CN113797705B - Gas concentration device, organic solvent recovery system and organic gas recovery concentration method - Google Patents
Gas concentration device, organic solvent recovery system and organic gas recovery concentration method Download PDFInfo
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- CN113797705B CN113797705B CN202110928203.7A CN202110928203A CN113797705B CN 113797705 B CN113797705 B CN 113797705B CN 202110928203 A CN202110928203 A CN 202110928203A CN 113797705 B CN113797705 B CN 113797705B
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- 239000003960 organic solvent Substances 0.000 title claims abstract description 128
- 238000011084 recovery Methods 0.000 title claims abstract description 57
- 238000000034 method Methods 0.000 title claims abstract description 26
- 238000001179 sorption measurement Methods 0.000 claims abstract description 142
- 230000008929 regeneration Effects 0.000 claims abstract description 57
- 238000011069 regeneration method Methods 0.000 claims abstract description 57
- 238000004519 manufacturing process Methods 0.000 claims abstract description 53
- 238000009833 condensation Methods 0.000 claims abstract description 22
- 230000005494 condensation Effects 0.000 claims abstract description 22
- 238000001816 cooling Methods 0.000 claims abstract description 21
- 238000000746 purification Methods 0.000 claims abstract description 14
- 239000007789 gas Substances 0.000 claims description 169
- 238000010438 heat treatment Methods 0.000 claims description 14
- 238000003795 desorption Methods 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 5
- 239000000498 cooling water Substances 0.000 claims description 4
- 230000001172 regenerating effect Effects 0.000 claims description 3
- 230000008569 process Effects 0.000 claims description 2
- 230000008901 benefit Effects 0.000 abstract description 2
- 239000002957 persistent organic pollutant Substances 0.000 abstract 1
- 239000003570 air Substances 0.000 description 11
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 10
- 239000003463 adsorbent Substances 0.000 description 9
- 238000004064 recycling Methods 0.000 description 7
- 239000007788 liquid Substances 0.000 description 6
- 238000000926 separation method Methods 0.000 description 5
- HBBGRARXTFLTSG-UHFFFAOYSA-N Lithium ion Chemical compound [Li+] HBBGRARXTFLTSG-UHFFFAOYSA-N 0.000 description 4
- 238000010521 absorption reaction Methods 0.000 description 4
- 229910001416 lithium ion Inorganic materials 0.000 description 4
- 239000002808 molecular sieve Substances 0.000 description 4
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 4
- 239000000112 cooling gas Substances 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000012855 volatile organic compound Substances 0.000 description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 238000004134 energy conservation Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 238000003912 environmental pollution Methods 0.000 description 2
- 230000013011 mating Effects 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000002904 solvent Substances 0.000 description 2
- 230000002411 adverse Effects 0.000 description 1
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 1
- 239000012080 ambient air Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 239000011248 coating agent Substances 0.000 description 1
- 238000000576 coating method Methods 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005485 electric heating Methods 0.000 description 1
- 230000002209 hydrophobic effect Effects 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 239000003566 sealing material Substances 0.000 description 1
- 239000004065 semiconductor Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- B01D53/06—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 moving adsorbents, e.g. rotating beds
-
- 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
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D207/00—Heterocyclic compounds containing five-membered rings not condensed with other rings, with one nitrogen atom as the only ring hetero atom
- C07D207/02—Heterocyclic compounds containing five-membered rings not condensed with other rings, with one nitrogen atom as the only ring hetero atom with only hydrogen or carbon atoms directly attached to the ring nitrogen atom
- C07D207/18—Heterocyclic compounds containing five-membered rings not condensed with other rings, with one nitrogen atom as the only ring hetero atom with only hydrogen or carbon atoms directly attached to the ring nitrogen atom having one double bond between ring members or between a ring member and a non-ring member
- C07D207/22—Heterocyclic compounds containing five-membered rings not condensed with other rings, with one nitrogen atom as the only ring hetero atom with only hydrogen or carbon atoms directly attached to the ring nitrogen atom having one double bond between ring members or between a ring member and a non-ring member with hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
- C07D207/24—Oxygen or sulfur atoms
- C07D207/26—2-Pyrrolidones
- C07D207/263—2-Pyrrolidones with only hydrogen atoms or radicals containing only hydrogen and carbon atoms directly attached to other ring carbon atoms
