874A CN102908874A CN2012104046166A CN201210404616A CN102908874A CN 102908874 A CN102908874 A CN 102908874A CN 2012104046166 A CN2012104046166 A CN 2012104046166A CN 201210404616 A CN201210404616 A CN 201210404616A CN 102908874 A CN102908874 A CN 102908874A
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- gas
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- sodium hydroxide
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- naphtha
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- 238000000034 method Methods 0.000 title claims abstract description 31
- 239000002912 waste gas Substances 0.000 title claims abstract description 25
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims abstract description 53
- 239000007789 gas Substances 0.000 claims abstract description 53
- 238000001179 sorption measurement Methods 0.000 claims abstract description 27
- 230000003009 desulfurizing effect Effects 0.000 claims abstract description 26
- 238000010521 absorption reaction Methods 0.000 claims abstract description 25
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 claims abstract description 24
- RTZKZFJDLAIYFH-UHFFFAOYSA-N Diethyl ether Chemical compound CCOCC RTZKZFJDLAIYFH-UHFFFAOYSA-N 0.000 claims abstract description 24
- 230000020335 dealkylation Effects 0.000 claims abstract description 19
- 238000006900 dealkylation reaction Methods 0.000 claims abstract description 19
- 239000003921 oil Substances 0.000 claims abstract description 15
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 claims abstract description 11
- 229910000037 hydrogen sulfide Inorganic materials 0.000 claims abstract description 11
- 150000003568 thioethers Chemical class 0.000 claims abstract description 9
- 239000010724 circulating oil Substances 0.000 claims abstract description 5
- 239000010815 organic waste Substances 0.000 claims abstract description 5
- 238000005507 spraying Methods 0.000 claims abstract description 5
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims description 102
- 238000006477 desulfuration reaction Methods 0.000 claims description 21
- 230000023556 desulfurization Effects 0.000 claims description 21
- 229930195733 hydrocarbon Natural products 0.000 claims description 21
- 150000002430 hydrocarbons Chemical class 0.000 claims description 21
- OSGAYBCDTDRGGQ-UHFFFAOYSA-L calcium sulfate Chemical compound [Ca+2].[O-]S([O-])(=O)=O OSGAYBCDTDRGGQ-UHFFFAOYSA-L 0.000 claims description 14
- 239000004215 Carbon black (E152) Substances 0.000 claims description 10
- PMZURENOXWZQFD-UHFFFAOYSA-L Sodium Sulfate Chemical compound [Na+].[Na+].[O-]S([O-])(=O)=O PMZURENOXWZQFD-UHFFFAOYSA-L 0.000 claims description 9
- 229910052938 sodium sulfate Inorganic materials 0.000 claims description 9
- 235000011152 sodium sulphate Nutrition 0.000 claims description 9
- 238000011084 recovery Methods 0.000 claims description 6
- LSDPWZHWYPCBBB-UHFFFAOYSA-N Methanethiol Chemical compound SC LSDPWZHWYPCBBB-UHFFFAOYSA-N 0.000 claims description 5
- 238000004064 recycling Methods 0.000 claims description 5
- 230000008929 regeneration Effects 0.000 claims description 5
- 238000011069 regeneration method Methods 0.000 claims description 5
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 3
- 239000000920 calcium hydroxide Substances 0.000 claims description 3
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 3
- 238000006243 chemical reaction Methods 0.000 claims description 3
- 239000002244 precipitate Substances 0.000 claims description 3
- 229920006395 saturated elastomer Polymers 0.000 claims description 3
- 238000002336 sorption--desorption measurement Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 2
- 238000005086 pumping Methods 0.000 claims description 2
- 238000001816 cooling Methods 0.000 claims 1
- 230000000737 periodic effect Effects 0.000 claims 1
- 238000005057 refrigeration Methods 0.000 claims 1
- 150000001335 aliphatic alkanes Chemical class 0.000 abstract description 6
- 229910052799 carbon Inorganic materials 0.000 abstract description 5
- 230000000694 effects Effects 0.000 abstract description 2
- 238000003795 desorption Methods 0.000 abstract 1
- 230000000241 respiratory effect Effects 0.000 abstract 1
