CN115155237A - Waste gas treatment system for treating waste gas in chemical reservoir area and treatment method thereof - Google Patents
Waste gas treatment system for treating waste gas in chemical reservoir area and treatment method thereof Download PDFInfo
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- CN115155237A CN115155237A CN202210679023.4A CN202210679023A CN115155237A CN 115155237 A CN115155237 A CN 115155237A CN 202210679023 A CN202210679023 A CN 202210679023A CN 115155237 A CN115155237 A CN 115155237A
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- 238000001179 sorption measurement Methods 0.000 claims abstract description 61
- 238000003795 desorption Methods 0.000 claims abstract description 51
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- 230000005494 condensation Effects 0.000 claims abstract description 39
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 29
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- 239000002808 molecular sieve Substances 0.000 claims description 31
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 31
- 229910021536 Zeolite Inorganic materials 0.000 claims description 21
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 claims description 21
- 239000010457 zeolite Substances 0.000 claims description 21
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- 150000002894 organic compounds Chemical class 0.000 claims 1
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- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
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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
- B01D53/002—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
- 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
- B01D53/02—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 adsorption, e.g. preparative gas chromatography
- B01D53/04—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 adsorption, e.g. preparative gas chromatography with stationary adsorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
- B01J20/10—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising silica or silicate
- B01J20/16—Alumino-silicates
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/3408—Regenerating or reactivating of aluminosilicate molecular sieves
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
- B01J20/30—Processes for preparing, regenerating, or reactivating
- B01J20/34—Regenerating or reactivating
- B01J20/345—Regenerating or reactivating using a particular desorbing compound or mixture
- B01J20/3458—Regenerating or reactivating using a particular desorbing compound or mixture in the gas phase
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
- B01D2253/10—Inorganic adsorbents
- B01D2253/106—Silica or silicates
- B01D2253/108—Zeolites
-
- 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
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2258/00—Sources of waste gases
- B01D2258/02—Other waste gases
- B01D2258/0225—Other waste gases from chemical or biological warfare
-
- 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)
- Analytical Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Organic Chemistry (AREA)
- Engineering & Computer Science (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Inorganic Chemistry (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention discloses a waste gas treatment system for treating waste gas in a chemical reservoir area, which comprises a VOCs conveying and condensing device and a VOCs adsorption and desorption device, wherein the VOCs conveying and condensing device is arranged on the VOCs conveying and condensing device; the VOCs conveying and condensing device comprises a first VOCs conveying path and a VOCs condensing path; the VOCs adsorption and desorption device comprises a second VOCs conveying path, an adsorption and desorption path and a hot nitrogen stripping path; a treatment method of the waste gas treatment system for treating the waste gas in the chemical storage area is also disclosed. The VOCs conveying and condensing device reasonably standardizes the processing procedures of conveying, cooling and condensing and three-stage condensing of VOCs, realizes energy conservation and consumption reduction, condenses moisture in waste gas, and ensures that each condensing box keeps good heat exchange efficiency; VOCs adsorbs VOCs waste gas of desorption device reasonable norm condensation and carries and hot nitrogen desorption technology, adopts hot nitrogen desorption mode, can reach desorption behind the saturated condition with the organic matter, strengthens organic waste gas's processing high efficiency.
Description
Technical Field
The invention relates to the technical field of waste gas treatment, in particular to a waste gas treatment system for treating waste gas in a chemical reservoir area and a treatment method thereof.