- C07D207/267—2-Pyrrolidones with only hydrogen atoms or radicals containing only hydrogen and carbon atoms directly attached to other ring carbon atoms with only hydrogen atoms or radicals containing only hydrogen and carbon atoms directly attached to the ring nitrogen atom
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
- F28D21/0001—Recuperative heat exchangers
- F28D21/0014—Recuperative heat exchangers the heat being recuperated from waste air or from vapors
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Analytical Chemistry (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Treating Waste Gases (AREA)
Abstract
The invention relates to an organic gas concentration device, an organic solvent recovery system and an organic gas recovery concentration method, wherein an adsorption rotor of the organic gas concentration device comprises an adsorption zone, a regeneration zone and a cooling zone; the adsorption zone comprises more than two sub-adsorption zones, the more than two sub-adsorption zones are sequentially communicated, and the gas to be treated sequentially passes through the sub-adsorption zones to be subjected to multi-zone gradual purification adsorption so as to enable the tail gas to be close to zero emission; the organic solvent recovery system combines heat exchange, condensation recovery and adsorption concentration, wherein the heat exchange adopts multistage heat exchange, and is suitable for heat exchange between high-temperature tail gas containing organic solvent discharged from production equipment and low-temperature tail gas returned to the production equipment after the organic solvent is recovered. The invention not only greatly improves the recovery rate of the organic solvent and increases the economic benefit, but also reduces the organic pollutants discharged into the environment, thereby achieving the purpose of economically and efficiently treating the tail gas polluted by the organic solvent of the production equipment.
Description
Technical Field
The invention relates to a system and a method for recycling organic solvents and purifying Volatile Organic Compounds (VOCs) polluted gas, in particular to a system and a method for recycling organic solvents by combining adsorption concentration and condensation.
Background
The organic solvent used in some production processes (such as semiconductor manufacturing and lithium ion battery production processes) volatilizes into the surrounding environment in the production process, so that not only can the pollution of the ambient air be caused, but also the cost of the product manufacturing is greatly increased due to the fact that some organic solvent is directly discharged into the environment due to high price, so that an economic and efficient organic solvent recovery method is adopted to recover the organic solvent, and the method becomes an important subject of attention.
The recovery method of the organic solvent in the tail gas discharged from the common production equipment includes a condensation recovery method, an adsorption separation method and an absorption separation method (also called a water washing method for the water-soluble organic solvent). The condensation recovery method is to directly cool the tail gas containing the organic solvent to reduce the temperature of the tail gas below the dew point of the organic solvent, and condense the organic solvent contained in the tail gas into liquid for recovery. The adsorption separation method is to adsorb the organic solvent in the tail gas containing the organic solvent by using an adsorbent to separate the organic solvent from the tail gas, then desorb the organic solvent adsorbed in the adsorbent by a desorption operation, and then recover the organic solvent by a condensation operation. The absorption and separation method is to absorb the organic solvent in the tail gas by using the absorption liquid to separate the organic solvent from the tail gas, and then separate the organic solvent from the absorption liquid by distillation and other methods to obtain the organic solvent. At present, for some tail gas with large air volume and low concentration and containing organic solvent, a method of combining separation, concentration and condensation of an adsorption rotor is generally adopted. The concentration of the organic solvent in the gas at the outlet of the adsorption rotor adsorption zone can be reduced to below 10ppm in general, although the environmental emission standard is met. However, the total air volume of the drying engineering can reach 3500Nm 3/min due to the large exhaust air volume discharged in the general production process, such as a lithium ion battery plant with the speed of 4 GWh/Y. Even if the concentration of the organic solvent NMP in the gas discharged through the adsorption purification is only 10ppm, if the production apparatus is operated continuously for 8520 hours (355 days, 24 hours/day) per year, the total amount of NMP to be discharged into the atmosphere per year can reach about 79 tons. Not only causes the waste of raw and auxiliary materials, but also has adverse effect on the environment. Therefore, further reduction of the concentration of the organic solvent in the exhaust gas discharged to the atmosphere has become a new problem of reducing the production cost and reducing the environmental pollution.
