CN220478504U - Organic gas recovery processing system is used in inositol production - Google Patents
Organic gas recovery processing system is used in inositol production Download PDFInfo
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- CN220478504U CN220478504U CN202321969978.XU CN202321969978U CN220478504U CN 220478504 U CN220478504 U CN 220478504U CN 202321969978 U CN202321969978 U CN 202321969978U CN 220478504 U CN220478504 U CN 220478504U
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- 238000011084 recovery Methods 0.000 title claims abstract description 45
- CDAISMWEOUEBRE-UHFFFAOYSA-N scyllo-inosotol Natural products OC1C(O)C(O)C(O)C(O)C1O CDAISMWEOUEBRE-UHFFFAOYSA-N 0.000 title claims abstract description 23
- SQUHHTBVTRBESD-UHFFFAOYSA-N Hexa-Ac-myo-Inositol Natural products CC(=O)OC1C(OC(C)=O)C(OC(C)=O)C(OC(C)=O)C(OC(C)=O)C1OC(C)=O SQUHHTBVTRBESD-UHFFFAOYSA-N 0.000 title claims abstract description 21
- CDAISMWEOUEBRE-GPIVLXJGSA-N inositol Chemical compound O[C@H]1[C@H](O)[C@@H](O)[C@H](O)[C@H](O)[C@@H]1O CDAISMWEOUEBRE-GPIVLXJGSA-N 0.000 title claims abstract description 21
- 229960000367 inositol Drugs 0.000 title claims abstract description 21
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 19
- 238000012545 processing Methods 0.000 title claims description 14
- 239000007788 liquid Substances 0.000 claims abstract description 72
- 238000000926 separation method Methods 0.000 claims abstract description 69
- 239000012528 membrane Substances 0.000 claims abstract description 67
- 229920005989 resin Polymers 0.000 claims description 52
- 239000011347 resin Substances 0.000 claims description 52
- 238000001179 sorption measurement Methods 0.000 claims description 49
- 239000007789 gas Substances 0.000 abstract description 148
- 239000003960 organic solvent Substances 0.000 abstract description 19
- 238000004064 recycling Methods 0.000 abstract description 10
- 238000013461 design Methods 0.000 abstract description 8
- 239000002699 waste material Substances 0.000 abstract description 4
- 239000002912 waste gas Substances 0.000 abstract description 2
- 238000000034 method Methods 0.000 description 8
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 239000003507 refrigerant Substances 0.000 description 6
- 238000002425 crystallisation Methods 0.000 description 5
- 230000008025 crystallization Effects 0.000 description 5
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- 238000003795 desorption Methods 0.000 description 4
- 229920006395 saturated elastomer Polymers 0.000 description 4
- IMQLKJBTEOYOSI-GPIVLXJGSA-N Inositol-hexakisphosphate Chemical compound OP(O)(=O)O[C@H]1[C@H](OP(O)(O)=O)[C@@H](OP(O)(O)=O)[C@H](OP(O)(O)=O)[C@H](OP(O)(O)=O)[C@@H]1OP(O)(O)=O IMQLKJBTEOYOSI-GPIVLXJGSA-N 0.000 description 2
- 239000004793 Polystyrene Substances 0.000 description 2
- 240000008042 Zea mays Species 0.000 description 2
- 235000005824 Zea mays ssp. parviglumis Nutrition 0.000 description 2
- 235000002017 Zea mays subsp mays Nutrition 0.000 description 2
- 239000006227 byproduct Substances 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 2
- 230000005494 condensation Effects 0.000 description 2
- 235000005822 corn Nutrition 0.000 description 2
- 229920002223 polystyrene Polymers 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 240000007594 Oryza sativa Species 0.000 description 1
- 235000007164 Oryza sativa Nutrition 0.000 description 1
- IMQLKJBTEOYOSI-UHFFFAOYSA-N Phytic acid Natural products OP(O)(=O)OC1C(OP(O)(O)=O)C(OP(O)(O)=O)C(OP(O)(O)=O)C(OP(O)(O)=O)C1OP(O)(O)=O IMQLKJBTEOYOSI-UHFFFAOYSA-N 0.000 description 1
- 229930003270 Vitamin B Natural products 0.000 description 1
- 230000000712 assembly Effects 0.000 description 1
- 238000000429 assembly Methods 0.000 description 1
- 230000009286 beneficial effect Effects 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
- 239000002537 cosmetic Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 235000002949 phytic acid Nutrition 0.000 description 1
- 229940068041 phytic acid Drugs 0.000 description 1
- 239000000467 phytic acid Substances 0.000 description 1
- 239000002861 polymer material Substances 0.000 description 1
- 239000002952 polymeric resin Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 235000009566 rice Nutrition 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 235000019156 vitamin B Nutrition 0.000 description 1
- 239000011720 vitamin B Substances 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Gases By Adsorption (AREA)
Abstract