Background
At present, the discharge gas of the storage tank in the oil tank area is mainly the discharge gas of a breather valve of the storage tank and organic waste gas generated in the loading process. Because the exhaust gas contains organic solvent, the recycling value is high, substances such as naphtha and tar are stored in the storage tank, and the exhausted waste gas is similar to that in the petrochemical industry and is treated by a common combined recycling method. The oil gas recovery technology of the oil depot has relatively mature technology and equipment in China, but for chemical reservoir areas, the types of stored chemical substances are various and are mixed, the storage material types of the tank need to be replaced, the period is uncertain, and the tank is difficult to be specially used, so that higher requirements on tail gas collection and treatment are provided. The most critical step in the VOCs treatment process is refrigeration and condensation, the existing condensing device can only realize primary refrigeration, the condensation temperature range is small, and the condensing device cannot meet the condensation requirement of large-scale VOCs, and the condensing device generally adopts two compressors, if the same temperature requirement is met, the two compressors need to be started simultaneously, the overlapping energy consumption, the failure rate and the device cost are high, and the device is large in integral volume; secondly, in the VOCs waste gas transmission process, due to the fact that the initial temperature of the waste gas is high, a condensate tank is not arranged to cool the waste gas and condense the waste gas, the condensation burden of a condenser is greatly increased, the frosting speed of the surface of a generator is increased, and energy consumption is overhigh; in addition, the conventional organic waste gas adsorption and desorption device is commonly used in a superheated steam desorption process, is suitable for desorbing low molecular hydrocarbon and aromatic organic matters with lower boiling points, but has weaker desorption capability on high boiling point substances and long desorption period, cannot meet the requirements of large-flow organic waste gas such as naphtha or tar with medium and low concentration, has low adsorption and desorption efficiency and poorer production economy.
Disclosure of Invention
In order to overcome the technical problems, the invention discloses a waste gas treatment system for treating waste gas in a chemical reservoir area and a treatment method thereof.
The technical scheme adopted by the invention for realizing the purpose is as follows:
a waste gas treatment system for treating waste gas in a chemical reservoir area comprises a VOCs conveying and condensing device and a VOCs adsorption and desorption device which are sequentially arranged;
the VOCs conveying and condensing device comprises a first VOCs conveying path and a VOCs condensing path which are sequentially arranged;
VOCs adsorbs desorption apparatus including the second VOCs delivery path and the adsorption and desorption route that set gradually, adsorption and desorption route intercommunication is provided with the hot nitrogen and blows off the route, second VOCs delivery path with VOCs condensation route intercommunication.
Foretell a waste gas treatment system for handling chemical industry reservoir area waste gas, wherein first VOCs delivery path is including first pipeline, condensate tank and the second pipeline that communicates the setting in proper order, in draught fan, first valve, gas flowmeter and pressure transmitter have set gradually on the second pipeline.
In the above waste gas treatment system for treating waste gas in a chemical reservoir area, the condensation path of the VOCs includes a pre-cooling tank, a first-stage shallow cooling tank, a second-stage intermediate cooling tank and a third-stage deep cooling tank which are arranged in a loop, and the pre-cooling tank is communicated with the second conveying pipeline;
VOCs gas sequentially passes through the pre-cooling box, the first-stage shallow cooling box, the second-stage middle cooling box and the third-stage deep cooling box, so that non-condensable gas flows back into the pre-cooling box to form cold internal circulation.
The waste gas treatment system for treating the waste gas in the chemical storage area is characterized in that the condensation temperature range of the pre-cooling box is 5-25 ℃, the condensation temperature range of the first-stage shallow cooling box is 1-10 ℃, the condensation temperature range of the second-stage medium cooling box is-25 to-30 ℃, and the condensation temperature range of the third-stage deep cooling box is-60 to-70 ℃.
Foretell a waste gas treatment system for handling chemical industry reservoir area waste gas, wherein the lime set jar includes first feed inlet, second feed inlet and first discharge gate, first feed inlet with first pipeline intercommunication, first discharge gate with second pipeline intercommunication.
The above waste gas treatment system for treating waste gas in a chemical reservoir area, wherein the second transportation path for the VOCs includes a third transportation pipeline for transporting condensed VOCs and a fourth transportation pipeline for transporting desorbed organic matters, and the third transportation pipeline is communicated with the pre-cooling tank;
the adsorption and desorption path comprises an adsorption tank and an exhaust funnel which are communicated through a fifth conveying pipeline, and the third conveying pipeline and the fourth conveying pipeline are respectively connected with the adsorption tank;
the hot nitrogen blows and takes off route including nitrogen gas storage device and the sixth pipeline that the intercommunication set up, the sixth pipeline with the adsorption tank is connected, in be provided with the heater on the sixth pipeline.
In the above waste gas treatment system for treating waste gas in a chemical reservoir area, the adsorption tank includes a third feed inlet, a fourth feed inlet, a second discharge outlet and a third discharge outlet;
the third feeding port is connected with the third conveying pipeline;
the fourth feed port is connected with the sixth conveying pipeline;
the second discharge hole is connected with the fourth conveying pipeline;
and the third discharge hole is connected with the fifth conveying pipeline.
