CN201529414U - Low-temperature condensing-filter catching recycling equipment for volatility organic steam - Google Patents
Low-temperature condensing-filter catching recycling equipment for volatility organic steam Download PDFInfo
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- CN201529414U CN201529414U CN2009202475508U CN200920247550U CN201529414U CN 201529414 U CN201529414 U CN 201529414U CN 2009202475508 U CN2009202475508 U CN 2009202475508U CN 200920247550 U CN200920247550 U CN 200920247550U CN 201529414 U CN201529414 U CN 201529414U
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Abstract
The utility model relates to low-temperature condensing-filter catching recycling equipment for volatility organic steam, which sequentially comprises a heat exchange area, a condensing area and a filter catching area according to a volatility organic steam flowing direction. The condensing area comprises a primary condensing area and a secondary condensing area and is provided with a pipeline for communicating the primary condensing area with the secondary condensing area, fiber layer filter catching media are arranged inside the filter catching area, and an outlet of the filter catching area is communicated with a cold medium area of the heat exchanger area via a pipeline. The low-temperature condensing-filter catching recycling equipment adopts the refrigeration reusing technique and the low-temperature filter catching technique, can greatly reduce energy consumption and manufacturing cost, and further increases recovery rate of the volatility organic steam.
Description
Technical field
The utility model relates to the cryogenic temperature condensation reclaimer of volatile organic steam, relates in particular to the cryogenic temperature condensation-trap filter reclaimer of volatile organic steam.
Background technology
The production processes of a lot of industry, the discharging volatile organic steam, especially with the gasoline operation process of product oil accumulating merchandising business for very.Wherein, fixed tank and ground tank oil loading and unloading, tank car and road tanker loading oil process and hauling operation, oil barge and oil tanker loading and unloading oils process and hauling operation, gas station's nozzle are paid oily operation etc., all give off a large amount of volatile organic steams that are called oil gas.GB20950-2007 " storage tank farm atmosphere pollutants emission standards ", GB20952 " gas station's atmosphere pollutants emission standards " regulation, the tail gas of exhaust of oil treating apparatus, NMHC concentration of emission≤25g/m
3
The recovery of volatile organic steam and processing method mainly are divided into absorption method, absorption process, membrane separation process, regenerative oxidation method and cryogenic temperature condensation method etc.Condensation method is the effective ways that reclaim the volatility organic steam, reclaims volatile organic steams such as hydro carbons with the cryogenic temperature condensation method, and the NMHC concentration of emission under the different adiabatic condensation temperatures in the tail gas or the rate of recovery of hydrocarbons are as follows:
-73 ℃ adiabatic condensation temperature can reclaim 90% hydrocarbons in the oil gas;
-80 ℃ adiabatic condensation temperature can reclaim the hydrocarbons more than 90% in the oil gas; Control exhaust emissions concentration≤50g/m
3
-95 ℃ adiabatic condensation temperature can reclaim the hydrocarbons more than 95% in the oil gas, control exhaust emissions concentration≤35g/m
3
-110 ℃ adiabatic condensation temperature can reclaim in the oil gas 98% hydrocarbons, control exhaust emissions concentration≤25g/m
3
-120 ℃ condensation temperature can reclaim the hydrocarbons more than 98% in the oil gas, control exhaust emissions concentration≤13.4g/m
3
CN00135200.8 " the artificial cooling recovery system of storage, fortune, refueling device oil gas " discloses a kind of by oil gas collection, refrigeration and three recovery systems that subsystem is formed of oil gas cooling, and the cooling medium of oil gas cooling system is a cooling water.CN89206893.0 " oil gas condensation retracting device " discloses gasoline vapor carry out indirect heat exchange with-2 ℃ sodium chloride solution after, wherein oil-gas component recoverys that be liquefied coagulated gas and discharged.Because the oil gas condensation temperature is very high, exhaust emissions concentration can not reach≤25g/m
3The requirement of GB limit value.CN200320102333.2 " condensing type oil gas retracting device " discloses a kind of device for recovering oil and gas that is connected and composed by casing, cooling cylinder and refrigeration unit.Because condensation temperature does not reach below-110 ℃, exhaust emissions concentration can not reach≤25g/m
3The requirement of GB limit value.CN01115516.7 " Gu media zones cold-storage/condensation reclaims method of oil gas and solvent naphtha " discloses: in 〉=-70 ℃ general cold scope, the method for condensation liquefaction gasoline vapor reaches exhaust quality concentration≤35g/m
3Exhaust emissions concentration can not reach≤25g/m
3The requirement of GB limit value.CN200620078066.3 " condensing type oil gas retracting device " discloses a kind of " rate of recovery 〉=95%, exhaust of oil concentration≤25g/m
3", utilize the complex method of " condensation+active carbon " to reclaim gasoline vapor.