In order to solve the above problems, a method of using two stages of adsorption devices in series has been proposed (japanese laid-open patent publication JP 2014-521A), in which in order to achieve an improvement in the purification rate and a reduction in the concentration of the organic solvent in the exhaust gas, two stages of adsorption are used, and the gas to be treated is purified by adsorption with a first adsorbent and then sent to a second adsorbent for further purification, and then discharged to the atmosphere after reaching the desired concentration. Although the method can reduce the concentration of the organic solvent in the tail gas discharged into the atmosphere to the desired low concentration, the method is not the best solution to the problems of high equipment investment, large occupied area, complex system operation and the like of the system due to the adoption of the two-stage adsorption purification device.
Disclosure of Invention
In view of the fact that the prior art cannot simultaneously meet the requirements of low equipment investment and high exhaust gas purification rate of users, the main purpose of the invention is to provide an organic solvent recovery system which meets the requirements of customers and markets and combines adsorption concentration and condensation.
In order to achieve the above object, a first aspect of the present invention provides a gas recovery concentration device comprising: an adsorption rotor; a central shaft about which the suction rotor rotates; the adsorption rotor comprises an adsorption zone, a regeneration zone and a cooling zone; the adsorption zone comprises more than two sub-adsorption zones, the more than two sub-adsorption zones are sequentially communicated, and the gas to be recovered sequentially passes through the sub-adsorption zones to be subjected to multi-zone gradual purification adsorption so as to enable the tail gas to reach the emission standard; the cooling area receives external air or the gas to be recovered so as to cool the adsorption rotor; and the regeneration zone is used for desorbing and concentrating the organic solvent adsorbed on the adsorption rotor in a heating regeneration mode.
Further, the heating regeneration mode includes a mode of heating by a regeneration heater or a mode of directly using the external air heated after passing through the cooling zone or the gas to be recovered for heating desorption.
Further, the outside air after passing through the cooling zone or the gas to be recovered is heated by the regeneration heater and then is sent into the regeneration zone as regeneration gas.
Preferably, the number of the sub-adsorption areas is 2, namely a first sub-adsorption area and a second sub-adsorption area, and the area of the first sub-adsorption area is larger than that of the second sub-adsorption area.
Optionally, the adsorption rotor is divided into a first sub-adsorption zone, a regeneration zone, a cooling zone and a second sub-adsorption zone in turn in the rotating direction of the rotating wheel.
In a second aspect, the present invention provides an organic solvent recovery system using a combination of adsorption concentration and condensation for recovering an organic solvent from an organic solvent-containing tail gas discharged from a production apparatus, comprising: the device comprises a heat exchange component, an organic solvent condensing and recycling device and the gas recycling and concentrating device; the heat exchange assembly comprises at least one heat exchanger, wherein the heat exchanger exchanges heat between high-temperature tail gas containing the organic solvent discharged from the production equipment and low-temperature tail gas returned to the production equipment after the organic solvent is recovered; an organic solvent condensing and recovering device for condensing and recovering the organic solvent from the gas from the heat exchange assembly and the regeneration gas concentrated by the gas recovering and concentrating device; and the gas recovery concentration device is used for carrying out gradual adsorption recovery and concentration regeneration on the residual organic solvent gas after passing through the organic solvent condensation recovery device, and part of the residual low-temperature tail gas after adsorption is discharged, and part of the residual low-temperature tail gas is returned to the production device after heat exchange through the heat exchange component.
Preferably, the heat exchange assembly comprises at least two heat exchangers, and reverse cascade heat exchange is carried out between the high-temperature gas containing the organic solvent discharged from the production equipment and the low-temperature tail gas returned to the production equipment after the organic solvent is recovered through at least two stages of heat exchangers.
Further, the organic solvent condensation recovery device comprises at least two of a normal-temperature water cooler, a cooling water condenser, a heat pipe and a direct expansion pipe.
The third aspect of the present invention also provides a method for concentrating an organic gas, characterized by comprising the steps of:
i) Step of purifying and adsorbing the organic gas step by step in a multi-region of an adsorption rotor to enable the treated low-temperature tail gas to reach the emission standard;
ii) subjecting the adsorbent to regenerative heating to produce a regenerated concentrated organic gas;
iii) And cooling the adsorbent.