The utility model relates to the technical field of waste gas treatment, in particular to an organic gas recovery treatment system for inositol production, which comprises a first condenser and a second condenser which are communicated with an organic gas pipeline, wherein an uncondensed gas outlet of the second condenser is communicated with a gas compressor, an exhaust port of the gas compressor is communicated with a first gas-liquid separator, an exhaust port of the first gas-liquid separator is communicated with a first heat exchanger, an uncondensed gas outlet of the first heat exchanger is communicated with a second gas-liquid separator, and liquid outlets of the first gas-liquid separator and the second gas-liquid separator are respectively communicated with a second recovery tank; the exhaust port of the second gas-liquid separator is communicated with the second heat exchanger, and the non-condensable gas outlet of the second heat exchanger is communicated with the membrane separation assembly. The recycling system is reasonable in design, and the recycled liquid organic solvent is high in purity and can be directly utilized, so that the recycling efficiency is improved, and the resource waste is avoided.
Description
Technical Field
The utility model relates to the technical field of waste gas treatment, in particular to a recovery treatment system for organic gas for inositol production.
Background
Inositol, also known as inositol, belongs to vitamin B and is an important chemical product. Is widely applied to the fields of food industry, medicine industry, feed industry, cosmetics industry and the like. At present, the main raw materials of inositol production in China are byproducts generated in the agricultural product processing process, such as corn steep water, rice bran steep water and the like, and phytic acid contained in the corn steep water is extracted in a phytate form and then subjected to procedures of hydrolysis, separation, concentration, crystallization and the like to prepare inositol and byproducts. In the process of inositol crystallization, methanol or ethanol is required to be added, methanol or ethanol volatilizes in the crystallization process, and the organic gas is absorbed by adopting a spray tower at present, but the treatment effect is poor, and the concentration of the treated organic solvent is low and can not be directly used. Therefore, in view of the above problems, it is necessary to develop an organic gas recovery processing system for inositol production.
Disclosure of Invention
The technical problems to be solved by the utility model are as follows: aiming at the defects of the prior art, the organic gas recycling system for inositol production is provided, and the organic gas can be recycled by using the recycling system, so that the resource waste is avoided, and the pollution to the environment is reduced.
In order to solve the technical problems, the technical scheme of the utility model is as follows:
an organic gas recovery processing system for inositol production comprises a first condenser communicated with an organic gas pipeline, wherein an uncondensed gas outlet of the first condenser is communicated with a second condenser, and condensate outlets of the first condenser and the second condenser are respectively communicated with a first recovery tank; the non-condensable gas outlet of the second condenser is communicated with a gas compressor, the gas outlet of the gas compressor is communicated with a first gas-liquid separator, the gas outlet of the first gas-liquid separator is communicated with a first heat exchanger, the non-condensable gas outlet of the first heat exchanger is communicated with a second gas-liquid separator, and the liquid outlets of the first gas-liquid separator and the second gas-liquid separator are respectively communicated with a second recovery tank; the exhaust port of the second gas-liquid separator is communicated with the second heat exchanger, the non-condensable gas outlet of the second heat exchanger is communicated with the membrane separation assembly, the first exhaust port of the membrane separation assembly is communicated with the resin adsorption tank, the exhaust port of the resin adsorption tank is communicated with the buffer tank, and the second exhaust port of the membrane separation assembly is communicated with the gas compressor.
As an improved technical scheme, the non-condensable gas outlet of the second condenser is communicated with an air bag through a pipeline, and a pressure transmitter is arranged on the air bag.
As an improved technical scheme, the exhaust port of the second recovery tank is communicated with the air inlet of the first heat exchanger.