Condensation method reclaims in the volatility organic steam process, organic steam in the gas phase is condensed into liquid phase by cooling and reclaims, in order to obtain certain rate of recovery, condensation temperature and gas residence time are important conditions, condensation temperature is provided by refrigeration unit, the long time of staying need be adopted the Cryo Equipment and the large-area evaporative condenser of large space, and volatile organic matter is liquid phase and further reclaims in the evaporative condenser surface condensation.Therefore, the equipment investment and the operating cost of existing condensation recycling method recovery volatile organic matter are higher.
Summary of the invention
At the deficiencies in the prior art, the utility model provides a kind of cryogenic temperature condensation-trap filter reclaimer of volatile organic steam, and this equipment can reduce equipment scale, reduces operating cost.
The cryogenic temperature condensation of the utility model volatile organic steam-trap filter reclaimer comprises heat transfer zone, condensing zone and trap filter district successively by the volatile organic steam flow direction, condensing zone comprises one-level condensing zone and B-grade condensation district, the pipeline that is communicated with one-level condensing zone and B-grade condensation district is set, fibrage trap filter medium is set in the trap filter district, and the cold dielectric area of outlet of trap filter district and heat transfer zone is with pipeline connection.
In the utility model, oil sump tank is set communicates with heat transfer zone, one-level condensing zone, B-grade condensation district and trap filter district.
In the utility model, heat transfer zone adopts the conventional gas heat exchanger, volatile organic steam is in gas heat exchanger, and the cryogenic gas after handling with trap filter carries out the indirect heat exchange, can reduce to about 0 ℃ through the temperature of heat exchanger volatile organic steam.
In the utility model, one-level condensing zone control gas temperature is reduced to-45 ℃～-50 ℃, and B-grade condensation district control gas temperature is reduced to-95 ℃～-110 ℃.
In the utility model, the trap filter district is provided with separately and is connected with the B-grade condensation district by pipeline, and perhaps the trap filter district is arranged in the B-grade condensation district and the evaporative condenser in B-grade condensation district is set up in parallel.The temperature in trap filter district is-95 ℃～-110 ℃, and the flow velocity of gas during by the trap filter district is less than 0.1m/s.
The utility model adopts the reuse technology of cold, has done without gas and has reduced to 0 ℃ of needed refrigeration compressor unit of left and right sides temperature from environment temperature, can cut down the consumption of energy significantly and cost of manufacture.
The utility model adopts the filter at low temperature trapping technique, can effectively isolate 0.01 micron and above fine vaporific hydro carbons that the condensation of gas process produces, can simplify the structure of evaporative condenser, reduces cost of manufacture, and improves the rate of recovery of volatile organic steam.In the utility model, the evaporative condenser in B-grade condensation district only needs that gas is reduced to required temperature and gets final product, and does not have the requirement of gas residence time, and therefore, equipment can be simplified greatly, and investment and operating cost all can obviously reduce.In common condensation removal process, gas needs enough time of staying, fully collect recovery to guarantee condensed liquid, so equipment scale is bigger.
The utility model device can effectively be removed the hydrocarbons more than 98% in the gasoline oil gas, handles back exhaust emissions concentration and can reach≤25g/m
3The requirement of GB limit value.
Description of drawings
Fig. 1 is the cryogenic temperature condensation-trap filter reclaimer structural relation schematic diagram of the utility model volatile organic steam.
The specific embodiment
The utility model use is as follows: the volatile organic steam from airtight collection conduit at first enters gas heat exchanger, carry out the indirect heat exchange with the cryogenic gas after the trap filter processing, temperature reduces, and isolates condensation water from the bottom of heat exchanger, and condensation water drains into oil sump tank; Noncondensing gas does not enter the one-level evaporative condenser, and gas temperature is reduced to-45 ℃～-50 ℃, and isolates condensation water from the bottom of one-level evaporative condenser, and condensation water drains into oil sump tank; Noncondensing gas does not enter the dual evaporation condenser, and gas temperature is reduced to-95 ℃～-110 ℃, and isolates condensation water from the bottom of dual evaporation condenser, and condensation water drains into oil sump tank; The gas of isolating condensation water enters filter traps, in filter traps, isolates 0.01 micron remaining in the gas of particle diameter and above vaporific hydro carbons.Filter traps captures the vaporific hydro carbons that gets off, and the big back of coalescent change forms liquid, flow to oil sump tank by self gravitation; Gas behind the trap filter with in heat exchanger, carry out the indirect heat exchange from the volatile organic steam of airtight collection conduit, temperature recovery, discharging then.
