CN101143297B - Sewage storage tank exhaust air-release purification processing method - Google Patents
Sewage storage tank exhaust air-release purification processing method Download PDFInfo
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Abstract
The invention relates to a purification processing method of the discharge gas of an acid waste water tank, belongs to waste gas purification treatment technology. The invention makes the discharge gas of the acid waste water tank process two-stage purification treatment: the first stage purification treatment uses segregation liquid in the process of rich ammonia segregation in the acid waste water stripping process or stripping purified water as absorption liquid; the purification treatment in the second stage uses property stable and high boiling point solvent oil and so on as absorbent. The invention organically combines the acid waste water stripping process with the purification treatment process of the acid waste water tank discharge gas, which not only can remove the odorous substances in the acid waste water tank discharge gas, but also can effectively reclaim hydrocarbon substances. The invention has simple devices and low operation cost, and has no potential safety hazard.
Description
Technical field
The present invention relates to a kind of purifying treatment method of sewage storage tank discharging gas, in particularly a kind of petroleum refining enterprise and the part petrochemical enterprise, the purifying treatment method of the acid sewage storage tank discharging gas of sulfur compound, ammonia, volatile organic matter (VOC).
Background technology
In petroleum refining enterprise and part petrochemical enterprise, can produce a kind of sour water that contains hydrogen sulfide, organic sulfur sulfide, ammonia, volatile organic matter pollutants such as (VOC), these sewage can't directly discharge, the general steam stripping that adopts is handled and recovery hydrogen sulfide and ammonia wherein, and purifying waste water behind the stripping can be used as the fresh water (FW) reuse or enter the sewage-farm and further handle discharging.
The sour water stripping generally can adopt double tower stripping flow process and single tower stripping flow process.Double tower stripping flow process such as US3335071, US3404072 etc., single tower stripping flow process such as US3518167, CN1059291A etc.The sour water stripping process is the very ripe technical process in present technique field, extensive use in enterprise.In double tower stripping flow process, it (mainly is H that the hydrogen sulfide column overhead is discharged sour gas
2S and CO
2), it (mainly is NH that the ammonia column overhead is discharged rich ammonia vapour
3And H
2O); In single tower stripping flow process, rich ammonia vapour is extracted out from side line, and cat head is discharged sour gas.The sour gas that stripping produces generally adopts claus process further to produce sulphur.Ammonia concentration is generally 10%～30% in the rich ammonia vapour that stripping produces, and can obtain the ammonia of higher degree through 2～3 grades of fractional condensation processes, and the branch lime set that contains finite concentration ammonia is returned the stripper inlet or mixed with pending sour water; Every grade of fractional condensation can be adopted different conditions in the fractional condensation process, to improve the rate of recovery of ammonia, as described in CN1059291A.The stripper bottom is discharged stripping and is purified waste water, and can be used as the fresh water (FW) reuse or advances the sewage-farm processing.Also can add appropriate bases in the stripping process, as NaOH etc., to improve the extracting rate of ammonia, as described in CN1205983A.
In petroleum refining and petrochemical enterprise, have multiple device and discharge sour water, generally these sour waters are collected to unify the stripping purified treatment.In order to keep the steady running of stripper plant, in sour water stripping process flow process, the bigger acid water pot of one or several volumes need be set, the unified storage of pending sour water, homogeneous.These acid sewage storage tanks are generally atmospheric operation, the pneumostome that is communicated with atmosphere is arranged, thereby [s such as pollutants in sewage such as ammonia, hydrogen sulfide, organic sulfur compound, VOC are known from experience and are dispersed in the atmosphere in a large number, the severe contamination surrounding environment, be detrimental to health the corrosion production equipment.