The above waste gas treatment system for treating waste gas in a chemical reservoir area is characterized in that a plurality of zeolite molecular sieve layers are arranged in parallel in the adsorption tank according to the interval distance.
In the above waste gas treatment system for treating waste gas in a chemical reservoir area, the zeolite molecular sieve layer is a molecular sieve framework formed by three-dimensionally stacking SiO4 and AlO4 tetrahedrons through vertexes.
A treatment method of an exhaust gas treatment system for treating exhaust gas of a chemical reservoir area comprises the following steps:
step 6, after the waste gas is refrigerated to-60 to-70 ℃ through the three-stage deep cooling box, obtaining condensed VOCs liquid and non-condensable gas, wherein the non-condensable gas further flows back into the pre-cooling box to transfer cold energy into the pre-cooling box;
step 7, introducing clean nitrogen into the adsorption tank along a sixth conveying pipeline to purge the zeolite molecular sieve layer so as to remove part of oxygen and water vapor in the gas phase in the adsorption tank;
step 8, introducing the condensed VOCs liquid into the adsorption tank along a third conveying pipeline, adsorbing organic matters in the condensed VOCs liquid by the zeolite molecular sieve layer, closing a third valve to stop introducing the condensed VOCs liquid after the organic matters adsorbed by the zeolite molecular sieve layer reach a saturated state, and discharging desorbed gas by an exhaust funnel;
and 9, heating clean nitrogen by a heater, introducing the heated clean nitrogen into the adsorption tank for stripping, desorbing organic matters from the zeolite molecular sieve layer, and outputting the desorbed organic matters along a fourth conveying pipeline to realize adsorption and desorption of the organic matters in the VOCs.
The invention has the beneficial effects that: according to the VOCs conveying and condensing device, the first VOCs conveying path and the VOCs condensing path are independently divided, the processing procedures of conveying, cooling and condensing of VOCs are reasonably standardized, the VOCs waste gas with corresponding amount can be continuously and stably introduced conveniently, the energy is saved to the maximum extent, the consumption is reduced, meanwhile, the moisture in the waste gas is condensed, the surface frosting speed of an evaporator in each subsequent condensing box is retarded, the good heat exchange efficiency of each condensing box is ensured, and the phenomenon of causing large strain to the subsequent adsorption and desorption procedures is avoided; and VOCs adsorbs desorption device and independently divides second VOCs delivery path, adsorbs desorption route and hot nitrogen blows off the route, and the VOCs waste gas of reasonable standard condensation carries and hot nitrogen desorption technology, adopts hot nitrogen desorption mode, both can reach desorption behind the saturated condition with the organic matter, and very big degree ground strengthens organic waste gas's processing high efficiency, improves the desorption rate, and the emission of reducible organic waste gas reduces the influence to the environment again, improves production economy.
Drawings
The invention is further illustrated with reference to the following figures and examples.
FIG. 1 is a schematic structural view of the present invention;
FIG. 2 is a schematic diagram of the VOCs transport and condensing unit of the present invention;
fig. 3 is a schematic structural diagram of the adsorption and desorption device for VOCs in the present invention.
Detailed Description
The present invention is further illustrated by the following specific examples, which are intended to facilitate the understanding and appreciation of the technical solutions of the present invention, rather than to limit the invention thereto.
Example (b): referring to fig. 1 to fig. 3, the waste gas treatment system for treating waste gas in a chemical reservoir area according to the present embodiment includes a VOCs transportation and condensation device and a VOCs adsorption and desorption device, which are sequentially disposed;
the VOCs conveying and condensing device comprises a first VOCs conveying path 1 and a VOCs condensing path 2 which are arranged in sequence;
VOCs adsorbs desorption device is including the second VOCs transport path 3 and the absorption desorption route 4 that set gradually, absorption desorption route 4 intercommunication is provided with hot nitrogen and blows off route 5, second VOCs transport path 3 with VOCs condensation route 2 intercommunication.
