CN101721832B - Method for treating discharged waste gas of acid water tank area - Google Patents
Method for treating discharged waste gas of acid water tank area Download PDFInfo
- Publication number
- CN101721832B CN101721832B CN2008102283476A CN200810228347A CN101721832B CN 101721832 B CN101721832 B CN 101721832B CN 2008102283476 A CN2008102283476 A CN 2008102283476A CN 200810228347 A CN200810228347 A CN 200810228347A CN 101721832 B CN101721832 B CN 101721832B
- Authority
- CN
- China
- Prior art keywords
- gas
- acid water
- tank
- storage tank
- waste 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
Landscapes
- Treating Waste Gases (AREA)
Abstract
The invention relates to a method for treating the discharged waste gas of an acid water tank area. The acid water tank area at least comprises an acid water storage tank and is provided with an acid water tank area waste gas discharge reducing system. After the acid water tank area waste gas discharge reducing system is mounted, the waste gas discharge amount of the tank area is reduced, and the waste gas processing is further carried out on the discharged waste gas. A condensing system and an adsorbing system are adopted in the waste gas processing. The acid water tank area waste gas discharge reducing system is one or more of an acid water degasification processing system, an acid water tank temperature control system, an acid water tank pH value control system, an acid water tank liquid level control system and an elastic respiratory gas bin. The method has the characteristics of less gas discharge amount of the acid water tank area, high hydrocarbon recovery rate, no secondary pollution, low energy consumption, high operation safety, and the like.
Description
Technical field
The present invention relates to a kind of improvement method of discharged waste gas of acid water tank area, particularly the improvement method of the acid water Tank Farm discharging waste gas of industries such as oil refining, chemical industry.
Background technology
The acid water Tank Farm exhaust gas discharged of industries such as oil refining, chemical industry is important foul gas pollution sources; The pollutant such as volatile hydrocarbon, hydrogen sulfide, organic sulfur compound, ammonia that wherein contains higher concentration; If do not take effectively to administer method; Serious pollution can be caused, a large amount of wastings of resources can be caused simultaneously.
The existing improvement method of this type of waste gas has several types of firing method, condensation method, bioanalysis, absorption method, chemical absorption method and combination methods etc.Foul gas is handled and is selected which kind of treatment technology actually, can take all factors into consideration according to gas source, pollutant composition, concentration, tolerance, processing requirements, operation, security and technological adaptability.
Firing method can be handled various odorant pollutants, and oxidation deodorizing is thorough.This method can be divided into three types of direct burning, flame combustion method and catalytic combustions.Directly burning is applicable to high-concentration organic waste gas.The flame combustion method usually need be with foul smell and fuel mix, and ignition temperature is generally at 600～800 ℃, and stench and total hydrocarbon clearance are near 100%.Shortcoming is to need to consider the blast bound, and fuel consumption is big, has by the substituted trend of catalytic combustion.Some refinery also utilizes the torch foul gas that directly burns usually.Catalytic combustion is under catalyst action, and organic pollution can be burnt under 200～300 ℃ of temperature, and stench and total hydrocarbon clearance can reach 99%.This method is simple to operate, efficient is high, has become a kind of important deodorization means, generally is suitable for handling low-concentration organic exhaust gas.High for hydrocarbon content, sulfide concentration big and be in the tank deck foul gas in inflammable and explosive zone, the measure of considered prevention catalyst poisoning, explosion precaution and economy.
Condensation method and freezing generally are used to reclaim higher lighter hydrocarbons of boiling point or odorant pollutant.This method is usually united use with other method, as the condensation+adsorption technology of employing is arranged in the oil gas recovery; Condensation+oxidation+adsorption technology that the chemical enterprise treatment of high concentration adopts when containing methyl disulfide (103 ℃ of boiling points), methyl mercaptan (6 ℃), methyl sulfide waste gas such as (37 ℃); To methyl disulfide, methyl sulfide condensing and recycling, the pollutant in the tail gas is further removed through oxidation and absorption.