The purifying treatment method of the raw material water tank discharging gas of Daqing Petrochemical Company oil plant sulphur recovery workshop acidic water stripping device introduced in " petroleum refining and chemical industry " 2003 02 phase P15 " sulfur-bearing, contain the technological transformation of ammonia sewage jar exhaust deodorization " literary composition, and mainly adopting with the iron complexes is the desulfurizing agent adsorption desulfurize processing of main component.The iron complexes desulfurizing agent generally has removal effect preferably to sulfide, and is limited in one's ability to removing of other odorant pollutants such as ammonia and volatile organic matter.The more important thing is, because the factors such as variation of the inside and outside gas pressure of acid water storage tank, variations in temperature and liquid level, storage tank often is in certain " breathing " state, consequently oxygen concentration is higher in the storage tank discharging gas, and iron complexes absorbs the sulfide that will change iron behind the sulfide into, oxidation can take place in the sulfide of iron in the presence of oxygen, with spontaneous combustion, and then cause other security incident when serious.Therefore, this method has bigger potential safety hazard." petrochemical industry environmental protection " 2005 the 04th phase P32～33 " the airtight deodorizing of the acid water pot of sewage stripping " literary composition introduction is adopted two-stage to absorb and is handled; the discharging gas of the acid water pot of the stripper plant of purifying waste water; it adopts special-purpose high-efficiency absorbent (unexposed composition; but as can be seen from the reaction equation that provides; comprising catalyst, oxidant etc.); by odorants such as secondary eddy flow tower absorbing and removing hydrogen sulfide, mercaptan, thioethers, do not remove the function of volatile organic matter.This method flow is comparatively complicated, needs to use special absorbent, and undesirable to the clean-up effect of hydrocarbons.
Summary of the invention
At the deficiencies in the prior art, the invention provides the purifying treatment method of the simple acid sewage storage tank discharging gas of a kind of flow process, in conjunction with the stripping process of sour water, provide a kind of can the purified treatment acid sewage storage tank discharging gas in the purifying treatment method of stench pollutant and hydrocarbons.
The purifying treatment method of acid sewage storage tank discharging gas of the present invention is on the basis of existing sour water stripping process, acid sewage storage tank discharging gas is handled through two-step purification, storage tank discharging gas at first passes through first order purified treatment, and leacheate adopts the branch lime set or the stripping of the rich ammonia vapour fractional condensation process in the sour water stripping process to purify waste water.The discharging gas that purifies through first order drip washing carries out second level purified treatment, and second level purified treatment adopts absorption pattern to reclaim the hydro carbons that discharges in the gas, and further purifies the stench pollutant.It is the stable high boiling point solvent oil of chemical property that the second level purifies absorption liquid.
In the inventive method, described sour water stripping process can be the double tower stripping process, also can be single tower stripping process.Because single tower stripping process equipment is simple, the preferred use.In the sour water stripping process, the fractional condensation process of the rich ammonia gas that stripper is extracted out is general to adopt 2 grades or 3 grades.The method of operating of sour water stripping process and condition are contents well known to those skilled in the art.Sour water is generally from the hydrogenation plant of petroleum refining, PETROLEUM PROCESSING enterprise, often subtract in distillation pressure device, coking plant, the catalytic cracking unit etc. one or more.When acid sewage storage tank sewage pH value≤9, can adopt rich ammonia vapour branch lime set is that the first order is handled leacheate; When sewage pH value＞9, can adopt stripping to purify waste water or other industry water is that the first order is handled leacheate; When having the discharging gas mixed processing of a plurality of different operating mode acid sewage storage tanks, determine the type of leacheate according to the amount of hydrogen sulfide and ammonia in the dual disposal gas, if the hydrogen sulfide amount is close to or higher than the amount (is benchmark to generate sulphur hydrogenation ammonium) of ammonia in the dual disposal gas, the branch lime set of preferred employing stripping process is a leacheate, if the amount of ammonia is greater than the amount of hydrogen sulfide, preferred employing is purified waste water and is leacheate.After the leacheate discharging that the first order is handled, can enter acid sewage storage tank and go stripping to handle.