- KKCBUQHMOMHUOY-UHFFFAOYSA-N sodium oxide Chemical compound [O-2].[Na+].[Na+] KKCBUQHMOMHUOY-UHFFFAOYSA-N 0.000 abstract 1
- 229910001948 sodium oxide Inorganic materials 0.000 abstract 1
- 238000003860 storage Methods 0.000 description 5
- 239000000047 product Substances 0.000 description 4
- 239000003344 environmental pollutant Substances 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 238000009826 distribution Methods 0.000 description 2
- 230000029058 respiratory gaseous exchange Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- ISWSIDIOOBJBQZ-UHFFFAOYSA-N Phenol Chemical compound OC1=CC=CC=C1 ISWSIDIOOBJBQZ-UHFFFAOYSA-N 0.000 description 1
- UCKMPCXJQFINFW-UHFFFAOYSA-N Sulphide Chemical compound [S-2] UCKMPCXJQFINFW-UHFFFAOYSA-N 0.000 description 1
- 230000006326 desulfonation Effects 0.000 description 1
- 238000005869 desulfonation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 150000002170 ethers Chemical class 0.000 description 1
- 150000002576 ketones Chemical class 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- -1 naphtha Chemical compound 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- Treating Waste Gases (AREA)
Abstract
The invention relates to a comprehensive method for the treatment of organic waste gases and respiratory gases of oil tanks produced during a truck loading process so as to solve the problem on the difficulty in the achievement of a treatment effect caused by a single method when the waste gases are complex in components. The method comprises four steps of acetone and ether removal, dealkylation, wet desulphurization and dry desulphurization, corresponding components in the waste gases are removed step by step, and the method mainly comprises the steps of: sending loading gases in an absorption tower through a fan, and removing the acetone and the ether by spraying naphtha, wherein the remaining gases together with respired gases in a tank area enter an active carbon adsorption bed layer, alkane is removed through vacuum desorption and circulating oil absorption, gases which are not adsorbed by active carbon enter a desulfurizing tower, sulfides in airflow are washed off by sodium oxide, gases after the treatment of wet desulphurization enter a thioether- and mercaptan-removed active carbon tank after being dehydrated so as to remove the corresponding sulfides, and enter a hydrogen sulfide removing tank to remove hydrogen sulfide, and therefore up-to-standard emission of gases is achieved.
Description
Technical Field
The invention relates to the field of waste gas treatment, in particular to a comprehensive method for treating organic gas with complex components step by step.
Background
At present, light oil products such as gasoline and the like inevitably volatilize in the processes of storage, transportation, loading and unloading, so that not only can the resource waste be caused, but also the quality of the oil products can be reduced. In addition, the concentrated oil gas discharged into the atmosphere can cause environmental pollution and potential safety hazard.
At present, oil gas recovery devices are installed in a plurality of oil storage depots and oil refineries, and the oil gas recovery devices have many activated carbon adsorption methods, so that good effects are achieved. However, the components of the oil products loaded on the oil delivery platform of some petrochemical plants are very complex, including acetone, naphtha, phenol tar and the like besides gasoline, and the components of the generated waste gas and the breathing gas of the oil storage tank include acetone, ether, sulfide and the like besides alkane. The single treatment method is difficult to meet the emission requirements specified in the atmospheric pollutant emission standard GB16297-1996, the comprehensive emission standard for atmospheric pollutants in oil storage reservoirs GB20950-2007 and the emission standard for malodorous pollutants GB 14554-93, and the waste gas is treated by a comprehensive method.
Disclosure of Invention
The invention discloses a method for comprehensively treating waste gas, which treats each component of the waste gas step by step to ensure that the discharged gas can reach the national standard.
