CN115253609A - Method and device for recycling VOCS (volatile organic Compounds) in tank field - Google Patents
Method and device for recycling VOCS (volatile organic Compounds) in tank field Download PDFInfo
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- CN115253609A CN115253609A CN202210833968.7A CN202210833968A CN115253609A CN 115253609 A CN115253609 A CN 115253609A CN 202210833968 A CN202210833968 A CN 202210833968A CN 115253609 A CN115253609 A CN 115253609A
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- 238000000034 method Methods 0.000 title claims abstract description 47
- 239000012855 volatile organic compound Substances 0.000 title abstract description 35
- 238000004064 recycling Methods 0.000 title description 4
- 239000007789 gas Substances 0.000 claims abstract description 116
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 84
- 238000003860 storage Methods 0.000 claims abstract description 36
- 239000007788 liquid Substances 0.000 claims abstract description 32
- 238000009833 condensation Methods 0.000 claims abstract description 25
- 230000005494 condensation Effects 0.000 claims abstract description 25
- 238000011068 loading method Methods 0.000 claims abstract description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 18
- 239000002131 composite material Substances 0.000 claims abstract description 18
- 239000012528 membrane Substances 0.000 claims abstract description 18
- 239000001301 oxygen Substances 0.000 claims abstract description 18
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 18
- 239000011261 inert gas Substances 0.000 claims abstract description 11
- 238000011084 recovery Methods 0.000 claims abstract description 8
- 238000002156 mixing Methods 0.000 claims abstract description 5
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 18
- 239000003063 flame retardant Substances 0.000 claims description 9
- 229910052757 nitrogen Inorganic materials 0.000 claims description 9
- 238000000926 separation method Methods 0.000 claims description 6
- RNFJDJUURJAICM-UHFFFAOYSA-N 2,2,4,4,6,6-hexaphenoxy-1,3,5-triaza-2$l^{5},4$l^{5},6$l^{5}-triphosphacyclohexa-1,3,5-triene Chemical compound N=1P(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP(OC=2C=CC=CC=2)(OC=2C=CC=CC=2)=NP=1(OC=1C=CC=CC=1)OC1=CC=CC=C1 RNFJDJUURJAICM-UHFFFAOYSA-N 0.000 claims description 3
- 230000006837 decompression Effects 0.000 claims description 3
- 230000001105 regulatory effect Effects 0.000 claims description 3
- 230000001502 supplementing effect Effects 0.000 claims description 3
- 238000010926 purge Methods 0.000 claims description 2
- 239000002912 waste gas Substances 0.000 abstract description 16
- 230000033228 biological regulation Effects 0.000 abstract description 3
- 238000001179 sorption measurement Methods 0.000 description 7
- 230000003647 oxidation Effects 0.000 description 6
- 238000007254 oxidation reaction Methods 0.000 description 6
- 230000003197 catalytic effect Effects 0.000 description 5
- 238000000746 purification Methods 0.000 description 5
- 238000010521 absorption reaction Methods 0.000 description 4
- 239000000126 substance Substances 0.000 description 4
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 3
- 239000003054 catalyst Substances 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 3
- 239000000446 fuel Substances 0.000 description 3
- 230000001172 regenerating effect Effects 0.000 description 3
- 238000009841 combustion method Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000004880 explosion Methods 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000002918 waste heat Substances 0.000 description 2
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000010170 biological method Methods 0.000 description 1
- 238000007084 catalytic combustion reaction Methods 0.000 description 1
- 238000012824 chemical production Methods 0.000 description 1
- 238000004140 cleaning Methods 0.000 description 1
- 239000010849 combustible waste Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- IEJIGPNLZYLLBP-UHFFFAOYSA-N dimethyl carbonate Chemical compound COC(=O)OC IEJIGPNLZYLLBP-UHFFFAOYSA-N 0.000 description 1
- 238000004090 dissolution Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000012847 fine chemical Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 201000009240 nasopharyngitis Diseases 0.000 description 1
- 239000003345 natural gas Substances 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 238000005201 scrubbing Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
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Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D5/00—Condensation of vapours; Recovering volatile solvents by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/002—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by condensation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/708—Volatile organic compounds V.O.C.'s
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
- Y02A50/00—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE in human health protection, e.g. against extreme weather
- Y02A50/20—Air quality improvement or preservation, e.g. vehicle emission control or emission reduction by using catalytic converters
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
The invention discloses a method and a device for recovering VOCS (volatile organic Compounds) in a tank field, belonging to the technical field of VOC (volatile organic compounds) recovery, and comprising the following steps of: (1) Separating oxygen from the processing gas from the loading and unloading station area through an organic composite membrane, and mixing the processing gas with the methanol tank gas purged by using inert gas; (2) Feeding the mixed gas into a heat exchanger for condensation, wherein the uncondensed gas is fed into a separator at the inlet of a compressor, and the liquid obtained by condensation is fed into the separator; (3) Collecting the liquid separated in the separator, sending the separated gas into the compressor inlet separator, and sending the liquid in the compressor inlet separator into the separator; (4) The gas entering the compressor inlet separator is compressed by the compressor and enters a storage tank for standby. The circulating inert seal non-discharge process provided by the invention has the advantages that the waste gas discharged by the breather valve is closely collected after the inert seal is additionally arranged on the storage tank, and the waste gas is purified, compressed, stored, subjected to peak regulation and then used as the inert seal, so that the whole process is in closed circulation, and the problem of discharge pollution of the storage tank is solved.