In the inventive method, if rich ammonia vapour branch lime set is adopted in the first purification level drip washing, can adopt arbitrary fraction lime set of fractional condensation process in the stripping process, also can be that what branch lime set is mixed use.If stripping process adopts 2 grades of fractional condensation, be leacheate preferably with second level branch lime set; If stripping process adopts 3 grades of fractional condensation, be leacheate preferably with the second level and/or third level branch lime set.First order drip washing can be adopted common equipment and mode of operation and condition.Absorption equipment can be selected various suitable equipment such as Venturi absorber or packed tower for use, the preferred filler tower, leacheate sprays downwards from the packing layer top, and acid sewage storage tank discharging gas can pass through packing layer from the top down, also can pass through packing layer from bottom to top, preferred gas-liquid counter current mode.Stripping is purified waste water when doing leacheate, and preferred leacheate once passes through packed tower; When rich ammonia vapour branch lime set is done leacheate, can once pass through packed tower, also can all or part ofly recycle, can when leacheate pH value is reduced to certain limit, replenish the branch lime set in the stripping process when recycling continuously or off and on.The alkaline matter that can also add other type in the leacheate, as NaOH, sodium carbonate etc., addition is with the leacheate after absorbing, enter acid water stripping raw material water tank after, do not influence the stripper normal running and be advisable.The leacheate of discharging can enter acid sewage storage tank, also can directly enter stripper, preferably the former.It is leacheate that first order drip washing is purified waste water with stripping, is to utilize water that low concentration ammonia and hydrogen sulfide are had solvability, removes ammonia and hydrogen sulfide; First order drip washing is leacheate with rich ammonia vapour branch lime set, mainly is to utilize in the branch lime set to contain certain density ammonia, can fully absorb odorants such as hydrogen sulfide in the storage tank discharging gas, organic sulfur compound, and remove the part hydrocarbons.In order to reach desirable assimilation effect, first order drip washing operating temperature preferably is controlled at 5～50 ℃, select stainless steel, plastics or porcelain corrosion-resistant filling for use, the filler type can be Raschig ring, Pall ring, cascade ring, rectangular saddle ring, structured packing etc., the optional 20～50mm of filler nominal diameter.Packed tower structure and operation determine that by the conventional knowledge in this area be generally 2～5m as bed stuffing height, empty tower gas velocity is generally 0.2～2.0m/s, and liquid-gas ratio is generally 1～20L/m
3Adopt when dividing the lime set cycling elution, leacheate pH value is reduced to and need be changed or replenish fresh minute lime set at 7.5～9.0 o'clock.In the sour water stripping process downtime or before running well, can adopt water for industrial use, external ammoniacal liquor or contain other alkaline matter ammoniacal liquor, contain the absorption liquid of the solution of other alkaline matter as first order drip washing.Acid sewage storage tank discharging gas can be the nature discharging, also can adopt air inducing equipment to draw.
In the inventive method, the absorbent that second level purified treatment is used is the stable high boiling point solvent oil of chemical property, as distillate or the artificial oil of boiling range between 180～450 ℃, initial boiling point preferably is higher than 220 ℃, 95% distillate is lower than 420 ℃, solvent naphtha adds antioxidant, detersive to improve the stability of absorbent, helps long-term use.40 ℃ of kinematic viscosity that require absorbent simultaneously are less than 20mm
2/ s is preferably less than 10mm
2/ s, condensation point requires to be lower than-5 ℃, preferred-10～-50 ℃.