Specifically, the first VOCs conveying path 1 and the VOCs condensing path 2 are independently divided, the processing procedures of conveying, cooling and condensing and three-stage condensing of VOCs are reasonably standardized, so that VOCs waste gas with corresponding amount can be continuously and stably introduced conveniently, energy conservation and consumption reduction are realized to the maximum extent, meanwhile, moisture in the waste gas is condensed, the surface frosting speed of an evaporator in each subsequent condensing box is retarded, good heat exchange efficiency of each condensing box is ensured, and great strain is avoided in the subsequent adsorption and desorption procedures; and independently divide second VOCs transfer path 3, adsorption desorption route 4 and hot nitrogen blow off route 5, the VOCs waste gas of reasonable standard condensation carries and hot nitrogen desorption technology, adopts the hot nitrogen desorption mode, both can reach desorption behind the saturated condition with the organic matter, and the processing high efficiency of organic waste gas is greatly strengthened, improves the desorption rate, and reducible organic waste gas's emission reduces the influence to the environment again, improves production economy.
Preferably, the first VOCs transportation path 1 comprises a first transportation pipeline, a condensate tank 11 and a second transportation pipeline which are sequentially communicated, and an induced draft fan 12, a first valve 13, a gas flowmeter and a pressure transmitter are sequentially arranged on the second transportation pipeline; specifically, the induced draft fan 12 is a roots induced draft fan 12;
the VOCs condensation path 2 comprises a pre-cooling box 21, a first-stage shallow cooling box 22, a second-stage intermediate cooling box 23 and a third-stage deep cooling box 24 which are arranged in a loop, and the pre-cooling box 21 is communicated with the second conveying pipeline;
the VOCs gas sequentially passes through the pre-cooling box 21, the first-stage shallow cooling box 22, the second-stage middle cooling box 23 and the third-stage deep cooling box 24, so that the non-condensable gas flows back into the pre-cooling box 21 to form cold internal circulation; the method comprises the steps of combining a pre-cooling and three-stage condensation fractional condensation method, enabling waste gas to sequentially pass through a pre-cooling box 21, a first-stage shallow cooling box 22, a second-stage middle cooling box 23 and a third-stage deep cooling box 24 to obtain condensed VOCs liquid and non-condensable gas with a large amount of cold, transmitting the condensed VOCs liquid to an adsorption desorption device to perform a subsequent adsorption desorption process, and further refluxing the non-condensable gas to the pre-cooling box 21 to transfer the cold to the pre-cooling box 21, so that the condensation efficiency is further improved, and the energy consumption and the production cost are reduced; in addition, the first VOCs conveying path 1 and the VOCs condensing path 2 are controlled by a PLC, the VOCs condensing path 2 adopts a double-channel condensing process, and double-channel evaporators are arranged in parallel, so that alternate cooling and defrosting can be realized, and continuous 24-hour condensing recovery is really realized.
Preferably, the first-stage shallow cold box 22 comprises a first cold box body and a first return pipeline, and the first return pipeline sequentially passes through the first-stage compressor 221 and the first-stage air condenser 222 to realize return communication with the first cold box body; specifically, the primary compressor 221 performs refrigeration, and the first cold box body is refrigerated after being precooled by the primary air condenser 222, so that the number of the compressors is reduced, and the device cost and the operation energy consumption of the refrigeration system meeting the same temperature requirement are reduced.
Preferably, the secondary intermediate cooling box 23 includes a second cooling box body and a second return pipeline, and the second return pipeline sequentially passes through the secondary compressor 231 and the secondary air condenser 232 to realize return communication with the second cooling box body; specifically, the secondary compressor 231 performs refrigeration, and the secondary air condenser 232 performs precooling and then performs refrigeration on the second cold box body, so that the number of the compressors is reduced, and the device cost and the operation energy consumption of the refrigeration system meeting the same temperature requirement are reduced.
Preferably, the tertiary cryogenic tank 24 includes a third cold tank body and a third return conduit that in turn passes through a tertiary compressor 241 and a first heat exchanger 242 to achieve return communication with the third cold tank body;
the first heat exchanger 242 is connected with a fourth stage compressor 243 and a third stage wind condenser 244 in sequence through a fourth return pipeline; specifically, the three-stage compressor 241 refrigerates and refrigerates the first heat exchanger 242, and the four-stage compressor 243 refrigerates, and precools the first heat exchanger 242 through the three-stage air condenser 244, and refrigerates the third cold box body when the temperature of the first heat exchanger 242 reaches a set temperature, so that the third cold box body can quickly reach-60 to-70 ℃, the set number of compressors is reduced, and the device cost and the operation energy consumption of the refrigeration system meeting the same temperature requirement are reduced.