Description
Technical Field
The invention belongs to the technical field of VOC (volatile organic compounds) recovery, and particularly relates to a method and a device for recovering VOCS (volatile organic compounds) in a tank field.
Background
VOC is an english abbreviation of volatile organic compounds (volatile organic compounds), which is widely used in various production in chemical industry, and for conventional VOC pollutants like methanol and ethylene glycol in chemical industry, according to different concentrations and emission laws, common VOC exhaust gas treatment processes mainly include processes of condensation recovery, adsorption, combustion/thermal oxidation, biological purification, and the like, and the following description is respectively given for the treatment ranges of each treatment method:
1. condensation recovery method: the condensation method under the common cold medium is generally mainly suitable for the concentration range of 50-100 gVOC/m3The method can not treat VOC gas with low concentration, and the treated gas can not reach the emission standard.
2. Absorption method (gas scrubbing): the absorption method works through gas-liquid two-phase dissolution balance of organic matters in a proper solvent, is generally suitable for good solubility and has the concentration range of 0.3-5 g/m3At very low concentrations, the absorption efficiency decreases with decreasing gas phase concentration, below 0.3g/m3The gas phase concentration of the catalyst is very low by adopting an absorption method, and cannot directly reach the standard, so that the catalyst is generally used for pretreatment processes of other processes and cannot be deeply treated.
3. An adsorption method: in general, the adsorption method includes regenerative adsorption and non-regenerative adsorption, and the regenerative adsorption is generally applied to 0.01 to 10g/m3The non-regenerable adsorption is suitable for 0.01-1.2 g/m3Concentration range.
4. The combustion method comprises the following steps: the method is divided into direct combustion and high-temperature thermal oxidation (RTO) processes according to the temperature interval of the clean room. The direct combustion method has the treatment temperature as high as 1000-1200 ℃, the heating energy consumption is too high, and the safety risk is high and is not considered. The treatment temperature of the RTO process is in the range of 700-900 ℃, and the applicable VOC concentration range is about 0.2-10 g/m3Most preferably 3 to 5g/m3The organic combustible waste gas with stable concentration range needs to provide fuel heat sources such as natural gas, diesel oil and the like to heat the waste gas and the temperature of a purifying chamber to the waste gas treatment temperature in the range of 700-900 ℃ if the concentration is lower than the range, and needs to arrange a heat energy extraction device in an RTO furnace, such as a combustion chamber, and a steaming chamber is added to increase the temperature of the waste gas and the temperature of the purifying chamber to the waste gas treatment temperature in the range of 700-900 ℃ if the concentration is higher than the optimum concentration rangeSteam-producing heat pipes or waste heat boilers, etc. And if the concentration fluctuation is large, such as the process exhaust of the intermittent production of the fine chemical production device, the intermittent exhaust of a breather valve of a storage tank, the irregular operation exhaust of a loading platform and the like, the RTO is easy to generate the explosion risk working condition that the VOC concentration exceeds 25LEL% of the lower explosion limit besides adding a large amount of fuel to maintain the stable operation of the RTO purification device, the operation cost is high, the safety risk is large, and the process is not recommended.