In addition, the fourth aspect of the present invention further provides a method for recovering and concentrating an organic solvent, characterized by comprising the steps of:
i) A step of heat-recovering the high-temperature tail gas containing the organic solvent discharged from the production facility;
ii) a step of condensing the tail gas after heat recovery to recover a large amount of the target organic solvent;
iii) Step of purifying and adsorbing the condensed tail gas step by step in a multi-region of an adsorption rotor so as to enable the treated low-temperature tail gas to reach the emission standard;
iv) carrying out regeneration heating desorption on the organic solvent adsorbed in the adsorption rotor in the multi-zone step-by-step purification adsorption process to generate regenerated concentrated organic solvent gas;
v) a step of recovering the regenerated concentrated organic solvent gas by secondary condensation;
vi) a step of heat-exchanging the low-temperature tail gas after multi-zone stepwise purification and adsorption with heat generated by heat recovery in step i) to generate high-temperature gas for recycling to production equipment.
Preferably, the heat recovery in step i) and the heat exchange in step vi) comprise at least two heat recovery and heat exchange steps.
Optionally, the condensing treatment in step ii) comprises at least two condensing treatment steps.
Based on the design, the invention has the beneficial effects that: a plurality of adsorption areas, preferably two adsorption areas, are arranged on one adsorption rotor, wherein the first sub-adsorption area is used for adsorbing organic solvent in tail gas containing the organic solvent, which is needed to be discharged out of the system, from part of the production device; the second sub-adsorption zone is used for further adsorbing and purifying the organic solvent in the tail gas which is adsorbed by the first sub-adsorption zone and needs to be discharged outside the system, so that the organic solvent in the discharged tail gas is close to zero emission. In addition, a cascade serial heat exchange mode is adopted, so that heat exchange is carried out between high-temperature tail gas containing the organic solvent discharged from production equipment and low-temperature tail gas returned to the production equipment after the organic solvent is recovered, the temperature of gas returned to the production equipment is greatly improved, and the organic combination of energy conservation, environmental protection and economic benefit is realized.
Drawings
FIG. 1 is a schematic view of the front surface of an adsorption rotor of a preferred embodiment of a gas concentration device according to the present invention.
FIG. 2 is a schematic flow diagram of a preferred embodiment of the organic solvent recovery system of the present invention.
In fig. 1-2:
100. production equipment; 200. a heat exchanger; 210. a first stage heat exchanger; 220. a second stage heat exchanger; 300. a solvent condensing and recycling device; 310. a cooler; 320. a condenser; 330 recovering the storage tank; 400. an adsorption rotor; 410. a first sub-adsorption zone; 420. a second sub-adsorption zone; 430. a cooling zone; 440. a regeneration zone; 500. a regenerative heater; 600. a processed gas blower; 700. a regeneration gas blower.
Detailed Description
In order to enable those skilled in the art to better understand the technical solutions of the present invention, the technical solutions in the embodiments of the present invention will be clearly and completely described below with reference to the embodiments shown in the drawings. It should be understood that these embodiments are not intended to limit the present invention, and that functional, method, or structural equivalents and alternatives falling within the scope of the present invention may be modified by any person skilled in the art to include such embodiments.
Meanwhile, in the present specification, references to the description of the orientation such as upper, lower, left, right, front, rear, inner, outer, longitudinal, lateral, vertical, horizontal, etc., are based on the orientation or positional relationship shown in the drawings, only for convenience of description and simplification of the description, and do not indicate or imply that the apparatus or element to be referred to must have a specific orientation, be constructed and operated in a specific orientation, and thus should not be construed as limiting the present invention.
In the description of the present invention, unless explicitly stated or limited otherwise, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected, mechanically connected, electrically connected, directly connected, indirectly connected via an intermediate medium, or in communication between two elements. It will be understood by those of ordinary skill in the art that the specific meaning of the terms above in the present invention should not be construed as limiting the invention as the case may be.