Preferably, the condensation temperature range of the pre-cooling box 21 is 5-25 ℃, the condensation temperature range of the first-stage shallow cooling box 22 is 1-10 ℃, the condensation temperature range of the second-stage middle cooling box 23 is-25 to-30 ℃, and the condensation temperature range of the third-stage deep cooling box 24 is-60 to-70 ℃; specifically, the condensation temperature ranges can be freely set according to actual condensation requirements, VOCs waste gas is condensed and liquefied under the gradient low-temperature condition, the temperature of non-condensable gas after passing through the three-stage deep cooling box 24 is as low as-70 ℃, in order to fully utilize the cold energy of the part, the non-condensable gas is creatively designed to flow back to the pre-cooling box 21, so that the energy is saved to the maximum extent, the consumption is reduced, meanwhile, the moisture in the waste gas is condensed, the surface frosting speed of the evaporator in each follow-up condensation box is retarded, and good heat exchange efficiency of each condensation box is guaranteed.
Preferably, the condensate tank 11 includes a first feeding port, a second feeding port and a first discharging port, the first feeding port is communicated with the first conveying pipeline, and the first discharging port is communicated with the second conveying pipeline, so as to optimize the feeding and discharging directionality and the ordering of the condensate tank 11.
Specifically, a second valve 14 is arranged on the first conveying pipeline; the first valve 13 and the second valve 14 are air inlet valves; the second valve 14 is used for communicating or blocking the transmission of the VOCs waste gas so as to adjust the throughput of the waste gas entering the first conveying pipeline; the first valve 13 is used for communicating or blocking the transmission of the VOCs waste gas so as to adjust the throughput of the waste gas entering the second conveying pipeline; and the valve and the like are used for interlocking switching, so that the safety of waste gas treatment between the device and the pipeline is further enhanced.
Specifically, the pressure transmitter is used for measuring, adjusting and indicating the internal pressure of the first VOCs conveying path 1, for example, the positive pressure at startup is 0-500 Pa, the negative pressure at suction is-300 Pa, the negative pressure at shutdown is-1000 Pa, the overpressure alarm evacuation is 2000Pa, and the pressure ranges can be freely set according to actual pressure requirements; in a preferred embodiment, if the gas pressure in the first conveying pipeline reaches a set value of "positive startup pressure", the induced draft fan 12 is started; if gas pressure is less than "shut down the negative pressure" set value in the first pipeline, then draught fan 12 stops, and PLC passes through the converter control the rotational speed of draught fan 12 makes first pipeline and second pipeline internal pressure are according to "the negative pressure that breathes in" set value, and upper and lower micro-fluctuation to introduce oil gas smoothly VOCs condensation route 2 is handled.
Preferably, the second VOCs transportation path 3 includes a third transportation pipe for transporting condensed VOCs and a fourth transportation pipe for transporting desorbed organic matters, and the third transportation pipe is communicated with the pre-cooling tank 21;
the adsorption and desorption path 4 comprises an adsorption tank 41 and an exhaust funnel 42 which are communicated through a fifth conveying pipeline, and the third conveying pipeline and the fourth conveying pipeline are respectively connected with the adsorption tank 41; the adsorption tank 41 absorbs the VOCs waste gas step by step, so that the adsorbent is fully and effectively utilized, the recovery efficiency of organic matter resources is improved, and the resource waste is reduced;
the hot nitrogen stripping path 5 comprises a nitrogen storage device 51 and a sixth conveying pipeline which are communicated, the sixth conveying pipeline is connected with the adsorption tank 41, and a heater 52 is arranged on the sixth conveying pipeline.
Preferably, the adsorption tank 41 comprises a third feeding port, a fourth feeding port, a second discharging port and a third discharging port;
the third feeding port is connected with the third conveying pipeline;
the fourth feed port is connected with the sixth conveying pipeline;
the second discharge hole is connected with the fourth conveying pipeline;
and the third discharge hole is connected with the fifth conveying pipeline.