As an improved technical scheme, the exhaust port of the buffer tank is communicated with the gas compressor, and the gas compressor comprises a first gas compressor and a second gas compressor.
As an improved technical scheme, the membrane separation assembly comprises a first membrane separation assembly, a second membrane separation assembly and a third membrane separation assembly which are connected in parallel, and second exhaust ports of the first membrane separation assembly, the second membrane separation assembly and the third membrane separation assembly are communicated with the gas compressor through an induced draft fan.
As an improved technical scheme, the resin adsorption tank comprises a first resin adsorption tank and a second resin adsorption tank which are connected in parallel, wherein the tops of the first resin adsorption tank and the second resin adsorption tank are respectively communicated with a steam pipeline, and the bottom exhaust ports of the first resin adsorption tank and the second resin adsorption tank are respectively communicated with the gas compressor through pipelines.
After the technical scheme is adopted, the utility model has the beneficial effects that:
because the organic gas recovery processing system for inositol production comprises a first condenser communicated with an organic gas pipeline, an uncondensed gas outlet of the first condenser is communicated with a second condenser, and condensate outlets of the first condenser and the second condenser are respectively communicated with a first recovery tank; the non-condensable gas outlet of the second condenser is communicated with the gas compressor, the gas outlet of the gas compressor is communicated with the first gas-liquid separator, the gas outlet of the first gas-liquid separator is communicated with the first heat exchanger, the non-condensable gas outlet of the first heat exchanger is communicated with the second gas-liquid separator, and the liquid outlets of the first gas-liquid separator and the second gas-liquid separator are respectively communicated with the second recovery tank; the exhaust port of the second gas-liquid separator is communicated with the second heat exchanger, the non-condensable gas outlet of the second heat exchanger is communicated with the membrane separation assembly, the first exhaust port of the membrane separation assembly is communicated with the resin adsorption tank, the exhaust port of the resin adsorption tank is communicated with the buffer tank, and the second exhaust port of the membrane separation assembly is communicated with the gas compressor. In actual production, organic gas generated in an inositol crystallization process enters a first condenser through an organic gas pipeline, after being cooled by a refrigerant of the first condenser, a part of liquid organic solvent enters a first recovery tank, and uncondensed organic gas enters the second condenser and is cooled by the refrigerant, and then a part of liquid organic solvent enters the first recovery tank; the uncondensed organic gas enters the gas compressor, compressed organic gas enters the first gas-liquid separator, the organic gas enters the first heat exchanger, and the liquid organic solvent in the first gas-liquid separator enter the second recovery tank along a pipeline after heat exchange; the uncondensed organic gas in the first heat exchanger enters the second gas-liquid separator, the liquid organic solvent also enters the second recovery tank along the pipeline, the gas in the second gas-liquid separator enters the second heat exchanger along the pipeline, the uncondensed gas enters the membrane separation assembly after heat exchange, part of the uncondensed gas and a small amount of organic gas pass through an inorganic membrane tube of the membrane separation assembly, enter the resin adsorption tank along a first gas outlet, are absorbed by the resin and then are introduced into steam for desorption, and the desorbed organic solvent gas enters the buffer tank and then enters the gas compressor along the pipeline for separation by the gas-liquid separator and condensation by the heat exchanger; and (3) organic gas which does not enter the inorganic membrane tube in the membrane separation assembly also enters the gas compressor through a pipeline, is compressed and then is separated by the gas-liquid separator and condensed by the heat exchanger, and finally, the condensed liquid organic solvent is recovered through the second recovery tank. The recycling system is reasonable in design, and the recycled liquid organic solvent is high in purity and can be directly utilized, so that the recycling efficiency is improved, and the resource waste is avoided.
Because the uncondensed gas outlet of the second condenser is communicated with the air bag through a pipeline, a pressure transmitter is arranged on the air bag. By arranging the air bags, the fluctuation of the organic gas can be effectively buffered, so that the air flow entering the gas compressor is more stable.
Because the exhaust port of the second recovery tank is communicated with the air inlet of the first heat exchanger. After the organic gas in the second recovery tank enters the first heat exchanger along the pipeline and is condensed by the refrigerant, the liquid organic solvent enters the second gas-liquid separator, and finally enters the second recovery tank through the pipeline. In this design, the non-condensed organic gas is further condensed and recovered.