Fig. 1 shows a preferred embodiment of the adsorption rotor according to the present invention, and the adsorption rotor 400 can perform adsorption recovery and concentration treatment on the organic solvent contained in the tail gas discharged to the outside of the system. When the adsorption rotor 400 operates, the adsorption rotor is driven by a driving motor (not shown in the drawing) to rotate around a central shaft, and is divided into a first sub-adsorption zone 410, a regeneration zone 440, a cooling zone 430 and a second sub-adsorption zone 420 in turn by a rotating wheel frame, a bracket and a sealing material (not shown in the drawing) in the rotating direction, that is, the adsorption material carried by the adsorption rotor 400 sequentially passes through the first sub-adsorption zone 410, the regeneration zone 440, the cooling zone 430 and the second sub-adsorption zone 420 in operation, and the area of the first sub-adsorption zone is larger than that of the second sub-adsorption zone, so that part of the tail gas containing the organic solvent which is in a relatively high concentration state and is required to be discharged out of the system passes through the first sub-adsorption zone at a relatively low wind speed, and on the other hand, the area of the second sub-adsorption zone is smaller, the flow rate of the treated gas in a relatively low concentration can be improved so as to increase the collision contact probability with the surface of a gas channel of the adsorption rotor, thereby achieving the aim of improving the adsorption purification efficiency; the adsorbent carried by the adsorption rotor is dependent on the organic solvent to be adsorbed, and the adsorbent material is typically, but not limited to, a hydrophobic molecular sieve, which generally refers to a molecular sieve having a silica to alumina ratio Si/Al of greater than 20, such as ZSM-5 type molecular sieve, Y type molecular sieve, and the like. In a preferred embodiment of the present invention, external air or gas to be recovered may be used, and the gas to be recovered is preferably used as cooling gas to cool the adsorption rotor, and the cooling gas may be heated and desorbed and concentrated directly in the regeneration zone after being heated by the cooling zone, when the desorption efficiency is reduced due to low temperature, the cooling gas heated by the cooling zone through heat exchange may be sent to the regeneration zone after being heated to the regeneration temperature again by the regeneration heater 500, or concentrated organic gas may be generated directly by heating by the regeneration heater, and the heating source of the regeneration heater 500 is preferably high-temperature hot oil, high-temperature steam, or electric heating.
In addition, it should be understood that although the number of sub-adsorption zones is two in the present embodiment and the shape of the adsorption rotor is circular, the number and shape should not be construed as limiting the scope of protection of the claims, and those skilled in the art can select any number of sub-adsorption zones and design any shape of the adsorption rotor according to the requirements of the exhaust emission standard.
Fig. 2 shows a preferred embodiment of the organic solvent recovery system according to the present invention, in which the organic solvent recovery system is an organic solvent recovery system combining adsorption concentration and condensation, for recovering an organic solvent from a tail gas containing the organic solvent discharged from a production apparatus, as shown in fig. 2, the recovery system includes: the production facility 100, the heat exchange assembly, the organic solvent condensing and recovering device, and the adsorption rotor and its mating structure described above; the heat exchange assembly comprises at least one heat exchanger, and in order to further improve the heat exchange performance in practical production, two heat exchangers are preferably used, namely: a first stage heat exchanger 210 and a second stage heat exchanger 220; the organic solvent condensation recovery device comprises a cooler 310, a condenser 320 and a recovery storage tank 330; the adsorption rotor and its mating structure include the adsorption rotor 400, the regeneration heater 500, the treated gas blower 600, and the regeneration gas blower 700 described above. The system is used for recycling the organic solvent in the tail gas containing the organic solvent discharged by the production equipment. The source of the tail gas of the production equipment containing the organic solvent can be, but is not limited to, exhaust air of an oven of a lithium ion battery anode coating machine, and the organic solvent can be, but is not limited to, organic solvents such as N-methyl pyrrolidone (NMP) or volatile organic compounds.
It should be understood that, although two heat exchangers are used in the present embodiment and the condensation recovery apparatus selects the collocation between the cooler and the condenser, it should not be understood as limiting the scope of protection of the claims, and those skilled in the art may select at least one heat exchanger according to the actual heat exchange performance requirement, and select at least two of the normal temperature water cooler, the cooling water condenser, the heat pipe, and the direct expansion pipe as the combination of the condensation recovery apparatus.