5. Catalytic oxidation process (terminal area): the loading and unloading station area belongs to a low-temperature catalytic oxidation process at 180-400 ℃, and the VOC with medium and low concentration is oxidized into harmless CO for the oxygen in the waste gas under the catalytic action of the VOC catalytic combustion catalyst2And H2O, the terminal area is generally adapted to 0.05 to 3gVOC/m3The concentration range is 1.5-3.0 g VOC/m3When the concentration is lower than the range, a large amount of fuel needs to be added to maintain the purification temperature of the waste gas and a purification system, and if the concentration is higher than 3.0g VOC/m3And a complex CO waste heat extraction system needs to be arranged, otherwise, the catalytic oxidation of the CO device is seriously influenced.
6. A biological purification method: most of substances in the project, such as methanol, dimethyl carbonate and the like, belong to VOC substances with better biochemical property, but the decomposition speed is slow by a common biological method, the treatment load of a biological filter cannot be very high, and the concentration is not higher than 0.5g/m generally3And the inlet concentration fluctuation cannot be too large.
The total discharge of three exhaust gases generated by our company can reach 169 tons/year at most, wherein the average concentration of the trapped exhaust gas of the loading platform can reach 13g/m3Average concentration of the intermediate tank area is 4.0g/m3And product tank area 0.5g/m3The total concentration of the three waste gases is about 2.5g/m after being converged3In the case of the treatment range of the above methods, the catalytic oxidation method (terminal area) is finally applied, however, the gas treated by the method still contains partial VOC residues and also contains a large amount of nitrogen and oxygen, and for the gas, the prior art is usually directly evacuated, so that the effective components in the gas are difficult to be fully utilized, and the exhaust emission of a plant area is increased; in addition, some nailsThe alcohol tank can also generate a large amount of VOC tail gas after being used, and if the tail gas is not treated, the environment can be seriously influenced.
Disclosure of Invention
The invention aims to provide a method and a device for recovering a tank field VOCS (volatile organic Compounds) to solve the technical problems of high waste gas emission and difficulty in fully recycling effective components in the prior art by constructing a closed circulation treatment mode.
In order to realize the purpose, the technical scheme adopted by the invention is as follows:
a method for recovering VOCS in a tank field comprises the following steps:
(1) Separating oxygen from the processing gas from the loading and unloading station area through an organic composite membrane, and mixing the processing gas with the methanol tank gas purged by using inert gas;
(2) Feeding the mixed gas into a heat exchanger for condensation, wherein the uncondensed gas is fed into a separator at the inlet of a compressor, and the liquid obtained by condensation is fed into the separator;
(3) Collecting the liquid separated in the separator, and sending the separated gas into the inlet separator of the compressor;
(4) The gas entering the compressor inlet separator is compressed by the compressor and enters the storage tank for later use.
Preferably, the oxygen-enriched gas obtained by separating the treatment gas from the loading and unloading station area by the organic composite membrane is directly discharged.
Preferably, the inert gas in the step (1) is nitrogen.
Preferably, in the step (3), the liquid separated in the separator is conveyed to a rectification system through a pump to rectify and distill each component.
Preferably, in the step (4), qualified gas in the storage tank is used for purging the methanol tank in the step (1), and unqualified gas or gas with excessive oxygen content is emptied.
A recovery device for a tank field VOCS comprises a gas storage tank, an organic composite membrane separator, a methanol tank, a buffer tank, a heat exchanger, a separator, a compressor inlet separator, a compressor, a storage tank, a pipeline for connecting all devices and a valve in a loading and unloading station area;
wherein,
the gas storage tank in the loading and unloading station area conveys gas to the organic composite membrane separator through a pipeline, and a flame-retardant valve is arranged on the pipeline;
an emptying valve is arranged at the oxygen-enriched gas end of the organic composite membrane separator, the VOC gas end transmits gas to the buffer tank through a pipeline, and an oxygen analyzer, a stop valve, a check valve and a fire retardant valve are respectively arranged on the pipeline;
an outlet of the methanol tank conveys the gas to be treated, which is blown out by using inert gas, to a buffer tank through a pipeline, and fire retardant valves are respectively arranged on the pipelines;
the buffer tank conveys the mixed gas to be treated to a heat exchanger through a pipeline for heat exchange and condensation;
the heat exchanger conveys heat exchange condensed gas to a compressor inlet separator through a pipeline, and conveys liquid obtained by condensation to the separator through the pipeline;
the gas outlet of the separator transmits gas to the compressor inlet separator through a pipeline, and liquid in the compressor inlet separator is transmitted into the separator through the pipeline;
the compressor inlet separator delivers gas to the compressor through a conduit;
the compressor conveys gas to a storage tank through a pipeline;
the device is characterized in that the storage tank is provided with an emptying valve, a nitrogen supplementing valve and pipelines respectively connected with the methanol tank and the buffer tank, the pipeline connected with the methanol tank is provided with a pressure regulating valve, and the pipeline connected with the buffer tank is provided with a throttling decompression expansion device.