The fibrage filter traps mainly is the effect that utilizes Brownian movement to the capture of fine vaporific material.For trickle little of several microns particle at zero point zero as particle diameter, usually it is always carrying out irregular Brownian movement with gas molecule collision, Blang spreads that to capture be to utilize the Brownian movement of particle to contact with fiber and be captured in fiber-bed filter, particle is more little, Brownian movement Shaoxing opera is strong, and the probability that is captured is just high more.The spray plasmid footpath scope that contains in the gas is the particle of normal distribution between 0.01～11 micron, with the filter traps that above-mentioned catcher reason is set up, clearance is generally more than 99%.
The utility model is described in further detail to reclaim the gasoline vapor specific embodiment that oil depot gasoline entrucking process produces below.
Referring to Fig. 1, connect the power supply of the low temperature refrigerator group 3 of one-level evaporative condenser 2 earlier, and the power supply of the low temperature refrigerator group 5 of dual evaporation condenser 4, install fixed temperature and carry out condensation operation, to keep one-level evaporative condenser 2 to be in-45 ℃～-50 ℃, be in-95 ℃～-110 ℃ and filter traps 6 with dual evaporation condenser 4 and be in-95 ℃～-110 ℃ low-temperature condition.Evaporative condenser can be selected the equipment of this area routine.
When gasoline entrucking process, the volatile organic steam of generation enters heat exchanger 1 by closed gas pipeline 10, and-95 ℃～-110 ℃ gases with the exit gas connecting pipe of filter traps 6 in heat exchanger 1 carry out indirect heat exchange.-95 ℃～-110 ℃ gases are walked tube side, discharge as purified gas 8 after the heat exchange.Volatile organic steam is walked shell side, and temperature is reduced to a little more than 0 ℃, condensation water from the row of conduits of heat exchanger 1 bottom to oil sump tank 7.
The volatile organic steam that does not condense leaves heat exchanger 1, enters one-level evaporative condenser 2, is cooled to-45 ℃～-50 ℃ in one-level evaporative condenser 2, condensation water from the row of conduits of one-level evaporative condenser 2 bottoms to oil sump tank 7.
The volatile organic steam that one-level evaporative condenser 2 does not condense leaves one-level evaporative condenser 2, enter dual evaporation condenser 4, in dual evaporation condenser 4, be cooled to-95 ℃～-110 ℃, condensation water from the row of conduits of dual evaporation condenser 4 bottoms to oil sump tank 7.
The gas of isolating condensation water leaves dual evaporation condenser 4, enter filter traps 6, under-95 ℃～-110 ℃ temperature, gas is by the microfibre bed of filter traps, remaining particle diameter is captured down greater than 0.01 micron mist of oil, be trapped in the mist of oil on the fiber bed, the big back of coalescent change forms liquid, by the gravity of self, pipeline by filter bottom flow to oil sump tank 7, the gas of handling enters heat exchanger 1 by gas pipeline, walks tube side in heat exchanger 1, and discharges after the volatile organic steam heat exchange of walking shell side.
Claims (7)
1. the cryogenic temperature condensation of a volatile organic steam-trap filter reclaimer, it is characterized in that: comprise heat transfer zone, condensing zone and trap filter district successively by the volatile organic steam flow direction, condensing zone comprises one-level condensing zone and B-grade condensation district, the pipeline that is communicated with one-level condensing zone and B-grade condensation district is set, fibrage trap filter medium is set in the trap filter district, and the cold dielectric area of outlet of trap filter district and heat transfer zone is with pipeline connection.
2. according to the described equipment of claim 1, it is characterized in that: oil sump tank is set communicates with heat transfer zone, one-level condensing zone, B-grade condensation district and trap filter district.
3. according to the described equipment of claim 1, it is characterized in that: heat transfer zone adopts gas heat exchanger, and volatile organic steam is in gas heat exchanger, and the cryogenic gas after handling with trap filter carries out the indirect heat exchange.
4. according to the described equipment of claim 1, it is characterized in that: one-level condensing zone control gas temperature is reduced to-45 ℃～-50 ℃, and B-grade condensation district control gas temperature is reduced to-95 ℃～-110 ℃.
5. according to the described equipment of claim 1, it is characterized in that: the trap filter district is provided with separately and is connected with the B-grade condensation district by pipeline.
6. according to the described equipment of claim 1, it is characterized in that: the trap filter district is arranged in the B-grade condensation district and the evaporative condenser in B-grade condensation district is set up in parallel.