Biological deodorization method utilizes attached to the microorganism metabolic processes on the filler, and pollutant is decomposed into CO
2, water, NO
3 -And SO
4 2-Etc. innoxious compound, have characteristics such as technology is simple, with low cost, be the technology of people's common concern.The prior biological technology is suitable for handling that source of the gas is stable, water miscible, biodegradable low concentration gas, is difficult to that processing hydrocarbons content is high, pollutant levels are high, the foul gas of complicated component.
Absorption method is utilized the intrapore surface area of adsorbent absorption odorant, be a kind of traditional, still be in the deodorization technology of developing stage.Deodorization adsorbent commonly used has active carbon, amphoteric ion-exchange resin, activated alumina, silica gel, atlapulgite etc.Wherein, active carbon has higher voidage and specific area, can effectively adsorb boiling point and be higher than 40 ℃ malodor components.For H
2S (boiling point-60.4 ℃), CO
2(78.2 ℃), methyl mercaptan (6 ℃), ammonia (33.4 ℃), propane (42.1 ℃), propylene (47.7 ℃), hydrogen sulfide (60.2 ℃), ethane (88.5 ℃), ethene (103.7 ℃), butane (0.6 ℃), pentane (36.2 ℃), isopentane (28 ℃), trimethylamine low boiling odorants such as (3 ℃).Because the adsorption capacity of absorption method is lower; And no matter saturated adsorbent is that landfill or regeneration all produce secondary pollution; The replacing of adsorbent is trouble comparatively also, so absorption method generally is used to handle the foul gas of low concentration, or as the vent gas treatment of other method.
The adsorption and oxidation method is one of developing direction of absorption method.This method is a carrier with granular active carbon or fiber-reactive charcoal etc., through flooding alkali, having the noble metal of catalytic or the additives such as composite metal oxide of iron content, processes adsorption oxidation sweetening agent, is used to remove odorants such as hydrogen sulfide and organic sulfur.Deodorizing mechanism is that water vapour exists down H
2Odorant such as S, mercaptan and alkali reaction also are adsorbed on the desulfurizing agent, and oxygen reaction generates elemental sulfur, disulphide etc. under the metal catalytic effect and in the waste gas then.This method is used in a plurality of fields such as tank deck foul gas processing.The problem that exists is that the adsorption reaction thermal discharge is big, when vulcanizing object height especially heat release violent, the influence safety in production; When steam and hydrocarbon content are high, be prone to the parcel desulfurizing agent, cause the desulfurizing agent effect to descend and lost efficacy; To form ferrous sulfide after the low or desulfurizing agent of air capacity is saturated, and because of the ferrous sulfide spontaneous combustion, have hidden peril of explosion, similarly explosion accident had taken place in some enterprise.
Absorption process can be divided into Physical Absorption method and chemical absorption method.The Physical Absorption method mainly is to be absorbent with water or diesel oil, removes water-soluble foul gas (as removing NH
3Or sulfide), but it is not up to standard to handle back gas, and employing can be used as preprocessing means seldom separately.Chemical absorption method can be divided into alkali absorb method, sour absorption process, chemical oxidization method, air catalytic oxidation method, metal ion catalysis oxidizing process etc., is widely used, and particularly the oxidizing process development is rapid, and selectable technological kind is many.
Though the most improvement that can be used for acid water tank field discharging gas of said method do not provide the suitable optimization process method that combines acid water tank field discharging gas characteristics.
Summary of the invention
The present invention provides the improvement method of a kind of acid water tank field discharging gas, the inventive method have the hydrocarbon rate of recovery high, do not produce characteristics such as secondary pollution, unit scale are little, processing safety height.
The exhaust of acid water tank field and breathing process this area are called " breathing ", and the breathing that causes of fluctuating up and down of storage tank internal cause liquid level is commonly referred to as big breathing, and the breathing that causes because of the diurnal temperature fluctuation is commonly referred to as little breathing.In large-scale acid water tank field, in operation just often, big respiratory capacity generally can be controlled in the small range, therefore, and the main cause of discharging waste gas when little breathing is the tank field normal running.Little breathing has certain rules, promptly is generally tank temperature rising in the daytime, outwards exhaust; Night, tank temperature descended, and is inwardly air-breathing; Form respiratory intermittently.Certainly, also have the exhaust of acid water storage tank and air-breathing situation under the exceptional condition to take place.The present invention is directed to Tank Farm exhaust and air-breathing rule and characteristics, design following processing procedure.