Since the exhaust port of the buffer tank is communicated with the gas compressor, the gas compressor comprises a first gas compressor and a second gas compressor. After being discharged from the upper exhaust port, the organic gas in the buffer tank enters the first gas compressor and the second gas compressor along the pipeline, and enters the gas-liquid separator again for separation after being compressed. The design is reasonable, and the non-condensable organic gas is further recovered.
The membrane separation assembly comprises a first membrane separation assembly, a second membrane separation assembly and a third membrane separation assembly which are connected in parallel, and a second exhaust port of the first membrane separation assembly, the second membrane separation assembly and the third membrane separation assembly is communicated with the gas compressor through an induced draft fan. The uncondensed gas discharged by the second heat exchanger respectively enters the first membrane separation assembly, the second membrane separation assembly and the third membrane separation assembly, the uncondensed gas and a small amount of organic gas pass through the inorganic membrane tube to be discharged from the first exhaust port, and most of the organic gas is discharged through the second exhaust port, enters the gas compressor under the action of the induced draft fan, and enters the gas-liquid separator again for separation after being compressed. The organic gas recycling device is reasonable in design and is used for recycling organic gas.
Because the resin adsorption tank comprises a first resin adsorption tank and a second resin adsorption tank which are connected in parallel, the tops of the first resin adsorption tank and the second resin adsorption tank are respectively communicated with the steam pipeline, and the bottom exhaust ports of the first resin adsorption tank and the second resin adsorption tank are respectively communicated with the gas compressor through the pipelines. The method comprises the steps that uncondensed gas and a small amount of organic gas discharged from a first exhaust port of a first membrane separation assembly, a second membrane separation assembly and a third membrane separation assembly firstly enter a first resin adsorption tank, the organic gas adsorbed in the first resin adsorption tank is desorbed by adopting steam after being adsorbed and saturated by macroporous polystyrene type polymer material resin, meanwhile, the organic gas is adsorbed by adopting a second resin adsorption tank, and then the desorbed organic gas and water vapor enter a buffer tank along a pipeline after being adsorbed and saturated. The resin adsorption tank is reasonable in design, can adsorb organic gas, and is compressed again through the gas compressor after desorption, and separation is carried out by adopting the gas-liquid separator, so that the organic gas is fully recovered.
Drawings
FIG. 1 is a schematic diagram of an organic gas recovery processing system for inositol production according to the present utility model;
wherein, 1-first condenser, 2-second condenser, 3-first recovery tank, 4-gas compressor, 40-first gas compressor, 41-second gas compressor, 5-first gas-liquid separator, 6-first heat exchanger, 7-second gas-liquid separator, 8-second recovery tank, 9-second heat exchanger, 10-membrane separation assembly, 100-first membrane separation assembly, 101-second membrane separation assembly, 102-third membrane separation assembly, 11-resin adsorption tank, 110-first resin adsorption tank, 111-second resin adsorption tank, 12-buffer tank, 13-gasbag, 130-pressure transmitter.
Detailed Description
The present utility model will be described in further detail with reference to the drawings and examples, in order to make the objects, technical solutions and advantages of the present utility model more apparent. It should be understood that the specific embodiments described herein are for purposes of illustration only and are not intended to limit the scope of the utility model.
An organic gas recovery processing system for inositol production comprises a first condenser 1 communicated with an organic gas pipeline, wherein an uncondensed gas outlet of the first condenser 1 is communicated with a second condenser 2, and condensate outlets of the first condenser 1 and the second condenser 2 are respectively communicated with a first recovery tank 3; the non-condensable gas outlet of the second condenser 2 is communicated with the gas compressor 4, the gas outlet of the gas compressor 4 is communicated with the first gas-liquid separator 5, the gas outlet of the first gas-liquid separator 5 is communicated with the first heat exchanger 6, the non-condensable gas outlet of the first heat exchanger 6 is communicated with the second gas-liquid separator 7, and the liquid outlets of the first gas-liquid separator 5 and the second gas-liquid separator 7 are respectively communicated with the second recovery tank 8; the exhaust port of the second gas-liquid separator 7 is communicated with the second heat exchanger 9, the non-condensable gas outlet of the second heat exchanger 9 is communicated with the membrane separation assembly 10, the first exhaust port of the membrane separation assembly 10 is communicated with the resin adsorption tank 11, the exhaust port of the resin adsorption tank 11 is communicated with the buffer tank 12, and the second exhaust port of the membrane separation assembly 10 is communicated with the gas compressor 4.