Compared with the prior art, the invention has the following beneficial effects:
1. the method utilizes the deaerated gas of the waste gas in the loading and unloading station area to clean the used methanol tank, combines and cleans the tail gas of the methanol tank for further treatment and then recycles the tail gas, the recycling is inert and has no discharge process, the whole process is closed and recycled, and the problem of the discharge pollution of the storage tank is solved; the process only needs to add an inert seal on the storage tank, then the waste gas discharged by the breather valve is hermetically collected, and the waste gas is purified, compressed, stored and subjected to peak regulation to be used as the inert seal, so that the tail gas emission is greatly reduced, and the utilization rate of the inert gas is improved;
2. the invention is flexible to use, can combine and treat the waste gas and the methanol tank tail gas in the loading and unloading station area, and can also treat two sections of gas conditions respectively;
3. the process has the advantages of low technical investment, simple flow, low energy consumption, labor saving, easy start-up, stable and simple operation and the like.
Drawings
Fig. 1 is a schematic diagram of a device for recovering the VOCS in the tank farm according to the present invention.
Detailed Description
The present invention will be further described with reference to the following drawings and examples, which are included by way of illustration and not by way of limitation.
Example 1
As shown in fig. 1, which is a schematic diagram of a device of a VOCS recovery process in a tank farm provided by this embodiment, the device includes an air storage tank in a loading and unloading station area, an organic composite membrane separator, a methanol tank, a buffer tank, a heat exchanger, a separator, a compressor inlet separator, a compressor, a storage tank, a pipeline connecting each device, and a valve;
wherein,
the gas storage tank in the loading and unloading station area conveys gas to the organic composite membrane separator through a pipeline, and a flame-retardant valve is arranged on the pipeline;
an emptying valve is arranged at the oxygen-enriched gas end of the organic composite membrane separator, the VOC gas end transmits gas to the buffer tank through a pipeline, and an oxygen analyzer, a stop valve, a check valve and a fire retardant valve are respectively arranged on the pipeline;
an outlet of the methanol tank conveys the gas to be treated, which is blown out by using inert gas, to a buffer tank through a pipeline, and fire retardant valves are respectively arranged on the pipelines;
the buffer tank conveys the mixed gas to be treated to a heat exchanger through a pipeline for heat exchange and condensation;
the heat exchanger conveys heat exchange condensed gas to a compressor inlet separator through a pipeline, and conveys liquid obtained by condensation to the separator through the pipeline;
the gas outlet of the separator transmits gas to the compressor inlet separator through a pipeline, and liquid in the compressor inlet separator is transmitted into the separator through the pipeline;
the compressor inlet separator delivers gas to the compressor through a conduit;
the compressor conveys gas to a storage tank through a pipeline;
the storage tank is provided with an emptying valve, a nitrogen supplementing valve and pipelines respectively connected with the methanol tank and the buffer tank, the pipeline connected with the methanol tank is provided with a pressure regulating valve, and the pipeline connected with the buffer tank is provided with a throttling decompression expansion device.
One implementation of the device of the embodiment is as follows:
when using the device for the first time, close all valves of connecting the methanol tank, its flow is:
(1) Separating oxygen from the treated gas from the loading and unloading station area by an organic composite membrane, feeding the treated gas into a heat exchanger for condensation, feeding the uncondensed gas into a compressor inlet separator, and feeding the liquid obtained by condensation into a separator;
(2) Collecting the liquid separated in the separator, sending the separated gas into the compressor inlet separator, and sending the liquid in the compressor inlet separator into the separator through a pipeline for further separation;
(3) The gas entering the compressor inlet separator is compressed by the compressor and enters a storage tank for standby.