Second level purified treatment can effectively reclaim the volatile organic matter in the discharging gas, and further removes stench class material.Second level purified treatment can adopt the ordinary skill in the art, as selects for use equipment and operating condition to select in the equipment of above-mentioned first section purified treatment and operating condition scope.Absorbent can recycle or part recycles or once by using, thermal regeneration and/or decompression thermal regeneration mode are adopted in the regeneration of absorbent.Regeneration temperature is generally at 40 ℃ to 140 ℃, and preferred 60～100 ℃, regeneration pressure is generally normal pressure～1KPa (absolute pressure), preferred 2～20Kpa, and batch distillation or continuous still mode of operation are adopted in regeneration, preferred decompression distillation mode; Can load Pall ring, rectangular saddle ring, cascade ring, structured packing in the destilling tower, also column plate can be installed, less structured packing falls in preferred pressure, and structured packing is highly pressed number of theoretical plate 2～5 and determined.Decompression distillation regeneration is identical with conventional decompression distillation method of operating.
Before or after second section purified treatment, can also adopt industry water that discharging gas is purified drip washing, industry water drip washing purifies can adopt conventional method of operating, equipment and operating condition, as can in above-mentioned first order drip washing opereating specification, selecting, leacheate does not generally need cycling, the drip washing relief liquor can enter and go stripping to handle in the acid sewage storage tank again, also can enter the sewage-farm and handle.Adopt industry water to carry out drip washing and can further remove in the discharging gas and may have water soluble contaminants, reach better clean-up effect.
Remove the volatile organic matter in the waste gas, alternative method has condensation method, absorption method, absorption process and membrane separation process.Specific to this patent, requiring purified waste gas is acid sewage storage tank discharging gas.This waste gas also contains hydrogen sulfide, organic sulfur compound, ammonia, water vapour etc. except that containing volatile organic matter.Handle this waste gas if adopt condensation method, pretreatment process is very complicated, at least need to remove in advance hydrogen sulfide, ammonia, water vapour, liquid is not only arranged in the product that removes in advance, also crystallizations such as hydrogen sulfide ammonium and ice can occur, isolated these liquid or crystallization also exist volatilization again to cause the possibility of secondary pollution from system.If adopt absorption method to handle this waste gas, except that there being adsorption bed since exotherm cause also having the post processing problem of saturated adsorbent the danger such as spontaneous combustion; It is too high that the method expense is abandoned in saturated adsorbent employing, saturated adsorbent adopts method of reproduction, need be according to different adsorption mechanisms of pollutant such as hydrogen sulfide, organic sulfur compound, ammonia, volatile organic matters, adopt different desorption methods, desorption technique is very complicated, specific to the desorb of volatile organic matter, nothing more than being heating or decompression desorb, present application is based on decompression and heating and with desorb.Adopt membrane separation process, mainly have waste gas component complexity, still do not have problems such as suitable film element.Comparatively speaking, at this waste gas, absorption process is a kind of more advanced, feasible method.
The inventive method combines sour water stripping process and acid sewage storage tank discharging gas decontamination process, can reach desirable purified treatment effect.The inventive method not only can effectively be removed hydrogen sulfide, the organic sulfur compound class odorant in the sewage storage tank discharging gas, can also effectively reclaim hydrocarbons wherein.The inventive method can effectively absorb the hydrocarbons in the discharging gas on the one hand by selecting suitable lyosoption, and absorptive capacity is big simultaneously, and character is highly stable, can recycle for a long time, reduces processing cost.The inventive method equipment is simple, and operating cost is low, does not have potential safety hazard.
Description of drawings
Fig. 1 is a kind of typical process schematic diagram that sour water stripping process of the present invention combines with the acid sewage storage tank discharging gas purification process technique, wherein the sour water stripping process adopts single tower stripping process, and side line is extracted rich ammonia vapour fractional condensation process out and adopted three grades of fractional condensation technologies.
The specific embodiment
Further specify the technical process that the present invention relates to below in conjunction with accompanying drawing.
