CN101239272B - Processing method of sewage storage tank discharging gas - Google Patents
Processing method of sewage storage tank discharging gas Download PDFInfo
- Publication number
- CN101239272B CN101239272B CN200710010392XA CN200710010392A CN101239272B CN 101239272 B CN101239272 B CN 101239272B CN 200710010392X A CN200710010392X A CN 200710010392XA CN 200710010392 A CN200710010392 A CN 200710010392A CN 101239272 B CN101239272 B CN 101239272B
- Authority
- CN
- China
- Prior art keywords
- storage tank
- ammonia
- sour water
- stripping
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Abstract
The present invention provides a purifying treating method of sour water storage tank discharging. The sour water storage tank discharging of the invention is purified via two purifying treatments, the first treatment employs segregating liquid or stripped purifying water of the segregating course rich in ammonia in the stripped process of the sour water as absorption liquid, the second treatment employs cooling absorption process, the cooling process employs liquid ammonia vaporization refrigeration in the sour water stripped process, ammonia after vaporization returns to the ammonia liquefying system in the stripped process, the absorption course employs at least two active carbon beds switching operation, employs steam regeneration after absorption saturation of active carbon, the active carbon absorption steam comes from a reboiler at the bottom in the course of stripped process. The invention organical combination the stripped process of the sour water and the purifying treatment process of the sour water storage tank discharging, not only removes the malodorous substance in the sour water storage tank discharging, but alos effectively recovers hydrocarbons. The process method has simple equipment, lower cost and has no potential safety hazard.
Description
Technical field
The present invention relates to a kind of processing method of acid 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, volatilization hydrocarbon etc.
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 (or through water seal connection) is arranged with atmosphere, 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.
In addition, said method can not effectively remove the volatile hydrocarbon material in the discharging gas, and this causes certain environmental pollution on the one hand, has wasted precious resources on the other hand.Traditional volatile hydrocarbon recovery technology mainly comprises three types: the one, and condensation method reclaims, and adopts two-stage or the condensation of three grades of mechanical refrigeration degree of depth, and the major part hydrocarbon condensation of volatilizing is reclaimed; The 2nd, absorption process reclaims, and adopts various The suitable solvent to absorb the volatilization hydrocarbon; The 3rd, absorption is reclaimed, and adopts various suitable solid absorbents such as charcoal absorption volatilize hydrocarbon, regeneration then.Three types technology respectively has its advantage and deficiency, on the basis of these three kinds of technology, has various improvement technologies to produce again, aspect adsorption technology, is mainly developing to some extent aspect technology and the adsorbent two.
Adopting active carbon or NACF among the CN 2597058Y is adsorbent, adopt the obvious deficiency of this type of adsorbent to be the adsorbent bed focus that exists, as what mentioned among the CN1334313A, charcoal absorption oil gas (hydrocarbon promptly volatilizees) will be emitted a large amount of heats of adsorption, thereby make charcoal generation coking phenomenon, particularly when gas concentration was higher, the bed of active carbon very easily produced the phenomenon of hot-spot, under the situation that aerobic exists, the material of adsorbent and absorption thereof has the danger that spontaneous combustion takes place.
Japanese patent laid-open 9-141039 selects for use special silica-gel as adsorbent, has eliminated the danger that spontaneous combustion takes place.But the water imbibition of silica gel is stronger, hydrone be adsorbed oil gas and have competitive Adsorption, and silica gel is behind the excessive hydrone of absorption, because expansive force makes that the rigid structure of silica gel is destroyed.In addition, the capacity of silica gel absorption oil gas is relatively low.
CN1334313A discloses the technological process that a kind of absorption-adsorption combined reclaims oil gas, further reclaims oil gas earlier by absorption recovery section oil gas, and then by absorption, realization tail gas qualified discharge.This method is two kinds of combinations that typical oil gas reclaims technology, and weak point is that flow process is longer, and operating cost is higher.CN1522785A discloses a kind of oil-gas recovery method, with oil gas compression cooling, absorbs under pressurized conditions then or absorption.The weak point of this method is that when the oil gas instability of flow, when particularly oil and gas content fluctuated widely, compressor was difficult to stable operation.And in actual applications, particularly in the improvement of oil product storage tank tidal air, tolerance alters a great deal, even the phenomenon that gas flows backwards and enters storage tank occurs, and therefore, in this case, oil gas compression cooling-absorbing process can not be suitable for.
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, fully 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 volatile hydrocarbon material.