Discharged waste gas of acid water tank area improvement method of the present invention comprises following content; The acid water tank field comprises an acid water storage tank at least, and acid water tank field reducing discharge of waste gases system is set, and acid water tank field reducing discharge of waste gases system can be for following a kind of or several kinds: (1) is provided with acid water degassing treatment system; (2) acid water pot temperature control system is set; (3) acid water pot pH value control system is set, (4) are provided with acid water pot tank level control system, and (5) are provided with elasticity tidal air storehouse etc.
After acid water tank field reducing discharge of waste gases system was set, tank field toxic emission tolerance significantly reduced, and discharging waste gas is further carried out exhaust-gas treatment; Exhaust-gas treatment comprises condenser system and adsorption system; The acid water storage tank is provided with control pressurer system, when tank inner pressure is higher than environmental pressure, and the outside discharging waste gas of storage tank; Discharging waste gas gets into condenser system and reclaims condensate, gets into then and discharges after adsorption system further removes pollutant; When tank inner pressure is lower than environmental pressure when low, close the storage tank discharging gas outlet, when tank inner pressure is lower than setting value, open storage tank protection air valve, protection gas is inhaled into storage tank; When Tank Farm did not efflux waste gas, condenser system stopped refrigeration, and protection gas gets into condenser system and adsorption system, and the protection gas of process condenser system and adsorption system loops back storage tank and protects gas or get into the low pressure gas pipe network as storage tank.
In the inventive method, take the measure of proper acidic water storage tank reducing discharge of waste gases to different working conditions.For example for the acid water that produces in the hydrogenation technique process; Contain more so property and carry gas, can degassing tank be set through degassing treatment system is set; Adopt the nature degassing or gas to put forward to wait the physics mode that outgases; Get into the acid water storage tank again after the acid water degassing, the gas of deviating from can get into the low pressure gas system, and the tolerance of carrying after the acid water degassing significantly reduces.For coming under the higher or environment temperature condition with higher of coolant-temperature gage; The waste discharge tolerance of acid water storage tank will increase greatly; Lower the temperature to storage tank this moment; Can effectively reduce the storage tank discharging gas amount, the storage tank cooling can be taked the mode of shower water, and water can be underground water, running water, recirculated cooling water, greening cleaning water, qualified discharge waste water etc.The pH of acid water pot is the key factor of concentration of sulfur such as hydrogen sulfide in the influence discharging gas; PH value through control storage tank inner acidic water can effectively reduce concentration of sulfur and capacity in the discharging gas; Be provided with online or intermittently measure pH value device in the storage tank; When the pH value is lower than 7 in the storage tank, adds alkaline matter and make sewage maintenance neutrality or alkaline in the storage tank.The quick variation of liquid level also is the principal element that influences the storage tank discharging gas amount in the acid water pot; Tank level is stable in the time of should keeping normal running; Or the coordinated manipulation through a plurality of storage tanks, make total inflow suitable with the displacement maintenance the tank field in, can reduce discharge amount of exhaust gas.For the acid water storage tank, owing to be in different operating states, and the influence of storage tank day and night temperature; Consequently storage tank is in suction condition sometimes, handles the influence of exhaust condition, particularly day and night temperature sometimes; Air-breathing have certain rules with exhaust, and therefore elasticity tidal air storehouse is set, when storage tank exhaust (promptly exhaling); Elasticity tidal air storage capacity increases, and the waste gas of discharge gets in the tidal air storehouse and stores, when storage tank is air-breathing; The gas that stores in the elasticity tidal air storehouse returns storage tank again, and corresponding the reducing of volume in elasticity tidal air storehouse can be found out; Said process not only can reduce the amount of storage tank discharging waste gas, can also reduce the required protection gas consumption of storage tank.Structures such as gas holder or air bag can be adopted in elasticity tidal air storehouse, and maximum volume is confirmed according to the amount of Tank Farm discharging waste gas.