The invention provides a method for comprehensively treating organic waste gas, which is characterized by comprising the following steps of:
a. removing acetone and ether
Organic waste gas is pressurized by a fan and enters the front absorption tower 3, and the waste gas after acetone and ether removal enters the next step from a pipeline at the top of the front absorption tower; low-temperature naphtha is sent into the top of the front absorption tower 3 from the naphtha tank through a circulating oil pump to be sprayed down, and flows out from the bottom of the front absorption tower after absorbing acetone and ether in waste gas, and is sent back to the naphtha tank for recycling;
b. dealkane
B, combining the gas in the step a with the gas from the tank area, entering a dealkylation adsorption tank A from the bottom, and discharging the gas from the top of the dealkylation adsorption tank A after dealkylation to enter the next process; after the activated carbon in the dealkylation adsorption tank A is adsorbed and saturated, starting a vacuum pump 6, pumping out the hydrocarbons adsorbed on the surface of the activated carbon, conveying the hydrocarbons into a rear absorption tower from the bottom, and simultaneously spraying low-temperature naphtha from the top of the rear absorption tower to further absorb the hydrocarbons;
c. wet desulphurization
And c, feeding the dealkylated gas from the step b from the bottom of the desulfurization tower, spraying sodium hydroxide from the top of the desulfurization tower, and feeding the generated sodium sulfate into a sodium hydroxide regenerator to recycle the sodium hydroxide.
d. Dry desulfurization
The gas after wet desulphurization enters a thioether and mercaptan removal activated carbon tank 12 after being dewatered to remove corresponding sulfides, then enters a hydrogen sulfide removal tank 13 to remove final hydrogen sulfide,
after the treatment, the harmful components in the waste gas are basically removed and can be discharged to the atmosphere.
When the temperature of naphtha exceeds 30 ℃, naphtha is cooled by a refrigerating unit and then is recycled.
And the low-temperature naphtha is returned to the naphtha tank B for recycling by a circulating oil pump after absorbing the hydrocarbons.
When the vacuum pump desorbs the hydrocarbon removing adsorption tank A, the hydrocarbon removing adsorption tank B adsorbs in the same way, namely the hydrocarbon removing adsorption tanks A and B circularly operate in an adsorption-desorption way.
The hydrocarbons which are not completely absorbed are sent back to the hydrocarbon-removing adsorption tank A or B through a secondary recovery pipeline to be continuously adsorbed.
The step c uses two desulfurizing towers, the hydrocarbon-removed gas enters from the bottom of the desulfurizing tower A, the sodium hydroxide is sprayed from the top of the desulfurizing tower A, and the primarily desulfurized gas exits from the top of the desulfurizing tower A and enters the bottom of the desulfurizing tower B; the generated sodium sulfate flows into a sodium hydroxide regenerator A from the bottom of a desulfurizing tower A, the sodium sulfate reacts with calcium hydroxide in the regenerator to generate calcium sulfate precipitate and sodium hydroxide, the calcium sulfate is filtered by a filter and reacts again in a sodium hydroxide regenerator B, the regenerated sodium hydroxide enters from the top of the desulfurizing tower B and carries out desulfurization reaction with gas primarily desulfurized by the desulfurizing tower A, and gas secondarily desulfurized is discharged from the top of the desulfurizing tower B and enters the next process; and the sodium hydroxide is discharged from the bottom of the desulfurizing tower B and enters the top of the desulfurizing tower A to complete the circulation of the sodium hydroxide.
The activated carbon in the desulfonation activated carbon tank, the mercaptan activated carbon tank and the hydrogen sulfide removal tank is special activated carbon, the adsorption capacity is huge, the activated carbon needs to be replaced regularly, the activated carbon is mostly changed once a year, the activated carbon can be properly adjusted according to the waste gas production amount, and regeneration is not needed.
The invention can treat gas with complex components, such as waste gas generated by loading oil distribution platforms, and has higher recovery rate and lower concentration of discharged gas compared with a single method.