In actual production, organic gas generated in an inositol crystallization process enters a first condenser through an organic gas pipeline, after being cooled by a refrigerant of the first condenser, a part of liquid organic solvent enters a first recovery tank, and uncondensed organic gas enters the second condenser and is cooled by the refrigerant, and then a part of liquid organic solvent enters the first recovery tank; the uncondensed organic gas enters the gas compressor, compressed organic gas enters the first gas-liquid separator, the organic gas enters the first heat exchanger, and the liquid organic solvent in the first gas-liquid separator enter the second recovery tank along a pipeline after heat exchange; the method comprises the steps that uncondensed organic gas in a first heat exchanger enters the second gas-liquid separator, liquid organic solvent also enters the second recovery tank along a pipeline, gas in the second gas-liquid separator enters the second heat exchanger along the pipeline, the condensed organic solvent enters the second recovery tank, the uncondensed organic gas enters the membrane separation assembly, the uncondensed gas and a small amount of organic gas pass through an inorganic membrane tube in the membrane separation assembly, enter the resin adsorption tank along a first gas outlet, adsorb the organic gas through the resin, then introduce steam for desorption, the desorbed organic solvent gas enters the buffer tank, and then enters the gas compressor along the pipeline for separation by the gas-liquid separator and condensation by the heat exchanger; and (3) organic gas which does not enter the inorganic membrane tube in the membrane separation assembly also enters the gas compressor through a pipeline, is compressed and then is separated by the gas-liquid separator and condensed by the heat exchanger, and finally, the condensed liquid organic solvent is recovered through the second recovery tank. The recycling system is reasonable in design, and the recycled liquid organic solvent is high in purity and can be directly utilized, so that the recycling efficiency is improved, and the resource waste is avoided.
The non-condensable gas outlet of the second condenser 2 is communicated with the air bag 13 through a pipeline, and a pressure transmitter 130 is arranged on the air bag 13 and is electrically connected with a controller. By arranging the air bags, the fluctuation of the organic gas can be effectively buffered, so that the air flow entering the gas compressor is more stable; when the data detected by the air transmitter reaches a certain value, the controller starts the air compressor to operate.
Wherein the exhaust port of the second recovery tank 8 communicates with the inlet port of the first heat exchanger 6. After the organic gas in the second recovery tank enters the first heat exchanger along the pipeline and is condensed by the refrigerant, the liquid organic solvent enters the second gas-liquid separator, and finally enters the second recovery tank through the pipeline.
Wherein the exhaust port of the buffer tank 12 is in communication with the gas compressor 4, the gas compressor 4 comprising a first gas compressor 40 and a second gas compressor 41. After being discharged from the upper exhaust port, the organic gas in the buffer tank enters the first gas compressor and the second gas compressor along the pipeline, and enters the gas-liquid separator again for separation after being compressed.
Wherein the membrane separation assembly 10 (purchased from a manufacturer, comprising a housing, wherein one end of the housing is provided with an air inlet and a second air outlet, the interior of the housing is provided with a plurality of ceramic tubes, the outer wall of each ceramic tube is provided with an inorganic material coating, the other end of the housing is provided with a first air outlet) comprises a first membrane separation assembly 100, a second membrane separation assembly 101 and a third membrane separation assembly 102 which are connected in parallel, and the second air outlets of the first membrane separation assembly, the second membrane separation assembly and the third membrane separation assembly are communicated with a gas compressor through an induced draft fan. The uncondensed gas discharged by the second heat exchanger respectively enters the first membrane separation assembly, the second membrane separation assembly and the third membrane separation assembly, the uncondensed gas and a small part of organic gas pass through the inorganic membrane tube to be discharged from the first exhaust port, and most of organic gas and solvent molecules are discharged through the second exhaust port, enter the gas compressor under the action of the induced draft fan, and enter the gas-liquid separator again to be separated after being compressed.