The purifying treatment method of acid sewage storage tank discharging gas of the present invention is in conjunction with existing sour water stripping process, the sour water stripping process comprises that stripping is with tower bottom reboiler (being steam generator), rich ammonia vapour fractional condensation system, high-purity ammon liquefaction system, acid sewage storage tank discharging gas is handled through two-step purification, storage tank discharging gas is at first handled through first order washing, purifying, 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 cooled sorption process, cooling procedure adopts mechanical refrigeration, refrigeration system can be provided with the separate machine refrigeration system, also can adopt the liquefied ammonia vaporization refrigeration in the sour water stripping process, ammonia after the vaporization returns the ammoniacal liquor system in the stripping process, the preferred latter.Adsorption process adopts at least two active carbon bed handover operations, and steam regeneration is adopted in the saturated back of charcoal absorption, and active carbon is regenerated required steam can be from the steam pipe system of factory, also can be from the tower bottom reboiler of stripping process, preferably from the latter.
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, adopting rich ammonia vapour branch lime set if the first order purifies 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, simultaneously the discharge unit leacheate.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, second level purified treatment adopts cooling back charcoal absorption mode.Cooling procedure adopts mechanical refrigeration, and refrigeration system can independently be provided with, and also can adopt the liquefied ammonia vaporization refrigeration in the sour water stripping process, ammonia after the vaporization returns the ammoniacal liquor system in the stripping process, the preferred latter, the control Outlet Gas Temperature is-5～8 ℃, preferred 0～4 ℃.Return the ammoniacal liquor system in the stripping process after the ammonia evaporation, do not need to establish in addition ammonia compressor.Adsorption process adopts at least two active carbon bed handover operations, and absorption activated carbon can adopt commercially available oil gas absorption activated carbon, also can prepare according to this area commonsense method.Charcoal adsorption process adopts the common operating condition in this area, and steam regeneration is adopted in the saturated back of charcoal absorption, and active carbon is regenerated required steam can be from the steam pipe system of factory, also can be from the tower bottom reboiler of stripping process, preferably from the latter.The required liquefied ammonia amount of above-mentioned cooling and the active carbon required quantity of steam of regenerating is compared all less with the liquefied ammonia amount that stripping process obtains with required quantity of steam, in the normal operation range of equipment, do not influence the normal running of stripping process, reduced number of devices, reduced cost.
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 directly adopt absorption method to handle this waste gas, there is adsorption bed because exotherm causes danger such as spontaneous combustion.Adopt membrane separation process, mainly have waste gas component complexity, still do not have problems such as suitable film element.
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 is by fully combining sour water stripping process and acid sewage storage tank discharging gas decontamination process, particularly make full use of liquefied ammonia and steam in the stripping process, guaranteed the purified treatment effect of discharging gas on the one hand, save equipment on the other hand, reduced equipment investment and operating 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 treatment process, and 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 is pooled in the acid sewage storage tank 2, the sour water of storage tank 2 enters stripper 4 by pipeline 3 (being further divided into cold feed and hot feed usually), the stripper top obtains being rich in hydrogen sulfide sour gas 5 and enters the further processing of other device, 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, and some stripping is purified waste water and entered tower bottom reboiler (being steam generator) and produce stripping steam.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 is carried out second level fractional condensation, second level fractional condensation gas phase 9 is carried out third level fractional condensation, third level fractional condensation gas phase 10 is the very high ammonia of purity, and ammonia is liquefied ammonia 15 by liquefaction system 14 liquefaction.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 16 as the first order of acid water storage tank discharging gas, 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 cooling device 17, and refrigerant adopts the part of liquefied ammonia 15, and liquefied ammonia loops back liquefaction system 14 after evaporating and becoming gaseous state in cooling device 17; Cooling device 17 also can be to overlap independently refrigeration system.Cooled discharging gas enters absorbent charcoal adsorber 18,19, adopt two adsorbent equipments to carry out handover operation, saturated vapor regeneration is adopted in the saturated back of acticarbon, the saturated vapor temperature is 150 ℃～175 ℃, and water vapour is from the tower bottom reboiler 20 of stripper 4 or the steam pipe system of factory.
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.
The first order adopts the filler purifying column, 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 4～8L/m
3
In the cooling absorption of the second level, refrigerant adopts the liquefied ammonia in the stripping process, and control cooler outlet discharging temperature degree is 0 ℃, and the condensed water that cooler produces enters oil-containing sewage treatment system, and adsorbent adopts the common commercially available hydrocarbon active carbon that takes off, and design airspeed is 500h
-1, two adsorption towers switch use, and adsorbent bed maximum temperature is about 50 ℃, switches regeneration when absorption back gaseous contamination substrate concentration surpasses the existing discharge standard of air pollutants of China.The saturated vapor more than 150 ℃ is used in regeneration, the regeneration tower bottom reboiler of water vapour from stripping process.The regeneration emission gases is condensed into oil-water two-phase by recirculated water, and oil phase reclaims, and water removes oil-containing sewage treatment system.NMHC concentration is less than 120mg/m in the Purge gas
3, ordorless smell meets discharging standards.