In this embodiment, the first stage heat exchanger 210 and the second stage heat exchanger 220 perform reverse step heat exchange between the high temperature tail gas containing the organic solvent discharged from the production facility and the low temperature tail gas after the organic solvent is recovered in the production facility, so that the tail gas containing the high concentration organic solvent having a temperature of up to 100 ℃ or more from the production facility 100 is cooled to a normal temperature state (typically, a temperature of about 30 to 40 ℃) and the low temperature tail gas (typically, a temperature of less than 15 ℃) after the organic solvent is recovered in the production facility 100 from the outlet of the condenser 320 is heated to 75 ℃ or more. The organic solvent condensing and recovering device condenses and recovers the organic solvent from the gas from the heat exchange unit and the regeneration gas concentrated by the gas recovering and concentrating device, wherein the cooler 310 further cools the tail gas from the second stage heat exchanger 220 by the cooling water from the cooling tower at a temperature around 30 ℃, and the condenser 320 cools the tail gas from the cooler 310 by the low-temperature cold water (typically at a temperature below 12 ℃) to condense the organic solvent in the tail gas into a liquid and then recovers the liquid. The gas recovery concentration device is used for carrying out gradual adsorption recovery on the residual organic solvent gas after passing through the organic solvent condensation recovery device, and part of the residual low-temperature tail gas after adsorption is discharged, and part of the residual low-temperature tail gas is returned to the production device 100 after heat exchange through the heat exchange component. The processed gas blower 600 is used for sequentially blowing processed gas into the first adsorption zone 410 of the adsorption rotor 400, sending the processed gas which is primarily purified by the first sub-adsorption zone 410 into the second adsorption zone 420, adsorbing and removing almost all organic solvent contained in the tail gas after the two times of adsorption and purification by the adsorption rotor 400, and discharging the purified gas to the outside of the system; the regeneration fan 700 blows the regeneration gas heated to a predetermined temperature by the regeneration heater 500 from the regeneration zone inlet to the regeneration zone 440 of the adsorption rotor 400, blows the regeneration gas desorbed from the organic solvent adsorbed in the adsorption rotor 400 to the inlet end of the cooler 310, mixes the regeneration gas with the low-temperature tail gas cooled by the recovered organic solvent returned to the production facility 100 through the second-stage heat exchanger 220, and then introduces the cooled tail gas containing the high-concentration organic solvent into the cooler 310, and further condenses and recovers the organic solvent by the condenser 320.
In the design of the present preferred embodiment, as shown in fig. 2, the amount of air of the organic solvent-containing off-gas a from the production facility 100 is 110,000nm 3/h, the temperature is 100 ℃, the concentration of the organic solvent-containing N-methylpyrrolidone (NMP) is 2279ppm, the off-gas b having a temperature reduced to 70.3 c after heat exchange with the off-gas h having a temperature of about 50.5 c from the outlet of the second stage heat exchanger 220 enters the second stage heat exchanger 220, and the off-gas g returned from the outlet of the condenser 320 (the amount of air is 99,500nm 3/h, the temperature is 12 ℃ and is reduced to 35.3 ℃ after heat exchange, the tail gas c with the temperature of 35.3 ℃ and the gas d (the air quantity is 111,500Nm 3/h, the temperature is 35.6 ℃ and the NMP concentration is 2278 ppm) obtained by mixing the regeneration outlet gas s led out by a regeneration fan 700 at the outlet of a regeneration zone 440 of an adsorption rotor 400 are sequentially fed into a cooler 310 and a condenser 320, the outlet gas f of the condenser 320 is cooled to 12 ℃, a substantial portion of the organic solvent NMP contained therein is condensed into a liquid which enters the recovery tank 330 and a substantial portion of the off-gas g at the outlet of the condenser 320 is returned to the low temperature side inlet of the second stage heat exchanger 220. On the other hand, a small part of the exhaust gas l required to be discharged to the outside of the system is sent to the first sub-adsorption zone 410 of the adsorption rotor 400, a substantial part of the organic solvent contained in the exhaust gas is adsorbed in the adsorption rotor 400 by the adsorption of the adsorbent in the adsorption rotor 400, the exhaust gas passing through the first sub-adsorption zone 410 is sent to the second sub-adsorption zone 420, almost all of the organic