Drawings
FIG. 1 is a flow diagram of an apparatus for the integrated process of the present invention; wherein,
1, a fan; 2.1 naphtha tank A; 2.2 the naphtha tank B; 3 a front absorption tower; 4, a rear absorption tower; 5.1 a hydrocarbon removing adsorption tank A; 5.2 a hydrocarbon removal adsorption tank B; 6, a vacuum pump; 7 a refrigerating unit; 8.1 desulfurizing tower A; 8.2 desulfurizing tower B; 9.1 sodium hydroxide regenerator A; 9.2 sodium hydroxide regenerator B; 10 a filter; 11 sodium hydroxide storage tank; 12 removing thioether and mercaptan tanks; 13 hydrogen sulfide removal tank.
Detailed Description
The comprehensive treatment method mainly comprises 4 steps of acetone and ether removal, alkane removal, wet desulphurization and dry desulphurization.
a. Removing acetone and ether
The waste gas of loading the oil distribution platform is collected, pressurized by a fan 1, enters a front absorption tower 3, and flows from the bottom of the tower to the top of the tower. The treated waste gas enters the next step from the pipeline at the top of the front absorption tower 3. The liquid phase of the absorption tower is low-temperature naphtha, and the waste gas and the low-temperature naphtha are sprayed down from top to bottom in the front absorption tower 3. All ketones and ethers are absorbed by the low-temperature naphtha, other chemical products are partially absorbed, meanwhile, alkane is added into the waste gas, and the absorbed naphtha flows out from the bottom of the front absorption tower 3 and is sent back to the naphtha tank B2.2. The high temperature of the waste gas is also reduced by naphtha, if the temperature of the naphtha exceeds 30 ℃, the naphtha is cooled by a refrigerating unit 7, and the cooled low-temperature naphtha is pumped back to the front absorption tower 3 by another circulating oil for recycling or enters the next step for use.
b. Dealkane
Two dealkylation adsorption tanks are needed, and special active carbon for adsorbing alkane is filled in the adsorption tanks. The gas from the top of the front absorption tower 3 and the gas from the large breathing of the tank field are combined and enter the hydrocarbon-removing adsorption tank A5.1 from the bottom. The gas passes through the active carbon, the hydrocarbon substances are completely adsorbed, and the remaining hydrogen sulfide and air components pass through the bed layer from bottom to top and are discharged from the top of the dealkylation adsorption tank to enter the next process. When the activated carbon adsorbs hydrocarbons and is saturated, the vacuum pump 6 is started to pump out the hydrocarbons adsorbed on the surface of the activated carbon of the dealkylation adsorption tank A5.1 and send the hydrocarbons into the rear absorption tower 4 from the bottom, meanwhile, the low-temperature naphtha is sprayed from the top of the rear absorption tower 4, and the hydrocarbons are absorbed by the low-temperature naphtha and then are pumped back to the naphtha tank B2.2 for recycling. While the vacuum pump 6 is desorbing the dealkylation adsorption tank a5.1, the dealkylation adsorption tank B5.2 is adsorbing in the same manner, i.e., the dealkylation adsorption tanks a and B are operated cyclically in adsorption-desorption manner. The hydrocarbons which are not completely absorbed are sent back to the hydrocarbon-removing adsorption tank A or B through a secondary recovery pipeline to be continuously adsorbed. The process can remove alkane component in the waste gas.
c. Wet desulphurization
And c, the dealkylation gas from the step b enters from the bottom of the desulfurization tower, sodium hydroxide is sprayed from the top of the desulfurization tower, the dealkylation gas and the sodium hydroxide are in full contact in the desulfurization tower, sulfides in the dealkylation gas are washed away, and the generated sodium sulfate flows into a sodium hydroxide regenerator to recycle the sodium hydroxide. Here, two desulfurization towers are used, the dealkylation gas entering from the bottom of the desulfurization tower a8.1 and the sodium hydroxide being sprayed from the top thereof. The primary desulfurization gas is discharged from the top of the primary desulfurization gas and enters the bottom of a desulfurization tower B8.2; the generated sodium sulfate flows into a sodium hydroxide regenerator A9.1 from the bottom of a desulfurizing tower A8.1, the sodium sulfate reacts with calcium hydroxide in the regenerator to generate calcium sulfate precipitate and sodium hydroxide, the calcium sulfate is filtered by a filter 10 and reacts again in a sodium hydroxide regenerator B9.2 for regeneration, the regenerated sodium hydroxide enters from the top of the desulfurizing tower B8.2 and carries out desulfurization reaction with gas primarily desulfurized by the desulfurizing tower A8.1, and gas desulfurized for the second time flows out from the top of the desulfurizing tower B8.2 and enters the next process; and the sodium hydroxide is discharged from the bottom of the desulfurizing tower B8.2 and enters the top of the desulfurizing tower A8.1 to complete the circulation of the sodium hydroxide.