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) | 5～75v％ |
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
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 5～10L/m
3
In the cooling absorption of the second level, refrigerant adopts the liquefied ammonia in the stripping process, and control outlet discharging temperature degree is 3 ℃, and the condensed water that cooler produces enters oil-containing sewage treatment system, and adsorbent adopts the common commercially available hydrocarbon active carbon that takes off, and design airspeed is 600h
-1, two adsorption towers switch use, and adsorbent bed maximum temperature is about 52 ℃, switches regeneration when absorption back gaseous contamination substrate concentration surpasses the existing discharge standard of air pollutants of China.The saturated vapor more than 150 ℃ is used in regeneration, the regeneration tower bottom reboiler of water vapour from stripping process.The regeneration emission gases is condensed into oil-water two-phase by recirculated water, and oil phase reclaims, and water removes oil-containing sewage treatment system.NMHC concentration is less than 120mg/m in the Purge gas
3, ordorless smell meets discharging standards.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 purification method of a sewage storage tank discharging gas, in conjunction with existing sour water stripping process, the sour water stripping process comprises that stripping is with tower bottom reboiler, rich ammonia vapour fractional condensation system, high-purity ammon liquefaction system, it is characterized in that acid sewage storage tank discharging gas is through the two-step purification processing, storage tank discharging gas is at first handled through first order washing, purifying, 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 cooled sorption process, and adsorption process adopts at least two active carbon bed handover operations, and steam regeneration is adopted in the saturated back of charcoal absorption; In the cooled sorption process of described second level purified treatment, cooling procedure adopts the liquefied ammonia sweat cooling mode in the acid water stripping process, and the ammonia after the vaporization returns the ammoniacal liquor system in the stripping process; Described second level purified treatment adopts in the cooled sorption process, and the steam of the saturated back of charcoal absorption steam regeneration is from the tower bottom reboiler of stripping process.
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. according to claim 1 or 2 described methods, it is characterized in that in the described sour water stripping process that the fractional condensation process of the rich ammonia gas that stripper is extracted out adopts 2 grades or 3 grades.
4. in accordance with the method for claim 1, it is characterized in that when acid sewage storage tank sewage pH value≤9 that adopting rich ammonia vapour branch lime set is that the first order is handled leacheate; When sewage pH value＞9, adopt stripping to purify waste water or other industry water is that the first order is handled leacheate.
5. in accordance with the method for claim 1, it is characterized in that described first order purified treatment selects Venturi absorber or packed tower for use.
6. in accordance with the method for claim 1, it is characterized in that described first order purified treatment operating temperature is controlled at 5～50 ℃, select stainless steel, plastics or porcelain corrosion-resistant filling for use, empty tower gas velocity is 0.2～2.0m/s, and liquid-gas ratio is 1～20L/m
3
7. in accordance with the method for claim 1, it is characterized in that in the cooled sorption process of described second level purified treatment that cooling procedure control Outlet Gas Temperature is-5～8 ℃.
8. in accordance with the method for claim 1, it is characterized in that described second level purified treatment adopts in the cooled sorption process, the saturated-steam temperature of the saturated back of charcoal absorption steam regeneration is 150 ℃～175 ℃.