Further, a flame arrester 31 and a third valve 32 are sequentially arranged along the conveying direction of the third conveying pipeline; in particular, the flame arrester 31 is used for blocking the flame transmission inside the third conveying pipeline, so as to further enhance the safety of waste gas treatment between the device and the pipeline; the third valve 32 is used to connect or block the transmission of the condensed liquid in the third delivery pipe so as to adjust the introducing amount of VOCs into the adsorption tank 41.
Preferably, a fourth valve 33, a second heat exchanger 34, a vacuum pump 35 and a check valve 36 are sequentially arranged along the conveying direction of the fourth conveying pipeline; specifically, under the pumping action of vacuum pump 35, the organic matter that has desorbed is followed the further cooling lime set of making in fourth pipeline backward flow to first VOCs delivery path 1, the organic matter that has desorbed is cooled down to second heat exchanger 34, check valve 36 is used for blocking the organic matter backward flow that has desorbed.
Preferably, a pressure regulating valve 53 and a fifth valve 54 are respectively arranged on the sixth conveying pipeline corresponding to the nitrogen storage device 51 and the heater 52, and between the heater 52 and the fourth feeding hole; specifically, the heater 52 is electrically heated to heat the nitrogen gas to a desired temperature, the pressure regulating valve 53 is used for regulating the nitrogen gas output pressure of the nitrogen gas storage device 51, and the fifth valve 54 is used for communicating or blocking the transmission of the nitrogen gas in the sixth conveying pipeline, so as to adjust the nitrogen gas introduction amount of the adsorption tank 41.
Further, a sixth valve 43 is disposed on the fifth delivery pipe, and the sixth valve 43 is used for communicating or blocking the transmission of the desorbed gas in the fifth delivery pipe, so as to adjust the gas discharge amount of the adsorption tank 41.
Preferably, a plurality of sets of zeolite molecular sieve layers are arranged in parallel at intervals in the adsorption tank 41, the zeolite molecular sieve layers are molecular sieve frameworks formed by three-dimensionally stacking SiO4 tetrahedra and AlO4 tetrahedra through vertexes to form 4, 5, 6, 8, 10 or 12-membered rings, further form channels with 0.3-1.2 nm pores and so-called cages, present a one-, two-or three-dimensional topological structure, and the molecular sieve frameworks all have similar chemical compositions and different channel topological structures.
When Si atoms in the molecular sieve framework are replaced by Al atoms, the zeolite molecular sieve framework carries negative charges, the negative charges are compensated by univalent or multivalent cations outside the framework, the affinity to polar molecules is higher in adsorption performance, the molecules with similar sizes are easier to be adsorbed by the molecular sieve when the polarity is larger, the capacity of the molecular sieve for adsorbing organic molecules is increased along with the increase of the unsaturation, the molecular sieve has strong adsorption capacity, and can still keep higher adsorption capacity under the conditions of low adsorbate concentration and higher adsorption temperature, the balance adsorption capacity of common adsorbents such as silica gel and active alumina is greatly influenced by the adsorbate concentration and even loses the adsorption capacity at higher adsorption temperature, and the molecular sieve can be widely applied to the deep drying and purifying processes of gas and liquid due to the characteristics, and the molecular sieve can be separated from other adsorbents due to the easiness in adjustment and less integral stability of the pore structure. Therefore, the zeolite molecular sieve layer is adopted in the embodiment to adsorb the organic waste gas with high flow rate and medium and low concentration.
Specifically, adsorption tanks 41 are at least provided with two groups in parallel, and two adsorption tanks 41 are adopted to absorb VOCs step by step, so that the adsorption and desorption efficiency of organic substances is greatly improved.