7. according to claim 1,5 or 6 described equipment, it is characterized in that: the temperature in trap filter district is-95 ℃～-110 ℃, and the flow velocity of gas during by the trap filter district is less than 0.1m/s.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202475508U CN201529414U (en) | 2009-10-27 | 2009-10-27 | Low-temperature condensing-filter catching recycling equipment for volatility organic steam |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2009202475508U CN201529414U (en) | 2009-10-27 | 2009-10-27 | Low-temperature condensing-filter catching recycling equipment for volatility organic steam |
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| CN201529414U true CN201529414U (en) | 2010-07-21 |
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| CN2009202475508U Expired - Lifetime CN201529414U (en) | 2009-10-27 | 2009-10-27 | Low-temperature condensing-filter catching recycling equipment for volatility organic steam |
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Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102743892A (en) * | 2012-07-18 | 2012-10-24 | 南京都乐制冷设备有限公司 | Energy-saving anti-freezing oil gas recovery device |
| CN103439153A (en) * | 2013-09-12 | 2013-12-11 | 苏州威阳环保科技有限公司 | Atmosphere volatile organic compound condensation and concentration sampling device and method |
| CN103537113A (en) * | 2013-10-09 | 2014-01-29 | 江苏中远环保科技有限公司 | Double-temperature three-channel oil and gas condenser |
| CN105344227A (en) * | 2015-12-11 | 2016-02-24 | 苟仲武 | Classified recycling method and device of heat pump condensation and liquidation exhaust gas |
| CN105771300A (en) * | 2015-12-01 | 2016-07-20 | 北京明天和创科贸有限公司 | Oil and gas recovery system |
| CN106215450A (en) * | 2016-08-29 | 2016-12-14 | 黎志春 | A kind of fragrance recovery method based on multi-stage condensing device |
| CN106267878A (en) * | 2016-08-29 | 2017-01-04 | 黎志春 | A kind of fragrance recovery method |
| CN106267877A (en) * | 2016-08-29 | 2017-01-04 | 黎志春 | A kind of Maillard reaction fragrance recovery method based on ossein |
| CN106377921A (en) * | 2016-08-29 | 2017-02-08 | 黎志春 | Method for recycling fragrance with multi-stage condenser |
| CN109207262A (en) * | 2018-10-17 | 2019-01-15 | 武汉轻工大学 | The extraction element and extracting method of volatile plant essence oil |
| CN109534275A (en) * | 2018-12-12 | 2019-03-29 | 无锡冠亚恒温制冷技术有限公司 | A kind of gas recovery system for oil |
| CN112957869A (en) * | 2021-03-09 | 2021-06-15 | 北京奇峰蓝达光学科技发展有限公司 | Volatile matter treatment system used in crystal growth process |
-
2009
- 2009-10-27 CN CN2009202475508U patent/CN201529414U/en not_active Expired - Lifetime
Cited By (15)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102743892A (en) * | 2012-07-18 | 2012-10-24 | 南京都乐制冷设备有限公司 | Energy-saving anti-freezing oil gas recovery device |
| CN103439153A (en) * | 2013-09-12 | 2013-12-11 | 苏州威阳环保科技有限公司 | Atmosphere volatile organic compound condensation and concentration sampling device and method |
| CN103439153B (en) * | 2013-09-12 | 2015-04-08 | 苏州聚阳环保科技股份有限公司 | Atmosphere volatile organic compound condensation and concentration sampling device and method |
| CN103537113A (en) * | 2013-10-09 | 2014-01-29 | 江苏中远环保科技有限公司 | Double-temperature three-channel oil and gas condenser |
| CN103537113B (en) * | 2013-10-09 | 2015-07-15 | 江苏中远环保科技有限公司 | Double-temperature three-channel oil and gas condenser |
| CN105771300A (en) * | 2015-12-01 | 2016-07-20 | 北京明天和创科贸有限公司 | Oil and gas recovery system |
| CN105344227A (en) * | 2015-12-11 | 2016-02-24 | 苟仲武 | Classified recycling method and device of heat pump condensation and liquidation exhaust gas |
| CN105344227B (en) * | 2015-12-11 | 2018-06-19 | 苟仲武 | A kind of heat pump condensation liquefaction discharge gas classification retracting device |
| CN106215450A (en) * | 2016-08-29 | 2016-12-14 | 黎志春 | A kind of fragrance recovery method based on multi-stage condensing device |
| CN106267878A (en) * | 2016-08-29 | 2017-01-04 | 黎志春 | A kind of fragrance recovery method |
| CN106267877A (en) * | 2016-08-29 | 2017-01-04 | 黎志春 | A kind of Maillard reaction fragrance recovery method based on ossein |
| CN106377921A (en) * | 2016-08-29 | 2017-02-08 | 黎志春 | Method for recycling fragrance with multi-stage condenser |
| CN109207262A (en) * | 2018-10-17 | 2019-01-15 | 武汉轻工大学 | The extraction element and extracting method of volatile plant essence oil |
| CN109534275A (en) * | 2018-12-12 | 2019-03-29 | 无锡冠亚恒温制冷技术有限公司 | A kind of gas recovery system for oil |
| CN112957869A (en) * | 2021-03-09 | 2021-06-15 | 北京奇峰蓝达光学科技发展有限公司 | Volatile matter treatment system used in crystal growth process |
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Granted publication date: 20100721 |
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