solvent contained in the exhaust gas is adsorbed by the adsorption rotor 400, the concentration of NMP in the exhaust gas at the outlet of the second sub-adsorption zone 420 is reduced to 1ppm or less, and the purified exhaust gas o is discharged to the atmosphere. The cooling zone 430 of the adsorption rotor 400 is introduced with the same exhaust gas p as the inlet of the first sub-adsorption zone 410, the temperature of the exhaust gas q at the outlet of the cooling zone 430 is raised to 170 ℃ or higher, and the exhaust gas q is sent to the regeneration heater 500 to be heated to 200 ℃ and then sent to the regeneration zone 440 of the adsorption rotor 400 as regeneration gas r, the organic solvent adsorbed in the rotating wheel is subjected to high-temperature desorption, the concentration of NMP in the outlet gas s of the regeneration zone 440 reaches 2250ppm, the temperature is about 60 ℃, and the gas is mixed with the exhaust gas c at the outlet of the second stage heat exchanger 220 and then sent to the high-temperature inlet side of the cooler 310. From the above design results, it can be seen that: the system can reduce the concentration of the organic solvent in the part of the tail gas which needs to be discharged into the atmosphere to about 1ppm, and the temperature of the tail gas returned to the production equipment 100 can reach more than 80 ℃.
Compared with the existing solvent recovery system adopting two adsorption devices in series, the preferred embodiment of the invention only uses one adsorption rotor, realizes high purification rate without increasing equipment investment, obviously reduces the concentration of the organic solvent discharged into the atmosphere, reduces environmental pollution, increases the recovery rate of the organic solvent, reduces production cost, and increases the temperature of tail gas returned to production equipment and realizes energy conservation due to the adoption of a two-stage heat exchange reverse step heat exchange mode. In particular to the tail gas treatment and the organic solvent recovery process in the production process using expensive organic solvents, such as lithium ion battery manufacturing.
It should be understood that although the present disclosure describes embodiments, not every embodiment is provided with a separate embodiment, and that this description is for clarity only, and that the skilled artisan should recognize that the embodiments may be combined as appropriate to form other embodiments that will be understood by those skilled in the art.
The above list of detailed descriptions is only specific to practical embodiments of the present invention, and they are not intended to limit the scope of the present invention, and all equivalent embodiments or modifications that do not depart from the technical core and spirit of the present invention should be included in the scope of the present invention.
Claims (11)
1. A gas concentration device comprising: an adsorption rotor;
a central shaft about which the suction rotor rotates;
The method is characterized in that: the adsorption rotor comprises an adsorption zone, a regeneration zone and a cooling zone; the adsorption zone comprises more than two sub-adsorption zones, the more than two sub-adsorption zones are sequentially communicated, and the gas to be recovered sequentially passes through the sub-adsorption zones to be subjected to multi-zone gradual purification adsorption so as to enable the tail gas to reach the emission standard; the cooling area receives external air or the gas to be recovered so as to cool the adsorption rotor; the regeneration zone carries out desorption concentration on the organic solvent adsorbed on the adsorption rotor in a heating regeneration mode; the heating regeneration mode comprises a mode of heating by a regeneration heater or a mode of directly using the external air heated after passing through a cooling zone or the gas to be recovered for heating desorption;
the flow direction of the adsorbed gas in each sub-adsorption zone is the same and is opposite to the flow direction of the regenerated air in the regeneration zone.
2. The gas concentration device of claim 1, wherein: and (3) after the air passing through the cooling zone or the gas to be recovered is heated, the air is heated again by the regeneration heater and is used as regeneration gas to be sent into the regeneration zone.
3. The gas concentration device of claim 1, wherein: the number of the sub-adsorption areas is 2, namely a first sub-adsorption area and a second sub-adsorption area, and the area of the first sub-adsorption area is larger than that of the second sub-adsorption area.
4. A gas concentrating apparatus according to claim 3 wherein: the adsorption rotor is divided into a first sub-adsorption zone, a regeneration zone, a cooling zone and a second sub-adsorption zone in turn in the rotating direction of the rotating wheel.