The embodiment also discloses a treatment method of the waste gas treatment system for treating the waste gas in the chemical storage area, which comprises the following steps:
step 6, after the waste gas is refrigerated to-60 to-70 ℃ through the three-stage deep cooling box 24, obtaining condensed VOCs liquid and non-condensable gas, wherein the non-condensable gas further flows back into the pre-cooling box 21 so as to transfer cold energy into the pre-cooling box 21;
step 7, introducing clean nitrogen into the adsorption tank 41 along a sixth conveying pipeline to purge the zeolite molecular sieve layer so as to remove part of oxygen and water vapor in the gas phase in the adsorption tank 41;
step 8, introducing the condensed VOCs liquid into the adsorption tank 41 along a third conveying pipeline, adsorbing organic matters in the condensed VOCs liquid by the zeolite molecular sieve layer, closing the third valve 32 to stop introducing the condensed VOCs liquid after the organic matters adsorbed by the zeolite molecular sieve layer reach a saturated state, and discharging the desorbed gas from the exhaust funnel 42;
step 9, heating clean nitrogen by a heater 52, introducing the heated clean nitrogen into the adsorption tank 41 for stripping, desorbing organic matters from the zeolite molecular sieve layer, and outputting the desorbed organic matters along a fourth conveying pipeline to realize adsorption and desorption of the organic matters in the VOCs; at this time, the zeolite molecular sieve layer recovers the activity thereof, namely regeneration.
The waste gas treatment system for treating the waste gas in the chemical reservoir area has the following advantages: according to the invention, the VOCs conveying and condensing device is used for independently dividing the first VOCs conveying path and the VOCs condensing path, so that the processing procedures of conveying, cooling and condensing, and three-stage condensation of VOCs are reasonably standardized, the VOCs waste gas with corresponding quantity can be continuously and stably introduced conveniently, the energy is saved to the maximum extent, the consumption is reduced, the moisture in the waste gas is condensed, the surface frosting speed of an evaporator in each subsequent condenser box is retarded, the condenser boxes are ensured to keep good heat exchange efficiency, and the phenomenon of great strain caused by the subsequent adsorption and desorption procedures is avoided; and the VOCs adsorbs desorption device and independently divides second VOCs delivery path, adsorbs desorption route and hot nitrogen blows off the route, and the VOCs waste gas of reasonable standard condensation carries and hot nitrogen desorption technology, adopts hot nitrogen desorption mode, both can reach desorption behind the saturated condition with the organic matter, and the processing high efficiency of organic waste gas is strengthened to very big degree ground, improves the desorption rate, and the emission of reducible organic waste gas reduces the influence to the environment again, improves production economy.
The foregoing is merely a preferred embodiment of the invention and is not intended to limit the invention in any manner. Those skilled in the art can make many possible variations and modifications to the disclosed solution, or modify the equivalent embodiments using the technical means and teachings disclosed above, without departing from the scope of the present solution. Therefore, all equivalent changes made according to the shape, structure and principle of the present invention should be covered by the protection scope of the present invention without departing from the contents of the technical scheme of the present invention.
Claims (10)
1. A waste gas treatment system for treating waste gas in a chemical reservoir area is characterized by comprising a VOCs conveying and condensing device and a VOCs adsorption and desorption device which are sequentially arranged;
the VOCs conveying and condensing device comprises a first VOCs conveying path and a VOCs condensing path which are sequentially arranged;
VOCs adsorbs desorption device including the second VOCs transport path and the absorption desorption route that set gradually, it is provided with the hot nitrogen and blows off the route to adsorb desorption route intercommunication, second VOCs transport path with VOCs condensation route intercommunication.
2. The waste gas treatment system for treating the waste gas of the chemical reservoir area according to claim 1, wherein the first VOCs conveying path comprises a first conveying pipeline, a condensate tank and a second conveying pipeline which are sequentially communicated, and an induced draft fan, a first valve, a gas flowmeter and a pressure transmitter are sequentially arranged on the second conveying pipeline.
3. The exhaust treatment system for treating chemical reservoir exhaust according to claim 2, wherein the VOCs condensation path comprises a pre-cooling tank, a first-stage shallow cooling tank, a second-stage medium cooling tank and a third-stage deep cooling tank which are arranged in a loop, and the pre-cooling tank is communicated with the second conveying pipeline;
VOCs gas sequentially passes through the pre-cooling box, the first-stage shallow cooling box, the second-stage middle cooling box and the third-stage deep cooling box, so that non-condensable gas flows back into the pre-cooling box to form cold internal circulation.