As shown in Figure 1, sour water 1-1,1-2 are pooled among acid sewage storage tank 2-1, the 2-2, and the sour water of storage tank 2-1 further flows into (two jar series connection) among the storage tank 2-2.Enter stripper 4 by pipeline 3 then, the stripper top obtains being rich in hydrogen sulfide sour gas 5 and enters other device and further handle, and the stripper bottom obtains stripping and purifies waste water and 6 can be used as the fresh water (FW) reuse or enter that handle in the sewage-farm or the drip washing that is used for acid sewage storage tank discharging gas purifies.Stripper 4 middle part side lines 7 are extracted the gas phase mixture of ammonia and water out, it is rich ammonia gas, carry out first order fractional condensation, fractional condensation gas phase 8 enters second level fractional condensation, second level fractional condensation gas phase 9 enters third level fractional condensation, third level fractional condensation gas phase 10 is the very high ammonia of purity, and further refining usually and liquefaction is commercial liquefied ammonia.First order branch lime set 11, second level branch lime set 12, the third level divide the lime set 13 can be separately or mix the leacheate that purifies elution device 14 as the first order of acid water storage tank discharging gas 15, and leacheate is discharged in the acid water storage tank after absorbing in the discharging gas odorant pollutant such as hydrogen sulfide.The discharging gas that purifies through first order drip washing enters second level elution device 16, the hydrocarbons that adopts the stable high boiling point solvent oil of chemical property to absorb wherein as absorbent 18, the absorbent 19 that has absorbed hydrocarbons enters regenerating unit 20 processing of regenerating, the hydro carbons 21 that regeneration obtains is further handled or is utilized, and the absorbent after the regeneration recycles; If solvent naphtha is a diesel oil distillate, absorb the back diesel oil distillate and can enter oil plant gas-oil jar, diesel oil is not done regeneration and handle; Discharging gas 17 behind the absorption cleaning of the second level has been eliminated odorant pollutant and hydrocarbons, substantially can qualified discharge.
Further specify the method for operating and the effect of the inventive method below by embodiment.In conjunction with existing sour water list tower stripping process, on the basis of the single tower stripping process of certain enterprise, use its side line branch lime set and stripping to purify waste water and be leacheate, carry out the present invention's experiment, single tower stripping process adopts the existing method of operating in this area, repeats no more among the application.
Embodiment 1
Certain enterprise's acid water storage tank distributes the about 1000m of tolerance
3/ h, main odorant pollutant is formed as shown in table 1.The stripper side line is extracted out and is condensed into 3 grades of condensations, and wherein the weight concentration of the fractional condensation liquefied ammonia of third level condensation is about 30%.With above-mentioned third level condensation branch lime set is the first order absorption liquid of acid water storage tank discharging gas purified treatment.Absorbent carries out hydrofinishing for the catalytic cracking diesel oil cut, distills out 250～360 ℃ distillate then, and 40 ℃ of kinematic viscosity of this absorbent are 4mm
2/ s, condensation point-20 ℃.
The main odor pollution substrate concentration of table 1 acid water storage tank discharging gas
| Main malodorant kind | Malodorant kind concentration (mg/m 3) |
| Hydrogen sulfide | 2～150 |
| Organic sulfur compound | 5～350 |
| Volatile organic matter (VOC, v%) | 5～75 |
Acid sewage storage tank adopts the two-step purification operation.Purifying column adopts packed tower, and filler is Dg50 plastics Pall rings.First order eluting column diameter 600mm, filler floor height 3000mm, leacheate is from three grades of fractional condensation systems of acid water stripping ammonia, ammonia weight concentration 30%, liquid-gas ratio 12～15L/m
3Absorption tower, second level diameter 700mm, filler floor height 4000mm, liquid-gas ratio 6～8L/m
3The first order drip washing and the second level absorb operating temperature and are controlled at 40 ℃～50 ℃.The leacheate of first order packed tower recycles in tower, enters acid water pot and replenish new branch lime set when leacheate pH value reduces to 8.5.The absorbent of second level packed tower absorbs the processing of regenerating behind the hydrocarbons, recycles after the regeneration.The relief liquor of first order drip washing enters the acid water storage tank.Table 2 is the purified treatment effects at the acid sewage storage tank discharging gas of different time monitoring.