Wherein the resin adsorption tank 11 comprises a first resin adsorption tank 110 and a second resin adsorption tank 111 which are connected in parallel, the tops of the first resin adsorption tank 110 and the second resin adsorption tank 111 are respectively communicated with a steam pipeline, and the bottom exhaust ports of the first resin adsorption tank 110 and the second resin adsorption tank 111 are respectively communicated with the gas compressor 4 through pipelines. Organic gas discharged from a first exhaust port of the first, second and third membrane separation assemblies firstly enters a first resin adsorption tank, the organic gas adsorbed in the first resin adsorption tank is desorbed by adopting steam after being adsorbed and saturated by macroporous polystyrene type polymer resin, meanwhile, the organic gas is adsorbed by adopting a second resin adsorption tank, the organic gas is desorbed by utilizing steam after being adsorbed and saturated, and the desorbed organic gas and water vapor enter a buffer tank along a pipeline. The resin adsorption tank is reasonable in design, can adsorb organic gas, and is compressed again through the gas compressor after desorption, and separation is carried out by adopting the gas-liquid separator, so that the organic gas is fully recovered.
The foregoing description of the preferred embodiments of the utility model is not intended to be limiting, but rather is intended to cover all modifications, equivalents, and alternatives falling within the spirit and principles of the utility model.
Claims (6)
1. An organic gas recovery processing system for inositol production, which is characterized in that: the device comprises a first condenser which is communicated with an organic gas pipeline, wherein an uncondensed gas outlet of the first condenser is communicated with a second condenser, and condensate outlets of the first condenser and the second condenser are respectively communicated with a first recovery tank; the non-condensable gas outlet of the second condenser is communicated with a gas compressor, the gas outlet of the gas compressor is communicated with a first gas-liquid separator, the gas outlet of the first gas-liquid separator is communicated with a first heat exchanger, the non-condensable gas outlet of the first heat exchanger is communicated with a second gas-liquid separator, and the liquid outlets of the first gas-liquid separator and the second gas-liquid separator are respectively communicated with a second recovery tank; the exhaust port of the second gas-liquid separator is communicated with the second heat exchanger, the non-condensable gas outlet of the second heat exchanger is communicated with the membrane separation assembly, the first exhaust port of the membrane separation assembly is communicated with the resin adsorption tank, the exhaust port of the resin adsorption tank is communicated with the buffer tank, and the second exhaust port of the membrane separation assembly is communicated with the gas compressor.
2. The organic gas recovery processing system for inositol production according to claim 1, wherein: the non-condensable gas outlet of the second condenser is communicated with an air bag through a pipeline, and a pressure transmitter is arranged on the air bag.
3. The organic gas recovery processing system for inositol production according to claim 1, wherein: and the exhaust port of the second recovery tank is communicated with the air inlet of the first heat exchanger.
4. The organic gas recovery processing system for inositol production according to claim 1, wherein: the gas compressor is communicated with the gas exhaust port of the buffer tank, and comprises a first gas compressor and a second gas compressor.
5. The organic gas recovery processing system for inositol production according to claim 1, wherein: the membrane separation assembly comprises a first membrane separation assembly, a second membrane separation assembly and a third membrane separation assembly which are connected in parallel, and second exhaust ports of the first membrane separation assembly, the second membrane separation assembly and the third membrane separation assembly are communicated with the gas compressor through an induced draft fan.
6. The organic gas recovery processing system for inositol production according to claim 1, wherein: the resin adsorption tanks comprise a first resin adsorption tank and a second resin adsorption tank which are connected in parallel, the tops of the first resin adsorption tank and the second resin adsorption tank are respectively communicated with a steam pipeline, and bottom exhaust ports of the first resin adsorption tank and the second resin adsorption tank are respectively communicated with the gas compressor through pipelines.
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| Application Number | Priority Date | Filing Date | Title |
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| CN202321969978.XU CN220478504U (en) | 2023-07-25 | 2023-07-25 | Organic gas recovery processing system is used in inositol production |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321969978.XU CN220478504U (en) | 2023-07-25 | 2023-07-25 | Organic gas recovery processing system is used in inositol production |
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| CN220478504U true CN220478504U (en) | 2024-02-13 |
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| CN202321969978.XU Active CN220478504U (en) | 2023-07-25 | 2023-07-25 | Organic gas recovery processing system is used in inositol production |
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| Country | Link |
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2023
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