In the waste gas processing method of the present invention, condenser system is provided with 2 grades or 3 grades, and first order control condensation temperature is 0～4 ℃, and the most of water vapor condensation that mainly will discharge in the gas is removed.Based on requirement second level condensation and third level condensation are set to the volatile organic matter rate of recovery in the waste gas.Second level control condensation temperature-35～-20 ℃, about 60% volatile organic matter can condensing and recycling.Third level control condensation temperature is-70 ℃～-55 ℃, and this moment, about 80%～90% volatile organic matter can condensing and recycling, and remainder is removed in follow-up adsorption system, and Purge gas reaches the discharging standards discharging.
In the second level and third level condensation process, the water vapour in the waste gas can frosting in condenser, and sulfuration gas and ammonia in the waste gas also can generate the inorganic salts crystallization, and this will reduce the heat transfer efficiency of condenser system greatly, reduces the condensing and recycling effect, increases energy consumption.Still contain more volatile component in the condensed waste gas, like hydrocarbon, hydrogen sulfide, ammonia, organic sulfur compound etc., can qualified discharge after the process absorption.
Adsorption system can be used various suitable adsorbents, the active carbon of preferred good adsorption performance.Because condensed EGT is lower, help improving the adsorption capacity of adsorbent, the potential safety hazard of having avoided the temperature rise in the adsorption process to bring simultaneously.Waste gas is generally 300～5000h through the volume space velocity of adsorbent
-1
The protection gas of storage tank can be any oxygen-free gas, the preferred lower nitrogen of cost.Using the purpose of protection gas is the oxidation and spontaneous combustion that prevents the storage tank metal sulfide, and then causes security incidents such as burning even blast.
In the inventive method, operating feature and exhaust and air-breathing rule trend in conjunction with the acid water storage tank are provided with the reducing discharge of waste gases measure, reduce the discharge capacity of waste discharge gas.Utilize the inspiratory duration section of storage tank night cooling; Utilize protection gas to carry out the defrosting of condenser system and the regeneration of adsorption system; Defrosting and regeneration can be according to the working conditions of condenser system and adsorption system; Be provided with and carry out once every day, or per a couple of days carry out once, be generally and carried out in 1～5 day once getting final product.In some cases, storage tank also inspiratory phenomenon possibly occur in the daytime, but the general air-breathing in the daytime lasting time is shorter, should not carry out the defrosting of condenser system and the regenerative operation of adsorbent at storage tank inspiratory duration in the daytime.The specific operation process of defrosting and regeneration is following: elder generation is with the hydrops emptying of condenser system; Replace with normal temperature protection gas then; To feed the protection gas lift temperature of condenser system after the displacement, and make the condensing zone internal temperature rise to 20～60 ℃ gradually, accomplish the defrosting of condenser; The protection gas that is used to defrost through condensing zone further is warming up to 120～150 ℃ of entering adsorption systems; Adsorbent bed temperature raises and makes the material desorption of absorption; Realize the regeneration of adsorbent, behind the regeneration ending with normal temperature protection gas to adsorbent bed lower the temperature subsequent use.
The regeneration gas of discharging from adsorption system can have two whereabouts: 1. under pressure control as the additional gas of Tank Farm; 2. by the pressure of protection source of the gas, import the low pressure gas pipe network.
The general normal pressure of storage tank uses, and therefore withstand voltage ability property is relatively poor, when in general tank inner pressure is lower than environmental pressure 1000～5000Pa, need opens the protection air valve and in jar, replenish protection gas.Tank inner pressure is an environmental pressure～when being higher than environmental pressure 5000Pa, need open the gas extraction system valve to the exhaust treatment system exhaust.In order to prevent that contingency from taking place, and generally also need be provided with seal water system.