d. Dry desulfurization
And the gas after wet desulphurization enters a thioether and mercaptan removal activated carbon tank 12 after being dewatered, corresponding sulfides are removed, and then the gas enters a hydrogen sulfide removal tank 13 to remove the final hydrogen sulfide, and the gas reaches the standard and is discharged. The activated carbon in the two tanks is special activated carbon, the adsorption capacity is huge, the activated carbon needs to be replaced regularly, the activated carbon is mostly changed once a year, and the activated carbon can be properly adjusted according to the generation amount of waste gas without regeneration.
After 4 steps of treatment, the harmful components in the waste gas are basically removed and can be discharged to the atmosphere.
Claims (7)
1. A method for comprehensively treating organic waste gas is characterized by comprising the following steps:
a. removing acetone and ether
Organic waste gas is pressurized by a fan and enters a front absorption tower (3), and the waste gas after acetone and ether removal enters the next step from a pipeline at the top of the front absorption tower; low-temperature naphtha is sent into the top of the front absorption tower (3) from the naphtha tank through a circulating oil pump to be sprayed down, flows out from the bottom of the front absorption tower after absorbing acetone and ether in waste gas, and is sent back to the naphtha tank for recycling;
b. dealkane
B, combining the gas in the step a with the gas from the tank area large breath, entering a dealkylation adsorption tank A (5.1) from the bottom, and after dealkylation, discharging the gas from the top of the dealkylation adsorption tank A (5.1) to enter the next process; after the activated carbon in the dealkylation adsorption tank A (5.1) is adsorbed and saturated, starting a vacuum pump (6), pumping out the hydrocarbons adsorbed on the surface of the activated carbon, conveying the hydrocarbons into a rear absorption tower (4) from the bottom, and simultaneously spraying low-temperature naphtha from the top of the rear absorption tower (4) to further absorb the hydrocarbons;
c. wet desulphurization
And c, feeding the dealkylated gas from the step b from the bottom of the desulfurization tower, spraying sodium hydroxide from the top of the desulfurization tower, and feeding the generated sodium sulfate into a sodium hydroxide regenerator to recycle the sodium hydroxide.
d. Dry desulfurization
The gas after wet desulphurization enters a desulphurization ether and mercaptan activated carbon tank (12) after being dewatered to remove corresponding sulfides, then enters a hydrogen sulfide removal tank (13) to remove final hydrogen sulfide,
after the treatment, the harmful components in the waste gas are basically removed and can be discharged to the atmosphere.
2. A method according to claim 1, characterized in that the naphtha is recirculated after cooling by means of a refrigeration unit (7) when the temperature of the naphtha exceeds 30 ℃.
3. The method of claim 1, wherein the low temperature naphtha is recycled by a recycle oil pump after absorbing hydrocarbons and returned to naphtha tank B (2.2).
4. A method according to claim 3, characterized in that while the vacuum pump (6) is desorbing the de-hydrocarbon adsorber a (5.1), the de-hydrocarbon adsorber B (5.2) is adsorbing in the same way, i.e. the de-hydrocarbon adsorbers a and B are operated cyclically adsorption-desorption.
5. The method of claim 3, wherein the hydrocarbons which are not completely absorbed are sent back to the hydrocarbon-removing adsorption tank A or B through the secondary recovery line to be continuously adsorbed.