After the storage tank obtains a certain storage amount of inert gas (nitrogen), a valve connected with the methanol tank can be opened for cleaning the used methanol tank, and then the treatment process of the whole device is as follows:
(1) Separating oxygen from the processing gas from the loading and unloading station area through an organic composite membrane, and mixing the processing gas with the methanol tank gas blown by inert gas;
(2) Feeding the mixed gas into a heat exchanger for condensation, wherein the uncondensed gas is fed into a separator at the inlet of a compressor, and the liquid obtained by condensation is fed into the separator;
(3) Collecting the liquid separated in the separator, sending the separated gas into the compressor inlet separator, and sending the liquid in the compressor inlet separator into the separator through a pipeline for further separation;
(4) The gas entering the compressor inlet separator is compressed by the compressor and enters the storage tank for circulation and standby.
The circulating inert sealing non-discharge process is formed, the whole process is in closed circulation, and the problem of storage tank discharge pollution is solved; the process only needs to add an inert seal on the storage tank, then the waste gas discharged by the breather valve is collected in a closed manner, and the waste gas is purified, compressed, stored and subjected to peak regulation and then used as the inert seal, so that the tail gas emission is greatly reduced.
The second implementation of the device of this embodiment is:
(1) Separating oxygen from the processing gas from the loading and unloading station area through an organic composite membrane, and mixing the processing gas with the methanol tank gas blown out by the nitrogen supplemented in the storage tank;
(2) Feeding the mixed gas into a heat exchanger for condensation, wherein the uncondensed gas is fed into a separator at the inlet of a compressor, and the liquid obtained by condensation is fed into the separator;
(3) Collecting the liquid separated in the separator, sending the separated gas into the compressor inlet separator, and sending the liquid in the compressor inlet separator into the separator through a pipeline for further separation;
(4) The gas entering the compressor inlet separator is compressed by the compressor and enters a storage tank for standby.
The third implementation mode of the device in the embodiment is as follows:
(1) Feeding the gas swept out into a heat exchanger for condensation by utilizing a methanol tank swept out by nitrogen supplemented in a storage tank, wherein the uncondensed gas is fed into a compressor inlet separator, and feeding the liquid obtained by condensation into the separator;
(2) Collecting the liquid separated in the separator, sending the separated gas into the compressor inlet separator, and sending the liquid in the compressor inlet separator into the separator through a pipeline for further separation;
(3) The gas entering the compressor inlet separator is compressed by the compressor and enters the storage tank for later use.
The fourth implementation manner of the device of the embodiment is as follows:
(1) Separating oxygen from the treated gas from the loading and unloading station area through an organic composite membrane, feeding the treated gas into a heat exchanger for condensation, feeding the uncondensed gas into a compressor inlet separator, and feeding the liquid obtained by condensation into a separator;
(2) Collecting the liquid separated in the separator, sending the separated gas into the compressor inlet separator, and sending the liquid in the compressor inlet separator into the separator through a pipeline for further separation;
(3) The gas entering the compressor inlet separator is compressed by the compressor and enters a storage tank for standby.
The above-mentioned embodiment is only one of the preferred embodiments of the present invention, and should not be used to limit the scope of the present invention, but all the insubstantial modifications or changes made within the spirit and scope of the main design of the present invention, which still solve the technical problems consistent with the present invention, should be included in the scope of the present invention.
Claims (6)
1. A recovery method of a tank farm VOCS is characterized by comprising the following steps:
(1) Separating oxygen from the processing gas from the loading and unloading station area through an organic composite membrane, and mixing the processing gas with the methanol tank gas blown by inert gas;
(2) Feeding the mixed gas into a heat exchanger for condensation, wherein the uncondensed gas is fed into a separator at the inlet of a compressor, and the liquid obtained by condensation is fed into the separator;
(3) Collecting the liquid separated in the separator, sending the separated gas into the compressor inlet separator, and sending the liquid in the compressor inlet separator into the separator;
(4) The gas entering the compressor inlet separator is compressed by the compressor and enters a storage tank for standby.
2. The method of claim 1, wherein oxygen-rich gas from the separation of the process gas from the terminal area by an organic composite membrane is vented directly.
3. The method for recovering VOCS from a tank farm according to claim 1, wherein the inert gas in step (1) is nitrogen.
4. The method for recovering a VOCS in a tank farm of claim 1, wherein in step (3), the liquid separated in the separator is pumped to a rectification system to rectify the components.