In the method for treating release gas in storage tank area of the present invention, make full use of the characteristics of Tank Farm discharging waste gas,, designed suitable governance flowchart to the concrete condition of the polluter that is contained in the discharging waste gas.Simultaneously; The defrosting of condenser system and the regeneration of sorbent system be in the supporting protection gas system of Tank Farm, the flow process of simplification, and the regeneration tail gas circulation is as storage tank protection gas or directly enter the low pressure gas pipe network; Can not produce secondary pollution, simplify processing method yet.Compared with prior art, it is simple that the inventive method has flow process, and discharge amount of exhaust gas is low, and the waste gas treatment equipment small scale is invested lowly, and the hydrocarbon rate of recovery is high, does not produce secondary pollution, handling safety, characteristics such as operation energy consumption is low.Be suitable for the purified treatment of tank field discharging gas such as acid water Tank Farm, oil product tank field.
Description of drawings
Fig. 1 is that acid water storage tank discharging gas of the present invention is administered the method flow sketch map.
The specific embodiment
Further specify the inventive method below in conjunction with accompanying drawing.
As shown in Figure 1, in the Tank Farm exhaust period, through elasticity tidal air storehouse 15 (can adopt one or more reduction of discharging measures, adopt elasticity tidal air storehouse among Fig. 1), elasticity tidal air storehouse 15 is full of the back to the exhaust treatment system discharging waste gas to Tank Farm discharging waste gas 1 earlier.Through one-level condensing zone 3, B-grade condensation district 4 and three grades of condensing zones 5, all condensing zones and refrigeration unit 2 link discharging waste gas successively.At the one-level condensing zone, condensate liquid 9 is mainly water, can further handle.At secondary and three grades of condensing zones, condensate liquid 10 is mainly organic volatile, Separation and Recovery in knockout drum 6, and the waste gas after the condensing and recycling is through adsorption system 7, and the waste gas 8 that further adsorbs behind the pollutant wherein can qualified discharge.In the air-breathing period of Tank Farm, condensing zone and storage tank block, and the gas in the elasticity tidal air storehouse 15 before elasticity tidal air storage capacity reaches minimum, need not protect gas to get into storage tank along with the air-breathing storage tank that returns of storage tank.Simultaneously, the hydrops in the emptying system, protection gas 11 gets into condenser system and (can get into from the one-level condensing zone; Preferably get into from the B-grade condensation district) and adsorption system replace; Start protection hot-air heater 12 and regenerative heater 13 then, during protection gas process condensing zone, the frosting and the solid crystal of B-grade condensation district and three grades of condensing zones are removed; During protection gas process adsorption system; With the adsorbent desorption and regeneration, the regeneration gas 14 of discharge can loop back storage tank as protection gas, also can enter the low pressure gas pipe network.
Through a specific embodiment scheme of the present invention and effect are described below.
Certain enterprise's acid water Tank Farm has 8 sewage storage tanks, carbon steel tank body, arch-roof tank.4 3000m
3Jar, 4 4500m
3Jar.Under the normal condition, the sour water amount is 160t/h, and when water was cut in the oil product tank field, sewage quantity can reach 200t/h.The time of staying of sewage in jar is generally more than 30 hours.
Acid water pot emission gases is formed as shown in table 1.
Table 1 acid water tank deck tidal air pollutant levels unit: μ L/L
| Pollutant | 2006.5.29 survey | 2006.6.2 survey |
| Hydrogen sulfide | ＜0.01 | ＜0.01 |
| Methyl mercaptan | 0.07 | 0.15 |
| Ethyl mercaptan | 0.65 | ＜0.01 |
| Methyl sulfide | 1.11 | 0.75 |
| Methyl disulfide | 13.3 | 7.25 |
| Benzene | 2.29×10 3 | 654 |
| Toluene | 433 | 137 |
| Ethylbenzene | 2.19 | Do not detect |
| Paraxylene | 1.17 | Do not detect |
| Meta-xylene | 4.05 | Do not detect |
| Ortho-xylene | 1.26 | Do not detect |
| Methane | 744 | 77.7 |
| Ethene | 341 | 25.7 |
| Ethane | 1.54×10 3 | 153 |
| Third is rare | 2.70×10 3 | 470 |
| Propane | 5.86×10 4 | 8.68×10 3 |
| Total hydrocarbon | 579000 | 181000 |
Set up in the acid water tank field under the situation of head space gas connection pipe network, calculate the maximum capacity in tank field, can calculate item by item as follows:
Call out suction tolerance=200-160=40m
3/ h.