9. in accordance with the method for claim 7, it is characterized in that described coolant outlet temperature is controlled to be 0～4 ℃.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200710010392XA CN101239272B (en) | 2007-02-09 | 2007-02-09 | Processing method of sewage storage tank discharging gas |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN200710010392XA CN101239272B (en) | 2007-02-09 | 2007-02-09 | Processing method of sewage storage tank discharging gas |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101239272A CN101239272A (en) | 2008-08-13 |
| CN101239272B true CN101239272B (en) | 2010-07-21 |
Family
ID=39931267
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200710010392XA Active CN101239272B (en) | 2007-02-09 | 2007-02-09 | Processing method of sewage storage tank discharging gas |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101239272B (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014080230A1 (en) * | 2012-11-26 | 2014-05-30 | Mast Carbon International Ltd | Carbon materials and their use |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102908882B (en) * | 2011-08-01 | 2015-06-17 | 中国石油化工股份有限公司 | Treatment method for emissions of sour water storage tank |
| CN104548882B (en) * | 2014-12-02 | 2016-06-01 | 北京空间飞行器总体设计部 | The dry detoxified device of toxic gas |
| CA3068058C (en) | 2017-06-27 | 2023-08-22 | Ecolab Usa Inc. | Non-phosphorous transition metal control in laundry applications |
| CN107606964A (en) * | 2017-10-31 | 2018-01-19 | 济南华闻节能工程技术有限公司 | A kind of low pressure exhaust steam recycling system for sulfuration process |
| CN108689441A (en) * | 2018-05-21 | 2018-10-23 | 山东京博石油化工有限公司 | A kind of sewage stripping system and its water storage device |
Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4066423A (en) * | 1976-09-27 | 1978-01-03 | Ht Management Company | Adsorption-absorption vapor recovery system |
| CN1022606C (en) * | 1990-08-31 | 1993-11-03 | 中国石油化工总公司抚顺石油化工研究院 | Single-tower gaseous extracting method with side-draw for recovering sulfur and ammonia from acidic waste water of oil refinery |
| JP2003001061A (en) * | 2001-06-19 | 2003-01-07 | Air Water Inc | Method of concentrating carbon dioxide in combustion gas |
| JP2003170021A (en) * | 2001-12-07 | 2003-06-17 | Nippon Soda Co Ltd | Method for cleaning exhaust ags and decomposition treatment facility of hardly decomposable halogen compound |
| CN2808275Y (en) * | 2005-05-31 | 2006-08-23 | 上海慎江机械设备有限公司 | Offensive odor treatment device |
-
2007
- 2007-02-09 CN CN200710010392XA patent/CN101239272B/en active Active
Patent Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4066423A (en) * | 1976-09-27 | 1978-01-03 | Ht Management Company | Adsorption-absorption vapor recovery system |
| CN1022606C (en) * | 1990-08-31 | 1993-11-03 | 中国石油化工总公司抚顺石油化工研究院 | Single-tower gaseous extracting method with side-draw for recovering sulfur and ammonia from acidic waste water of oil refinery |
| JP2003001061A (en) * | 2001-06-19 | 2003-01-07 | Air Water Inc | Method of concentrating carbon dioxide in combustion gas |
| JP2003170021A (en) * | 2001-12-07 | 2003-06-17 | Nippon Soda Co Ltd | Method for cleaning exhaust ags and decomposition treatment facility of hardly decomposable halogen compound |
| CN2808275Y (en) * | 2005-05-31 | 2006-08-23 | 上海慎江机械设备有限公司 | Offensive odor treatment device |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2014080230A1 (en) * | 2012-11-26 | 2014-05-30 | Mast Carbon International Ltd | Carbon materials and their use |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101239272A (en) | 2008-08-13 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101143297B (en) | Sewage storage tank exhaust air-release purification processing method | |
| Abatzoglou et al. | A review of biogas purification processes | |
| CN101898071B (en) | Method for treating sulfur- and hydrocarbon-containing foul waste gas | |
| CN205461670U (en) | Storage tank discharged waste gas's deep purification recovery unit | |
| CN101287691B (en) | Process and apparatus for the purification of methane rich gas streams | |
| CN102309913B (en) | Treatment method for stinky waste gas containing sulfides and hydrocarbons | |
| CN101239272B (en) | Processing method of sewage storage tank discharging gas | |
| KR101207532B1 (en) | Apparatus for performing drying and removing impurities process of bio-methane at high purity bio-methane purification system | |
| CA2437120A1 (en) | Carbon dioxide recovery plant | |
| CN102309914A (en) | Treatment method for stinky waste gas discharged by storage tank | |
| KR20010049511A (en) | System for recovering carbon dioxide from a lean feed | |
| CN101352653B (en) | Low-temperature micro-oxygen purification method for removing harmful gas in yellow phosphorus tail gas | |
| US11724229B2 (en) | Process and plant for removing disruptive components from raw synthesis gas | |
| CN102553390A (en) | Process for purifying chemical tail gas | |
| CN108380001B (en) | Storage tank area protection nitrogen recycling system and method | |
| CN102039077A (en) | Method for treating malodorous waste gas containing hydrocarbon | |
| CN110585861A (en) | Coking waste gas treatment system and treatment method | |
| CN1137753C (en) | Process for removing CO2 and H2S from biological gas | |
| CN101239271B (en) | Cleaning treatment method of acid sewage storage tank discharging gas | |
| CN102908882B (en) | Treatment method for emissions of sour water storage tank | |
| CN203549850U (en) | Organic waste gas comprehensive disposal system | |
| CN107774092A (en) | A kind of method of sorption extraction separation and purification | |
| CN101973603B (en) | Desorption method for reutilization of desorption agent | |
| CN102784552A (en) | Combined processing system and method for sulfur, nitrogen-containing waste water and exhaust gas in hydrogenation refining process | |
| CN87107783A (en) | Sulphur Dioxide or be reduced into the technology of elementary sulfur |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant |