CN202516336U - Storage tank area effluent gas treatment system - Google Patents
Storage tank area effluent gas treatment system Download PDFInfo
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- CN202516336U CN202516336U CN2012201740777U CN201220174077U CN202516336U CN 202516336 U CN202516336 U CN 202516336U CN 2012201740777 U CN2012201740777 U CN 2012201740777U CN 201220174077 U CN201220174077 U CN 201220174077U CN 202516336 U CN202516336 U CN 202516336U
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Abstract
The utility model relates to a storage tank area effluent gas treatment system which comprises a condensing device or an absorption device which is connected in series by a gas transmission line through a compressor, a vacuum pump, and a membrane separator, an adsorber and a nitrogen pipeline that are sequentially connected in series by the gas transmission line. The storage tank area effluent gas treatment system organically integrates a condensation method, an absorption method, a membrane separation method and an adsorption method according to the different boiling points of the liquid in a storage tank; and the system utilizes the technical advantages of the four methods, thus effectively recovering hydrocarbons in the effluent gas of a tank area, leading nitrogen to be completely utilized and causing no secondary pollution; and the system has the characteristic of being high in operation safety.
Description
Technical field
The utility model relates to the treating apparatus of release gas in storage tank area, is specifically related to a kind of treatment system at discharging gas such as oil product, aromatic hydrocarbons and chemicals Tank Farm.
Background technology
The discharging gas of the size of Tank Farm breathing has at present promptly caused the economic loss of raw material, also has the potential safety hazard of accidents such as breaking out of fire, blast.At present a lot of storage tanks have made internal floating roof tank into, eliminate a jar interior gas-phase space, have significantly reduced the loss that big or small breathing causes.But because the potted component between floating top and the tank skin still exist some to reveal, or the fluid discharge of some volatilization is along with storage tank discharging gas has lost.In order further to improve the safety of tank field; And the quality of assurance fluid product; Many Tank Farm designs have adopted internal floating roof tank or fixed tank to add the method for nitrogen envelope; Can prevent that like this storage tank (especially flammable liquid storage tank) top fire compartment from being that the zero inflammable and explosive steam of distinguishing in position reaches explosion limit, meets static discharge or other incendiary sources and blast.Also prevent to be prone to oxidized material oxidation simultaneously.When inner floating roof with nitrogen envelope or the feeding of fixed roof tank liquid; The pressure of storage tank can descend gradually, and this pressure drops to nitrogen when the setting value of the control valve of force regulating valve, and control valve is opened; Nitrogen can be injected in the storage tank; The pressure of storage tank slowly raises then, and when pressure during greater than the setting value of control valve, control valve cuts out.Linking to each other with the nitrogen pipe network of nitrogen envelope from force regulating valve.Adopt hydro carbons and the nitrogen of component that mainly contains in the storage tank discharging gas of nitrogen envelope for volatilizing.Because the existence that size is breathed, the nitrogen amount that consume every day is very high, and according to SH/T3007-2007 Oil Storage and Transport System of Petrochemistry tank field design specification, exhalation amount and soakage are following:
The gas soakage that maximum liquid outlet quantity caused when a) liquid goes out jar should be considered by the maximum liquid outlet quantity of liquid; The pot liquid steam exhalation amount that maximum feed liquor amount when liquid advances jar is caused, when liquid flash-point (remaining silent) is higher than 45 ℃, should be by 1.07 times of considerations of maximum feed liquor amount, when liquid flash-point (remaining silent) is lower than 45 ℃, should be by 2.14 times of considerations of maximum feed liquor amount,
B) little breathing is with 10000m
3Be example, it is 1210m that the maximum temperature drop of atmosphere causes jar interior contraction of gas to cause the amount of storage tank suction gas
3/ h because of the atmosphere maximum temperature rise causes jar gas that interior gas expands and breathes out, for when liquid flash-point (remaining silent) is higher than 45 ℃, is 807m
3/ h when liquid flash-point (remaining silent) is lower than 45 ℃, is 1210m
3/ h.
Release gas in storage tank area recovery way commonly used at present mainly contains condensation method, absorption process, film separation and absorption method.Condensation method is applicable to the recovery of hydro carbons in the discharging of higher boiling and high concentration, and the content of hydro carbons promptly can not recycle still than higher in the condensed nitrogen, can not qualified discharge.Absorption process often adopts the absorbent that boiling point is higher, vapour pressure is lower according to the similar principle that mixes of organic matter, makes the organic gas component transfer to liquid phase from gas phase.But the purity of nitrogen can not satisfy the standard of recycle in the discharging gas after absorption process is handled.It is according to the difference of hydro carbons and nitrogen infiltration rate in film that film separates, and realizes both separation, and the motive force of transmittance process is the partial pressure difference of gas component in the film both sides, and film separates the recovery that often need combine to realize organic component with other technology.Absorption method is applicable to handles the low concentration hydrocarbon gas, when the hydro carbons concentration ratio of handling is low, can realize the nitrogen gas purity requirement.Because tank field discharging gas generally is that fluctuation of concentration intermittently, gas component is bigger, above-mentioned single recovery technology often can not guarantee to realize the processing of tank field discharging gas.
Summary of the invention
In view of existing in prior technology the problems referred to above, the utility model is intended to disclose a kind of release gas in storage tank area treatment system, has hydro carbons rate of recovery height, nitrogen circulation utilization, does not produce characteristics such as secondary pollution, processing safety height.
The technical solution of the utility model is achieved in that
A kind of release gas in storage tank area treatment system is characterized in that:
It comprises by condensing unit or the absorption plant of gas transmission line through compressor serial connection, the membrane separator, absorber and the nitrogen pipeline that also comprise vavuum pump, be connected in series successively by gas transmission line;
Said condensing unit comprises condenser, gas-liquid separator and filter; Gas-liquid separator is connected with said coalescing filter in its napex on-condensible gas outlet, and is connected with liquid line at the liquid outlet of its bottom;
Said absorption plant is the absorption tower; The absorption liquid inlet on absorption tower is connected with the lean solution pipeline through lean pump; The bottom on absorption tower is connected with the rich solution pipeline through the rich solution pump;
The gas outlet at gas outlet, coalescing filter top and top, absorption tower is connected with membrane separator through gas transmission line respectively;
Absorber comprises that at least one adsorbent bed that is in adsorbed state and at least one are in the adsorbent bed of parse state;
Membrane separator is held back side at its film and is connected with the absorption side of said absorber;
The film per-meate side of membrane separator and the parsing side of absorber are connected with the arrival end of vavuum pump respectively through pipeline, and the port of export of vavuum pump then returns the entrance side that is connected to compressor through gas transmission line;
Nitrogen after absorber absorption is connected to nitrogen pipeline through pressure-control valve.
Different according to boiling point of liquid in the storage tank, to high boiling wet tank, hydrocarbon component is easy to condensation in the discharging gas, like the aromatic hydrocarbons storage tank, adopts condensation method, membrane separation process and the integrated integrated conduct method of absorption method; To the storage tank that contains low-boiling point liquid, hydrocarbon component has the component that is difficult for condensation in the discharging gas, like oil product storage tank, then adopts the integrated conduct method of absorption process, membrane separation process and absorption method organic integration; Utilize the advantage of technology separately, can effectively reclaim the hydro carbons in the tank field discharging gas, realize the recycle of nitrogen 100% simultaneously, do not produce secondary pollution, and processing safety is high.
Description of drawings
Fig. 1 is the system diagram of treating apparatus of the release gas in storage tank area of embodiment 1;
Fig. 2 is the system diagram of treating apparatus of the release gas in storage tank area of embodiment 2.
Among the figure, 1. compressor; 21. condenser; 22. gas-liquid separator; 23. filter; 3. membrane separator; 4. absorber; 5. control valve; 6. vavuum pump; 7. absorption tower; 8. lean pump; 9. rich solution pump; 100. admission line; 200. nitrogen pipeline; 300. liquid line; 400. lean solution pipeline; 500. rich solution pipeline.
The specific embodiment
Embodiment 1
To high boiling wet tank, like the aromatic hydrocarbons storage tank, adopt the treatment system of release gas in storage tank area as shown in Figure 1, specify as follows:
For the next discharging gas of nitrogen envelope Tank Farm; Enter into compressor 1 through air inlet pipeline 100; Boost to certain pressure then; And be sent to through air delivering pipeline and carry out condensation in the condenser 21, the gas-liquid mixture that obtains is sent to gas-liquid separator 22 to be separated, the hydrocarbon liquids that obtains after the separation from gas-liquid separator 22 outlet at bottoms through liquid line 300 carrying devices; On-condensible gas from gas-liquid separator 22 top exits come out enters into coalescing filter 23, removes particle and the drop carried secretly in the air-flow, protection subsequent membrane separation device 3.In membrane separator 3, when gas process membrane module, hydrocarbon component penetrated preferably film is in the per-meate side enrichment of film; In the stream of nitrogen gas that side is enrichment of holding back of film, through removing remaining hydro carbons in the air-flow in the pipeline entering absorber 4, absorber 4 has at least two adsorbent beds to form; One is in adsorbed state; Another is in parse state, and the nitrogen gas purity after the absorption reaches more than 99.5% (the mol percentage), through pressure-control valve 5 suitable nitrogen pipeline 200 carrying devices; Get into original nitrogen pipe network, recycling.In order to improve the parsing effect of membrane separation efficiency and absorber 4; Be provided with vavuum pump 6; The inlet of said vavuum pump 6 is connected with the per-meate side of membrane separator 3 and the parsing side of absorber 4 respectively through air delivering pipeline; The outlet of vavuum pump 6 is returned the inlet of receiving compressor 1 through air delivering pipeline, reclaims hydrocarbon component through further compression condensation.
Embodiment 2
To the storage tank that contains low-boiling point liquid, like oil product storage tank, adopt the treatment system of a kind of release gas in storage tank area as shown in Figure 2, specify as follows:
Discharging gas for nitrogen envelope Tank Farm is come through air inlet pipeline 100, enters into compressor 1 through appendix.Gas after compressor 1 compression is delivered to the bottom on absorption tower 7.In absorption tower 7, the gas phase of hydrocarbonaceous from bottom to top with the absorption liquid counter current contacting mass transfer of bringing through lean pump 8 from lean solution pipeline 400, the most of hydro carbons in the gas phase is absorbed, at the bottom of tower through rich solution pump 9 and rich solution pipeline 500 carrying devices; Then 7 the top discharge from the absorption tower of unabsorbed gas containing hydrocarbon gets into membrane separator 3 then.In order to improve the motive force of film separation process; Increase the efficient of film separation process, be provided with a vavuum pump 6, produce negative pressure in the per-meate side of membrane separator 3 through vavuum pump 6 in the film per-meate side of membrane separator 3; Improve the motive force of film separation process, to improve the film separative efficiency; Vavuum pump 6 outlets are rich hydro carbons gas, turn back to compressor 1 inlet through air delivering pipeline, are recycled compression, absorb; And film is held back the nitrogen-rich stream of side for separating through film, gets into through air delivering pipeline and removes hydro carbons remaining in the air-flow in the absorber 4.Absorber 4 has at least two adsorbent beds to form, and one is in adsorbed state, and another is in reproduced state.Adopt the way of vacuum desorption to come reproducing adsorbent, regeneration gas is got back to compressor 1 inlet by air delivering pipeline through vavuum pump 6, is recycled compression, absorbs.Nitrogen gas purity after the absorption reaches more than 99.5% (the mol percentage), along nitrogen pipeline 200 carrying devices, gets into original nitrogen pipe network through pressure-control valve 5, recycling.
The above; Be merely the preferable specific embodiment of the utility model; But the protection domain of the utility model is not limited thereto; Any technical staff who is familiar with the present technique field is equal to replacement or changes according to the technical scheme of the utility model and inventive concept thereof in the technical scope that the utility model discloses, and all should be encompassed within the protection domain of the utility model.
Claims (1)
1. release gas in storage tank area treatment system is characterized in that:
It comprises by condensing unit or the absorption plant of gas transmission line through compressor serial connection, the membrane separator, absorber and the nitrogen pipeline that also comprise vavuum pump, be connected in series successively by gas transmission line;
Said condensing unit comprises condenser, gas-liquid separator and filter; Gas-liquid separator is connected with said coalescing filter in its napex on-condensible gas outlet, and is connected with liquid line at the liquid outlet of its bottom;
Said absorption plant is the absorption tower; The absorption liquid inlet on absorption tower is connected with the lean solution pipeline through lean pump; The bottom on absorption tower is connected with the rich solution pipeline through the rich solution pump;
The gas outlet at gas outlet, coalescing filter top and top, absorption tower is connected with membrane separator through gas transmission line respectively;
Absorber comprises that at least one adsorbent bed that is in adsorbed state and at least one are in the adsorbent bed of parse state;
Membrane separator is held back side at its film and is connected with the absorption side of said absorber;
The film per-meate side of membrane separator and the parsing side of absorber are connected with the arrival end of vavuum pump respectively through pipeline, and the port of export of vavuum pump then returns the entrance side that is connected to compressor through gas transmission line;
Nitrogen after absorber absorption is connected to nitrogen pipeline through pressure-control valve.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012201740777U CN202516336U (en) | 2012-04-23 | 2012-04-23 | Storage tank area effluent gas treatment system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2012201740777U CN202516336U (en) | 2012-04-23 | 2012-04-23 | Storage tank area effluent gas treatment system |
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| CN202516336U true CN202516336U (en) | 2012-11-07 |
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| CN2012201740777U Expired - Fee Related CN202516336U (en) | 2012-04-23 | 2012-04-23 | Storage tank area effluent gas treatment system |
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Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106310697A (en) * | 2015-07-03 | 2017-01-11 | 江苏金门能源装备有限公司 | Novel integrated oil and gas deep recovery and emission control device |
| 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 |
| CN106742888A (en) * | 2016-12-15 | 2017-05-31 | 安徽科海压缩机制造有限公司 | The shallow cold recovery device of the supercharging of volatile organic steam in a kind of oil gas |
| CN108114573A (en) * | 2016-11-29 | 2018-06-05 | 中国石油化工股份有限公司 | The collection and purification recovery system and method for a kind of tank area head space gas |
| CN108380001A (en) * | 2018-05-09 | 2018-08-10 | 安徽实华工程技术股份有限公司 | A kind of tank area protection nitrogen recycling processing cycle utilizes system and method |
| CN110926107A (en) * | 2019-10-18 | 2020-03-27 | 中石化上海工程有限公司 | Nitrogen closed recovery system and method in bulk drug production |
| CN112007467A (en) * | 2020-08-25 | 2020-12-01 | 中冶焦耐(大连)工程技术有限公司 | Benzene hydrogenation tank zone tail gas purification device and method |
| CN114042367A (en) * | 2021-12-02 | 2022-02-15 | 大连理工大学盘锦产业技术研究院 | Near-zero emission productive recovery method and system for nitrogen-rich organic tail gas cleaned by electrolyte equipment |
-
2012
- 2012-04-23 CN CN2012201740777U patent/CN202516336U/en not_active Expired - Fee Related
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106310697A (en) * | 2015-07-03 | 2017-01-11 | 江苏金门能源装备有限公司 | Novel integrated oil and gas deep recovery and emission control device |
| 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 |
| CN108114573A (en) * | 2016-11-29 | 2018-06-05 | 中国石油化工股份有限公司 | The collection and purification recovery system and method for a kind of tank area head space gas |
| CN106742888A (en) * | 2016-12-15 | 2017-05-31 | 安徽科海压缩机制造有限公司 | The shallow cold recovery device of the supercharging of volatile organic steam in a kind of oil gas |
| CN108380001A (en) * | 2018-05-09 | 2018-08-10 | 安徽实华工程技术股份有限公司 | A kind of tank area protection nitrogen recycling processing cycle utilizes system and method |
| CN108380001B (en) * | 2018-05-09 | 2023-11-21 | 安徽实华工程技术股份有限公司 | Storage tank area protection nitrogen recycling system and method |
| CN110926107A (en) * | 2019-10-18 | 2020-03-27 | 中石化上海工程有限公司 | Nitrogen closed recovery system and method in bulk drug production |
| CN110926107B (en) * | 2019-10-18 | 2021-08-10 | 中石化上海工程有限公司 | Nitrogen closed recovery system and method in bulk drug production |
| CN112007467A (en) * | 2020-08-25 | 2020-12-01 | 中冶焦耐(大连)工程技术有限公司 | Benzene hydrogenation tank zone tail gas purification device and method |
| CN114042367A (en) * | 2021-12-02 | 2022-02-15 | 大连理工大学盘锦产业技术研究院 | Near-zero emission productive recovery method and system for nitrogen-rich organic tail gas cleaned by electrolyte equipment |
| CN114042367B (en) * | 2021-12-02 | 2024-04-05 | 大连理工大学盘锦产业技术研究院 | Nearly zero emission productization recovery method and system for cleaning nitrogen-rich organic tail gas by electrolyte equipment |
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Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20121107 Termination date: 20210423 |
|
| CF01 | Termination of patent right due to non-payment of annual fee |