Little breathing capacity is by 8 total gas-phase space volumes of jar, day 15 ℃ of temperature rises (20 ℃ to 35 ℃), is the temperature interval that evenly raises at 6 o'clock to 14 o'clock, and calculating little breathing capacity is 140m
3/ h.
From the gas-entrained 80m that presses of the acid water of hydrogenation plant
3/ h value.
The maximum capacity in tank field is 260m
3/ h (normal temperature and pressure).
Ordinary circumstance, this enterprise's location daily temperature is changed to: 3 point～15 temperature raises, and 15 to 3 temperature reductions next day.
Gas emissions roughly changes with temperature Change.If the gas that does not have acid water to carry secretly, generally 16 to next day 3 whole tank fields should be in suction condition, do not have gas discharging; If the acid water entrained gas scale of construction is 80m
3/ h, the tank field should just get into suction condition after 21.If the acid water degas system is set, then the about 800m of toxic emission can be reduced every day in the acid water tank field
3More than.
According to the inventive method, adopt flow process shown in Figure 1, it is 500m that maximum volume is set
3Elasticity tidal air storehouse, then reduce discharge amount of exhaust gas 500m every day
3More than, save storage tank protection gas 500m simultaneously
3More than.By maximum capacity design condenser system and adsorption system, three grades of condensing zones are set, one-level condensing zone control temperature is 2 ℃; B-grade condensation district control temperature is-30 ℃; Three grades are coagulated district's control temperature is-60 ℃, and adsorbent is common commercially available active carbon, and design airspeed is 1000h
-1Through this treatment system, the total hydrocarbon rate of recovery arrives 88% (weight), and discharging tail gas each item index all meets discharging standards.
Condensing zone defrosting and adsorbent reactivation are chosen at 22 to some next day 2, and defrosting control temperature is 50 ℃, and regeneration is controlled to be 130 ℃, and the regeneration tail gas part is as storage tank protection gas, and partial discharge is to the low pressure gas system.Once defrosted and regenerative operation in per 2 days, and can protect whole device under high efficiency, to operate.
Claims (13)
1. the improvement method of a discharged waste gas of acid water tank area; The acid water tank field comprises an acid water storage tank at least; It is characterized in that: acid water tank field reducing discharge of waste gases system is set, acid water tank field reducing discharge of waste gases system is set after, toxic emission tolerance in tank field reduces; Discharging waste gas is further carried out exhaust-gas treatment, and exhaust-gas treatment comprises condenser system and adsorption system; Described acid water tank field reducing discharge of waste gases system is following a kind of or several kinds: (1) is provided with acid water degassing treatment system; (2) acid water pot temperature control system is set; (3) acid water pot pH value control system is set, (4) are provided with acid water pot tank level control system, and (5) are provided with elasticity tidal air storehouse;
Storage tank is provided with control pressurer system, when tank inner pressure is higher than environmental pressure, and the outside discharging waste gas of storage tank, discharging waste gas gets into condenser system and reclaims condensate, gets into then and discharges after adsorption system further removes pollutant; When tank inner pressure is lower than environmental pressure, close the storage tank discharging gas outlet, when tank inner pressure is lower than setting value, open storage tank protection air valve, protection gas is inhaled into storage tank; When Tank Farm did not efflux waste gas, condenser system stopped refrigeration, and protection gas gets into condenser system and adsorption system, and the protection gas of process condenser system and adsorption system loops back storage tank and protects gas or get into the low pressure gas pipe network as storage tank.
2. according to the described method of claim 1; It is characterized in that: degassing treatment system is set, handles the acid water that produces in the hydrogenation technique process, adopt the nature degassing or gas to put forward degassing mode; Acid water degassing back gets into the acid water storage tank, and the gas of deviating from gets into the low pressure gas system.