5. An organic solvent recovery system employing a combination of adsorption concentration and condensation for recovering an organic solvent from an organic solvent-containing tail gas discharged from a production facility, comprising: a heat exchange assembly, an organic solvent condensing recovery unit and a gas concentration unit according to any one of claims 1 to 4;
the heat exchange assembly comprises at least one heat exchanger, wherein the heat exchanger exchanges heat between high-temperature tail gas containing the organic solvent discharged from the production equipment and low-temperature tail gas returned to the production equipment after the organic solvent is recovered;
The organic solvent condensation recovery device condenses the gas from the heat exchange component and the regeneration gas concentrated by the gas concentration device to recover the organic solvent, and most of tail gas recovered by the condensation recovery device is used as the low-temperature tail gas to exchange heat with high-temperature tail gas containing the organic solvent discharged from production equipment;
and the gas concentration device is used for carrying out gradual adsorption recovery and concentration regeneration on the residual small organic solvent gas passing through the organic solvent condensation recovery device, and the residual low-temperature tail gas after adsorption is partially discharged, and part of the residual low-temperature tail gas is returned to the production device after heat exchange through the heat exchange component.
6. The organic solvent recovery system of claim 5, wherein: the heat exchange assembly comprises at least two heat exchangers, and reverse cascade heat exchange is carried out between high-temperature gas containing the organic solvent discharged from the production equipment and low-temperature tail gas returned to the production equipment after the organic solvent is recovered through at least two stages of heat exchangers.
7. The organic solvent recovery system of claim 5, wherein: the organic solvent condensation recovery device comprises at least two of a normal-temperature water cooler, a cooling water condenser, a heat pipe and a direct expansion pipe.
8. A method for concentrating an organic gas, comprising the steps of:
i) Step of purifying and adsorbing the organic gas step by step in a plurality of sub-adsorption areas of an adsorption rotor so as to enable the treated low-temperature tail gas to reach the emission standard, wherein the flowing directions of the adsorbed gas in each sub-adsorption area are the same;
ii) a step of regenerating and heating a regeneration zone of the adsorption rotor to produce regenerated concentrated organic gas, wherein the flow direction of the regenerated air in the regeneration zone is opposite to the flow direction of the adsorbed gas in each sub-adsorption zone;
iii) And cooling the adsorption rotor.
9. The organic solvent recovery and concentration method is characterized by comprising the following steps:
i) A step of heat-recovering the high-temperature tail gas containing the organic solvent discharged from the production facility;
ii) a step of condensing the tail gas after heat recovery to recover a large amount of the target organic solvent;
iii) Taking most of the condensed tail gas as low-temperature tail gas, performing heat exchange with high-temperature tail gas containing organic solvent discharged from production equipment, and returning to the production equipment; the condensed small part of tail gas is purified and adsorbed step by step in a plurality of sub-adsorption areas of an adsorption rotor so that the treated low-temperature tail gas reaches the emission standard and is discharged; the flow directions of the adsorbed gases in the sub-adsorption areas are the same, part of the exhausted low-temperature tail gas is exhausted to the outside, and the other part of the exhausted low-temperature tail gas returns to production equipment after heat exchange;
iv) carrying out regeneration heating desorption on the gas of the organic solvent adsorbed in the adsorption rotor in the multi-zone gradual purification adsorption process in a regeneration zone to generate regenerated concentrated organic solvent gas, wherein the flow direction of the regenerated air in the regeneration zone is opposite to the flow direction of the adsorbed gas in each sub-adsorption zone;
v) a step of recovering the regenerated concentrated organic solvent gas by secondary condensation.
10. The organic solvent recovery and concentration method according to claim 9, wherein: the heat recovery in step i) comprises at least a secondary heat recovery step and the heat exchange in step iii) comprises at least a secondary heat exchange step.
11. The organic solvent recovery and concentration method according to claim 9, wherein: the condensing treatment in said step ii) comprises at least a two-stage condensing treatment step.
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| CN209333523U (en) * | 2018-10-22 | 2019-09-03 | 中船动力研究院有限公司 | A kind of novel VOCs processing unit |
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| CN209333523U (en) * | 2018-10-22 | 2019-09-03 | 中船动力研究院有限公司 | A kind of novel VOCs processing unit |
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