The purified treatment condition and the clean-up effect of table 2 acid sewage storage tank discharging gas
| 1 | 22 | 25 | ＜1 | ＜1 |
| 2 | 27 | 40 | ＜1 | ＜1 |
| 3 | 105 | 65 | ＜1.5 | ＜1 |
| 4 | 70 | 45 | ＜1 | ＜1 |
| 5 | 30 | 40 | ＜1 | ＜1 |
Embodiment 2
According to embodiment 1 described method, wherein filler adopts Dg38 stainless steel rectangular saddle ring.First order eluting column diameter 600mm, filler floor height 2600mm, leacheate is from acid water stripping ammonia fractional condensation system, and for secondary divides the mixed solution of lime set and three fraction lime sets, the weight concentration of ammonia is 20%, liquid-gas ratio 12～15L/m
3Absorption tower, second level diameter 700mm, filler floor height 3500mm, absorbent are that oil atmospheric distillate separated goes out 300～380 ℃ of cuts, then through acid, alkali refining, (40 ℃ of kinematic viscosity are 30mm to add the distillate that 10 μ g/g antioxidant, 2,6 di-tert-butylphenols obtain
2/ s, condensation point-5 ℃) or saualane (isotriacontane), liquid-gas ratio 6～8L/m
3First order drip washing and second level drip washing operating temperature are controlled at 35 ℃～45 ℃.The leacheate of first order packed tower recycles in tower, replenishes new branch lime set when leacheate pH value reduces to 9.The absorbent of second level packed tower adopts conventional reduced pressure distillation technique regeneration.The relief liquor of first order drip washing all enters the acid water storage tank.Table 3 is the purified treatment effects at the acid sewage storage tank discharging gas of different time monitoring.
The purified treatment condition and the clean-up effect of table 3 acid sewage storage tank discharging gas
Claims (9)
1. the purifying treatment method of a sewage storage tank discharging gas, on the basis of existing sour water stripping process, acid sewage storage tank discharging gas is handled through two-step purification, storage tank discharging gas at first passes through first order purified treatment, and leacheate adopts the branch lime set or the stripping of the rich ammonia vapour fractional condensation process in the sour water stripping process to purify waste water; The discharging gas that purifies through first order drip washing carries out second level purified treatment, second level purified treatment adopts absorption pattern to reclaim the hydro carbons that discharges in the gas, and further purify odorant pollutant, it is the stable high boiling point solvent oil of chemical property that the second level purifies absorbent, and high boiling point solvent oil is a boiling range between 180～450 ℃ distillate.
2. in accordance with the method for claim 1, it is characterized in that described sour water stripping process is the double tower stripping process, or single tower stripping process.
3. in accordance with the method for claim 1, it is characterized in that in the described sour water stripping process that the fractional condensation process that stripper is extracted rich ammonia gas out adopts 2 grades or 3 grades.
4. in accordance with the method for claim 3, it is characterized in that when described stripping process adopts 2 grades of fractional condensation, being the leacheate of first order purified treatment with second level branch lime set; When stripping process adopts 3 grades of fractional condensation, be the leacheate of first order purified treatment with the second level and/or third level branch lime set.
5. in accordance with the method for claim 1, it is characterized in that the relief liquor that first order drip washing purifies enters acid sewage storage tank.
6. in accordance with the method for claim 4, it is characterized in that the relief liquor that first order drip washing purifies enters acid sewage storage tank.
7. in accordance with the method for claim 1, it is characterized in that described high boiling point solvent oil contains antioxidant or detersive.
8. in accordance with the method for claim 1, it is characterized in that 40 ℃ of kinematic viscosity of described high boiling point solvent oil are less than 20mm
2/ s, condensation point is lower than-5 ℃.