4. The waste gas treatment system for treating the waste gas in the chemical storage area according to claim 3, wherein the condensation temperature range of the pre-cooling tank is 5-25 ℃, the condensation temperature range of the first-stage shallow cooling tank is 1-10 ℃, the condensation temperature range of the second-stage medium cooling tank is-25-30 ℃, and the condensation temperature range of the third-stage deep cooling tank is-60-70 ℃.
5. The waste gas treatment system for treating waste gas of a chemical reservoir area according to claim 4, wherein the condensate tank comprises a first feeding hole, a second feeding hole and a first discharging hole, the first feeding hole is communicated with the first conveying pipeline, and the first discharging hole is communicated with the second conveying pipeline.
6. The effluent treatment system for treating effluent gases from a chemical reservoir as claimed in claim 5, wherein the second transportation path for VOCs includes a third transportation conduit for transporting condensed VOCs and a fourth transportation conduit for transporting desorbed organic compounds, the third transportation conduit communicating with the pre-cooling tank;
the adsorption and desorption path comprises an adsorption tank and an exhaust funnel which are communicated through a fifth conveying pipeline, and the third conveying pipeline and the fourth conveying pipeline are respectively connected with the adsorption tank;
the hot nitrogen blows and takes off route including nitrogen gas storage device and the sixth pipeline that the intercommunication set up, the sixth pipeline with the adsorption tank is connected, in be provided with the heater on the sixth pipeline.
7. The exhaust gas treatment system for treating waste gas of a chemical reservoir area according to claim 6, wherein the adsorption tank comprises a third feed port, a fourth feed port, a second discharge port and a third discharge port;
the third feed port is connected with the third conveying pipeline;
the fourth feed port is connected with the sixth conveying pipeline;
the second discharge hole is connected with the fourth conveying pipeline;
and the third discharge hole is connected with the fifth conveying pipeline.
8. The exhaust gas treatment system for treating the exhaust gas of the chemical reservoir area according to claim 7, wherein a plurality of zeolite molecular sieve layers are arranged in parallel at intervals in the adsorption tank.
9. The exhaust gas treatment system for treating chemical reservoir exhaust gas according to claim 8, wherein the zeolite molecular sieve layer is made of SiO 4 And AlO 4 The tetrahedron is stacked according to the vertex according to the three-dimension to form the molecular sieve framework.
10. A treatment method of an exhaust gas treatment system for treating exhaust gas from a chemical reservoir area, the treatment method comprising the steps of:
step 1, introducing VOCs waste gas along a first conveying pipeline, and entering a condensate tank for preliminary cooling and condensation;
step 2, sucking the primarily cooled and condensed waste gas to a precooling box along a second conveying pipeline through a draught fan, and measuring the gas flow and the gas velocity of the waste gas in the second conveying pipeline through a gas flow meter;
step 3, pre-cooling the waste gas in the pre-cooling box, and then feeding the waste gas into a first-stage shallow cooling box;
step 4, refrigerating the waste gas to 1-10 ℃ through the primary shallow cooling box, and then entering a secondary intercooler;
step 5, refrigerating the waste gas to-25 to-30 ℃ through the secondary intercooler tank, and then feeding the waste gas into a tertiary intercooler tank;
step 6, after the waste gas is refrigerated to-60 to-70 ℃ through the three-stage deep cooling box, obtaining condensed VOCs liquid and non-condensable gas, wherein the non-condensable gas further flows back into the pre-cooling box to transfer cold energy into the pre-cooling box;
step 7, introducing clean nitrogen into the adsorption tank along a sixth conveying pipeline to purge the zeolite molecular sieve layer so as to remove part of oxygen and water vapor in the gas phase in the adsorption tank;
step 8, introducing the condensed VOCs liquid into the adsorption tank along a third conveying pipeline, adsorbing organic matters in the condensed VOCs liquid by the zeolite molecular sieve layer, closing a third valve to stop introducing the condensed VOCs liquid after the organic matters adsorbed by the zeolite molecular sieve layer reach a saturated state, and discharging desorbed gas by an exhaust funnel;
and 9, heating clean nitrogen by a heater, introducing the heated clean nitrogen into the adsorption tank for stripping, desorbing organic matters from the zeolite molecular sieve layer, and outputting the desorbed organic matters along a fourth conveying pipeline to realize adsorption and desorption of the organic matters in the VOCs.
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