6. The process according to claim 1, characterized in that step c uses two desulfurization towers, the de-hydrocarbon gas enters from the bottom of the desulfurization tower a (8.1), the sodium hydroxide is sprayed from the top thereof, and the primarily desulfurized gas exits from the top thereof and enters the bottom of the desulfurization tower B (8.2); the generated sodium sulfate flows into a sodium hydroxide regenerator A (9.1) from the bottom of a desulfurizing tower A (8.1), the sodium sulfate reacts with calcium hydroxide in the regenerator to generate calcium sulfate precipitate and sodium hydroxide, a filter (10) filters the calcium sulfate, the calcium sulfate reacts again in a sodium hydroxide regenerator B (9.2) for regeneration, the regenerated sodium hydroxide enters from the top of the desulfurizing tower B (8.2) and carries out desulfurization reaction with gas primarily desulfurized by the desulfurizing tower A (8.1), and the gas secondarily desulfurized is discharged from the top of the desulfurizing tower B (8.2) and enters the next process; and the sodium hydroxide is discharged from the bottom of the desulfurizing tower B (8.2) and enters the top of the desulfurizing tower A (8.1) to complete the circulation of the sodium hydroxide.
7. The method of claim 1, wherein the activated carbon in both tanks is a dedicated activated carbon, having a large adsorption capacity, requiring periodic replacement, mostly once a year, and can be properly adjusted according to the amount of exhaust gas produced without regeneration.
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| Application Number | Priority Date | Filing Date | Title |
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| CN2012104046166A CN102908874A (en) | 2012-10-22 | 2012-10-22 | Method for comprehensive treatment of waste gases |
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| CN2012104046166A CN102908874A (en) | 2012-10-22 | 2012-10-22 | Method for comprehensive treatment of waste gases |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106362573A (en) * | 2016-11-30 | 2017-02-01 | 唐山绿源环保科技有限公司 | Desulfurizer and desulphurising process for mixed gas containing sulfides in diversified forms |
| CN108211750A (en) * | 2018-03-28 | 2018-06-29 | 昆山金宏二氧化碳有限公司 | The desulfurizer and method of a kind of purifying carbon dioxide |
| CN110632260A (en) * | 2019-10-23 | 2019-12-31 | 苏州世康环境技术有限公司 | Atmospheric monitoring and governing method, environmental monitoring method and platform |
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| GB832639A (en) * | 1955-12-09 | 1960-04-13 | Phillips Petroleum Co | Process for separation of gaseous mixtures |
| CN1165051A (en) * | 1997-02-25 | 1997-11-19 | 沈阳环境科学研究所 | High efficiency flue gas desulfurization technology |
| CN101077984A (en) * | 2007-07-25 | 2007-11-28 | 中国石油大学(北京) | Deep desulfurization method for liquefied petroleum gas |
| CN102489122A (en) * | 2011-12-13 | 2012-06-13 | 上海神明控制工程有限公司 | Sulfur-bearing oil and gas mixture recovery process and device |
-
2012
- 2012-10-22 CN CN2012104046166A patent/CN102908874A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| GB832639A (en) * | 1955-12-09 | 1960-04-13 | Phillips Petroleum Co | Process for separation of gaseous mixtures |
| CN1165051A (en) * | 1997-02-25 | 1997-11-19 | 沈阳环境科学研究所 | High efficiency flue gas desulfurization technology |
| CN101077984A (en) * | 2007-07-25 | 2007-11-28 | 中国石油大学(北京) | Deep desulfurization method for liquefied petroleum gas |
| CN102489122A (en) * | 2011-12-13 | 2012-06-13 | 上海神明控制工程有限公司 | Sulfur-bearing oil and gas mixture recovery process and device |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106362573A (en) * | 2016-11-30 | 2017-02-01 | 唐山绿源环保科技有限公司 | Desulfurizer and desulphurising process for mixed gas containing sulfides in diversified forms |
| CN108211750A (en) * | 2018-03-28 | 2018-06-29 | 昆山金宏二氧化碳有限公司 | The desulfurizer and method of a kind of purifying carbon dioxide |
| CN110632260A (en) * | 2019-10-23 | 2019-12-31 | 苏州世康环境技术有限公司 | Atmospheric monitoring and governing method, environmental monitoring method and platform |
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Application publication date: 20130206 |