5. The method for recovering a VOCS in a tank farm of claim 1, wherein in step (4), the qualified gas in the storage tank is used for purging the methanol tank in step (1), and the unqualified or over-qualified gas is vented.
6. A recovery device for a tank field VOCS is characterized by comprising an air storage tank, an organic composite membrane separator, a methanol tank, a buffer tank, a heat exchanger, a separator, a compressor inlet separator, a compressor, a storage tank, a pipeline for connecting all devices and a valve in a loading and unloading station area;
wherein,
the gas storage tank in the loading and unloading station area conveys gas to the organic composite membrane separator through a pipeline, and a flame-retardant valve is arranged on the pipeline;
an emptying valve is arranged at the oxygen-enriched gas end of the organic composite membrane separator, the gas is conveyed to the buffer tank through a pipeline at the VOC gas end, and an oxygen analyzer, a stop valve, a check valve and a fire retardant valve are respectively arranged on the pipeline;
an outlet of the methanol tank conveys the gas to be treated, which is blown out by using inert gas, to a buffer tank through a pipeline, and fire retardant valves are respectively arranged on the pipelines;
the buffer tank conveys the mixed gas to be treated to a heat exchanger through a pipeline for heat exchange and condensation;
the heat exchanger conveys heat exchange condensed gas to a compressor inlet separator through a pipeline, and conveys liquid obtained by condensation to the separator through the pipeline;
the gas outlet of the separator transmits gas to the compressor inlet separator through a pipeline, and liquid in the compressor inlet separator is transmitted into the separator through the pipeline;
the compressor inlet separator delivers gas to the compressor through a conduit;
the compressor conveys gas to a storage tank through a pipeline;
the storage tank is provided with an emptying valve, a nitrogen supplementing valve and pipelines respectively connected with the methanol tank and the buffer tank, the pipeline connected with the methanol tank is provided with a pressure regulating valve, and the pipeline connected with the buffer tank is provided with a throttling decompression expansion device.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202210833968.7A CN115253609A (en) | 2022-07-14 | 2022-07-14 | Method and device for recycling VOCS (volatile organic Compounds) in tank field |
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| Application Number | Priority Date | Filing Date | Title |
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| CN202210833968.7A CN115253609A (en) | 2022-07-14 | 2022-07-14 | Method and device for recycling VOCS (volatile organic Compounds) in tank field |
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Citations (5)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN104923029A (en) * | 2015-06-01 | 2015-09-23 | 中国寰球工程公司 | Method for recovering exhaust gas according to polyolefin gas phase method |
| CN107789956A (en) * | 2017-11-10 | 2018-03-13 | 南京天膜科技股份有限公司 | It is a kind of to realize internal floating roof tank interbedded gas VOCs zero-emissions, remove oxygen and recycle the device of nitrogen |
| CN111589264A (en) * | 2020-06-30 | 2020-08-28 | 江苏京控装备有限公司 | Organic solvent waste gas compression condensation and membrane filtration recovery device thereof |
| CN212283426U (en) * | 2020-04-21 | 2021-01-05 | 嘉兴市三江浩嘉高分子材料科技有限公司 | Polypropylene steam pot tail gas processing apparatus |
| CN113996616A (en) * | 2021-11-12 | 2022-02-01 | 安庆军峰危险货物运输有限公司 | Hazardous chemical substance-related tank car green cleaning device and method based on VOCs separation and recovery technology |
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2022
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| CN104923029A (en) * | 2015-06-01 | 2015-09-23 | 中国寰球工程公司 | Method for recovering exhaust gas according to polyolefin gas phase method |
| CN107789956A (en) * | 2017-11-10 | 2018-03-13 | 南京天膜科技股份有限公司 | It is a kind of to realize internal floating roof tank interbedded gas VOCs zero-emissions, remove oxygen and recycle the device of nitrogen |
| CN212283426U (en) * | 2020-04-21 | 2021-01-05 | 嘉兴市三江浩嘉高分子材料科技有限公司 | Polypropylene steam pot tail gas processing apparatus |
| CN111589264A (en) * | 2020-06-30 | 2020-08-28 | 江苏京控装备有限公司 | Organic solvent waste gas compression condensation and membrane filtration recovery device thereof |
| CN113996616A (en) * | 2021-11-12 | 2022-02-01 | 安庆军峰危险货物运输有限公司 | Hazardous chemical substance-related tank car green cleaning device and method based on VOCs separation and recovery technology |
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