3. according to the described method of claim 1, it is characterized in that: acid water pot temperature control system is set, handles the storage tank under the higher or higher situation of environment temperature of coolant-temperature gage, temperature control system is taked the mode of shower water.
4. according to the described method of claim 3, it is characterized in that: described shower water is underground water, running water, recirculated cooling water, greening cleaning water or qualified discharge waste water.
5. according to the described method of claim 1, it is characterized in that: acid water pot pH value control system is set, and sewage keeps neutral or alkaline in the control storage tank.
6. according to the described method of claim 1, it is characterized in that: elasticity tidal air storehouse is set, and elasticity tidal air storehouse can be with gas holder or airbag structure.
7. according to the described method of claim 1, it is characterized in that: at least 2 grades of described condenser system settings, first order control condensation temperature is 0～4 ℃, second level control condensation temperature-35～-20 ℃.
8. according to the described method of claim 7, it is characterized in that: described condenser system is provided with 3 grades, and third level control condensation temperature is-70 ℃～-55 ℃.
9. according to the described method of claim 1, it is characterized in that when described Tank Farm does not efflux waste gas being the inspiratory duration section of storage tank night cooling, utilize protection gas to carry out the defrosting of condenser system and the regeneration of adsorption system.
10. according to the described method of claim 9, it is characterized in that described defrosting and regeneration are provided with 1～5 day and carry out once.
11. according to the described method of claim 9; It is characterized in that described defrosting and regenerative process are: elder generation is with the hydrops emptying of condenser system; Replace with normal temperature protection gas then; To feed the protection gas lift temperature of condenser system after the displacement, and make the condensing zone internal temperature rise to 20～60 ℃ gradually, accomplish the defrosting of condenser; The protection gas that is used to defrost through condensing zone further is warming up to 120～150 ℃ of entering adsorption systems, and adsorbent bed temperature raises and makes the material desorption of absorption, realizes the regeneration of adsorbent.
12., when it is characterized in that tank inner pressure is lower than environmental pressure 1000～5000Pa, open the protection air valve and in jar, replenish protection gas according to the described method of claim 1.
13., it is characterized in that tank inner pressure is an environmental pressure～when being higher than environmental pressure 5000Pa, open the gas extraction system valve to the exhaust treatment system exhaust according to the described method of claim 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008102283476A CN101721832B (en) | 2008-10-28 | 2008-10-28 | Method for treating discharged waste gas of acid water tank area |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2008102283476A CN101721832B (en) | 2008-10-28 | 2008-10-28 | Method for treating discharged waste gas of acid water tank area |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101721832A CN101721832A (en) | 2010-06-09 |
| CN101721832B true CN101721832B (en) | 2012-02-29 |
Family
ID=42443751
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN2008102283476A Active CN101721832B (en) | 2008-10-28 | 2008-10-28 | Method for treating discharged waste gas of acid water tank area |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN101721832B (en) |
Families Citing this family (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102463032A (en) * | 2010-11-04 | 2012-05-23 | 中国石油化工股份有限公司 | Treatment method of acid water head space gas |
| CN104139938B (en) * | 2014-08-01 | 2016-08-24 | 南京大学盐城环保技术与工程研究院 | A kind of storage tank tidal air collection and purification system and method |
| CN106693436A (en) * | 2015-11-13 | 2017-05-24 | 中国石化工程建设有限公司 | Tail gas treatment system for storage tank type material storage facilities |
| CN105869707B (en) * | 2016-05-20 | 2017-11-14 | 浙江光隆能源科技股份有限公司 | Aluminium paste for water boiling resistance solar cell and preparation method thereof |