9. in accordance with the method for claim 1, it is characterized in that 40 ℃ of kinematic viscosity of described high boiling point solvent oil are less than 10mm
2/ s, condensation point-10～-50 ℃.
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| CN102049171B (en) * | 2009-10-27 | 2014-07-23 | 中国石油化工股份有限公司 | Method for reclaiming and treating hydrocarbon-containing waste gas |
| EP2512993B1 (en) * | 2009-12-16 | 2013-11-27 | Basf Se | Method for treating nox-containing exhaust gas from process wastewater from nitration facilities |
| DE102010002812A1 (en) * | 2010-03-12 | 2011-09-15 | Wacker Chemie Ag | Process for the disposal of hexachlorodisilane-containing vapors |
| CN102309913B (en) * | 2010-07-07 | 2015-05-13 | 中国石油化工股份有限公司 | Treatment method for stinky waste gas containing sulfides and hydrocarbons |
| CN102441314A (en) * | 2010-10-12 | 2012-05-09 | 中国石油化工股份有限公司 | Oil gas recovery method |
| CN102911704B (en) * | 2011-08-01 | 2015-02-25 | 中国石油化工股份有限公司 | Method for comprehensive oil gas recovery |
| CN102908870B (en) * | 2011-08-01 | 2015-02-18 | 中国石油化工股份有限公司 | Method for oil gas recovery |
| CN103112910B (en) * | 2013-01-23 | 2014-04-30 | 陈社庭 | Wastewater treatment tank capable of self-cleaning binding materials and wastewater thermal circulation treatment system |
| CN105498491B (en) * | 2015-12-02 | 2018-03-27 | 郑州四维特种材料有限责任公司 | It is heat-treated reaction end gas cleaning and recovering process and system |
| CN106277529B (en) * | 2016-08-31 | 2019-06-07 | 中科合成油工程股份有限公司 | H in a kind of recycling acid water2S and NH3And the method for purifying acid water |
| CN109012089B (en) * | 2018-06-28 | 2021-04-16 | 北京科技大学 | Method for capturing carbon dioxide by using potassium hydroxide and potassium carbonate |
| CN111530255B (en) * | 2020-04-30 | 2022-07-22 | 励福(江门)环保科技股份有限公司 | Venturi effect-based waste gas treatment system and method |
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| EP0013049A1 (en) * | 1978-12-28 | 1980-07-09 | Shell Internationale Researchmaatschappij B.V. | Process for acid gas removal |
| CN1059291A (en) * | 1990-08-31 | 1992-03-11 | 中国石油化工总公司抚顺石油化工研究院 | Single tower gas stripping process that a kind of band side line that reclaims sulphur and ammonia from acid sewage from oil refinery is extracted out |
| US20010048902A1 (en) * | 2000-05-01 | 2001-12-06 | Christopher Hertzler | Treatment system for removing hazardous substances from a semiconductor process waste gas stream |
| US20060104877A1 (en) * | 2004-11-12 | 2006-05-18 | Renaud Cadours | Method of deacidizing a gas with a fractional regeneration absorbent solution |
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|---|---|---|---|---|
| EP0013049A1 (en) * | 1978-12-28 | 1980-07-09 | Shell Internationale Researchmaatschappij B.V. | Process for acid gas removal |
| CN1059291A (en) * | 1990-08-31 | 1992-03-11 | 中国石油化工总公司抚顺石油化工研究院 | Single tower gas stripping process that a kind of band side line that reclaims sulphur and ammonia from acid sewage from oil refinery is extracted out |
| US20010048902A1 (en) * | 2000-05-01 | 2001-12-06 | Christopher Hertzler | Treatment system for removing hazardous substances from a semiconductor process waste gas stream |
| US20060104877A1 (en) * | 2004-11-12 | 2006-05-18 | Renaud Cadours | Method of deacidizing a gas with a fractional regeneration absorbent solution |
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