| CN105810289B (en) * | 2016-05-20 | 2017-10-24 | 浙江光隆能源科技股份有限公司 | Aluminium paste that back of the body polishing polycrystalline solar cell is used and preparation method thereof |
| CN107731345B (en) * | 2016-07-05 | 2019-02-15 | 浙江光隆能源科技股份有限公司 | The preparation method of the back of solar cell silver paste of the anti-crack of the high-tensile strength of improvement |
| CN108114573B (en) * | 2016-11-29 | 2021-03-05 | 中国石油化工股份有限公司 | System and method for collecting, purifying and recycling tank top gas in storage tank area |
| CN107008133B (en) * | 2017-04-11 | 2020-02-07 | 湖北绿色家园材料技术股份有限公司 | Comprehensive treatment device for waste gas and waste water in benzyl alcohol production |
| CN106990799A (en) * | 2017-04-14 | 2017-07-28 | 中国石油化工股份有限公司 | The acid water storage tank of combined type prevention dodges quick-fried method of controlling security |
| CN112090104A (en) * | 2020-09-12 | 2020-12-18 | 浙江航威专用设备有限公司 | Organic solvent liquefaction collection system and collection method thereof |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1070129A (en) * | 1992-07-15 | 1993-03-24 | 江西省纺织工业科研设计院 | Exhaust gas treatment method and device during viscose rayon is produced |
| CN101298015A (en) * | 2008-01-21 | 2008-11-05 | 许小林 | Processing equipment for saving energy and reducing emissions of exhaust air |
-
2008
- 2008-10-28 CN CN2008102283476A patent/CN101721832B/en active Active
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1070129A (en) * | 1992-07-15 | 1993-03-24 | 江西省纺织工业科研设计院 | Exhaust gas treatment method and device during viscose rayon is produced |
| CN101298015A (en) * | 2008-01-21 | 2008-11-05 | 许小林 | Processing equipment for saving energy and reducing emissions of exhaust air |
Also Published As
| Publication number | Publication date |
|---|---|
| CN101721832A (en) | 2010-06-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN101721832B (en) | Method for treating discharged waste gas of acid water tank area | |
| CN101637663B (en) | Method for treating release gas in storage tank area | |
| CN202336287U (en) | Integrated treatment system of organic waste gases of refining company | |
| Singhal et al. | Upgrading techniques for transformation of biogas to bio‐CNG: a review | |
| CN101347708B (en) | Method for processing sulphur-containing exhaust air with fetor escaped from storage tank | |
| CN101898071B (en) | Method for treating sulfur- and hydrocarbon-containing foul waste gas | |
| Noyola et al. | Treatment of biogas produced in anaerobic reactors for domestic wastewater: odor control and energy/resource recovery | |
| Allegue et al. | Biogas and bio-syngas upgrading | |
| CN100496678C (en) | Combined purification method for effluvial exhaust air | |
| US8110028B2 (en) | Regenerable purification system for removal of siloxanes and volatile organic carbons | |
| CN106362547B (en) | A kind of processing method and processing device of sulfur-containing organic waste gas | |
| CN102309913A (en) | Treatment method for stinky waste gas containing sulfides and hydrocarbons | |
| CN108114573B (en) | System and method for collecting, purifying and recycling tank top gas in storage tank area | |
| CN106765210B (en) | A kind of incineration treatment method and device of refinery's organic exhaust gas | |
| CN101239272B (en) | Processing method of sewage storage tank discharging gas | |
| CN106362552B (en) | A kind of processing method and processing device of high-concentration organic waste gas | |
| CN203549850U (en) | Organic waste gas comprehensive disposal system | |
| CN101417729B (en) | Method for protecting storage tank by using flue gas | |
| CN207822795U (en) | Composite type ship harbour oil gas minimum discharge retracting device | |
| CN101347684B (en) | Method for treating tail gas during production processes of polyalcohol | |
| CN104548879B (en) | A kind of oil plant sour water tank method for treating release gas and device | |
| CN216143752U (en) | Butadiene tail gas treatment process device of nitrile rubber synthesizer | |
| CN102908849B (en) | The processing method of discharged exhaust gas in sewage disposal field | |
| CN101670926B (en) | Emission-reduction processing method and device for storage-tank waste gas | |
| CN102908799B (en) | Treatment method for emissions of aromatic hydrocarbon storage tank |
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 |