CN219807872U - Heparin sodium wastewater recovery treatment system - Google Patents
Heparin sodium wastewater recovery treatment system Download PDFInfo
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- CN219807872U CN219807872U CN202321326498.1U CN202321326498U CN219807872U CN 219807872 U CN219807872 U CN 219807872U CN 202321326498 U CN202321326498 U CN 202321326498U CN 219807872 U CN219807872 U CN 219807872U
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- heparin sodium
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- anaerobic
- flocculation
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- 239000002351 wastewater Substances 0.000 title claims abstract description 45
- 229920000669 heparin Polymers 0.000 title claims abstract description 28
- ZFGMDIBRIDKWMY-PASTXAENSA-N heparin Chemical compound CC(O)=N[C@@H]1[C@@H](O)[C@H](O)[C@@H](COS(O)(=O)=O)O[C@@H]1O[C@@H]1[C@@H](C(O)=O)O[C@@H](O[C@H]2[C@@H]([C@@H](OS(O)(=O)=O)[C@@H](O[C@@H]3[C@@H](OC(O)[C@H](OS(O)(=O)=O)[C@H]3O)C(O)=O)O[C@@H]2O)CS(O)(=O)=O)[C@H](O)[C@H]1O ZFGMDIBRIDKWMY-PASTXAENSA-N 0.000 title claims abstract description 28
- 229960001008 heparin sodium Drugs 0.000 title claims abstract description 28
- 238000011084 recovery Methods 0.000 title claims abstract description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 40
- 239000012528 membrane Substances 0.000 claims abstract description 37
- 238000005189 flocculation Methods 0.000 claims abstract description 34
- 230000016615 flocculation Effects 0.000 claims abstract description 34
- 239000007788 liquid Substances 0.000 claims abstract description 24
- 238000000926 separation method Methods 0.000 claims abstract description 20
- 238000006243 chemical reaction Methods 0.000 claims abstract description 16
- 238000001704 evaporation Methods 0.000 claims abstract description 12
- 230000008020 evaporation Effects 0.000 claims abstract description 12
- 235000019750 Crude protein Nutrition 0.000 claims abstract description 7
- 238000004064 recycling Methods 0.000 claims description 11
- 238000011045 prefiltration Methods 0.000 claims description 8
- 150000003839 salts Chemical class 0.000 claims description 8
- 238000007790 scraping Methods 0.000 claims description 8
- 238000003756 stirring Methods 0.000 claims description 8
- 239000002893 slag Substances 0.000 claims description 7
- 229920001661 Chitosan Polymers 0.000 claims description 6
- 239000000463 material Substances 0.000 claims description 6
- 239000006004 Quartz sand Substances 0.000 claims description 3
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 3
- 239000000835 fiber Substances 0.000 claims description 3
- 239000000446 fuel Substances 0.000 claims description 3
- 238000010438 heat treatment Methods 0.000 claims description 3
- 239000010802 sludge Substances 0.000 claims description 3
- 239000007787 solid Substances 0.000 claims description 3
- 238000000034 method Methods 0.000 abstract description 10
- 102000004169 proteins and genes Human genes 0.000 abstract description 10
- 108090000623 proteins and genes Proteins 0.000 abstract description 10
- 230000008569 process Effects 0.000 abstract description 7
- 210000004379 membrane Anatomy 0.000 description 27
- 238000004065 wastewater treatment Methods 0.000 description 6
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 238000001914 filtration Methods 0.000 description 3
- 230000004048 modification Effects 0.000 description 3
- 238000012986 modification Methods 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- 230000015556 catabolic process Effects 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 229920002683 Glycosaminoglycan Polymers 0.000 description 1
- QAOWNCQODCNURD-UHFFFAOYSA-L Sulfate Chemical compound [O-]S([O-])(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-L 0.000 description 1
- 230000003110 anti-inflammatory effect Effects 0.000 description 1
- 239000003146 anticoagulant agent Substances 0.000 description 1
- 229940127219 anticoagulant drug Drugs 0.000 description 1
- 230000010100 anticoagulation Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000008827 biological function Effects 0.000 description 1
- 239000008280 blood Substances 0.000 description 1
- 210000004369 blood Anatomy 0.000 description 1
- 238000005119 centrifugation Methods 0.000 description 1
- 239000012141 concentrate Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000018044 dehydration Effects 0.000 description 1
- 238000006297 dehydration reaction Methods 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000011152 fibreglass Substances 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 229920002521 macromolecule Polymers 0.000 description 1
- 238000005374 membrane filtration Methods 0.000 description 1
- 239000012452 mother liquor Substances 0.000 description 1
- 239000010413 mother solution Substances 0.000 description 1
- 210000004400 mucous membrane Anatomy 0.000 description 1
- 235000015277 pork Nutrition 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 239000013535 sea water Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 210000004927 skin cell Anatomy 0.000 description 1
- 210000000813 small intestine Anatomy 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
Abstract
The utility model discloses a heparin sodium wastewater recovery treatment system, which comprises a collecting tank, a flocculation air floatation tank, an anaerobic tank, a DTRO membrane assembly and a multi-effect evaporator which are connected in sequence through pipelines; the flocculation air floatation tank comprises a flocculation reaction area, a dissolved air release area, a solid-liquid separation area and a scum collecting tank; the dross collecting tank is connected to a centrifuge and a dryer in sequence through a dross delivery pipe, thereby separating out crude protein. The treatment system can effectively recover protein, treat wastewater by adopting an anaerobic process, recycle biogas by reducing organic matters in the wastewater, lighten the pollution of the wastewater to a membrane system, and reduce the evaporation capacity of concentrated water of the membrane system by adopting a DTRO membrane with higher recovery rate and strong anti-pollution capability.
Description
Technical Field
The utility model belongs to the field of wastewater treatment equipment, and particularly relates to a heparin sodium wastewater recovery treatment system.
Background
Heparin sodium is a mucopolysaccharide sulfate anticoagulant, has the functions of anticoagulation, blood fat reduction, pork skin cell protection, anti-inflammatory and the like, and has wide biological functions and medicinal values. The crude heparin sodium is usually extracted from the mucous membrane of the small intestine of a pig or a cow, and a large amount of high-protein, high-salt and high-organic wastewater is generated in the extraction process, and if the wastewater is directly treated conventionally, the wastewater not only causes great pressure on a sewage treatment system, but also wastes resources and energy.
The utility model patent CN 111573945A discloses a system and a method for recycling heparin sodium wastewater, which adopts a multi-stage membrane to separate and treat the heparin sodium wastewater and recover protein and salt in the wastewater. However, since raw water contains a large amount of macromolecular substances such as proteins, the membranes of each stage are still easily blocked only by simple pretreatment; the salinity in the raw water is as high as 30000-40000 mg/L, the recovery rate of the adopted seawater desalination membrane is low (30-45%), the concentrated water amount is large, and the energy consumption of an evaporation system is high; a large amount of organic matters in raw water are not degraded, concentrated in concentrated water and enter an evaporation system, so that evaporation efficiency is affected, and a large amount of concentrated mother solution is generated.
Disclosure of Invention
The utility model aims to: aiming at the defects of the prior art, the utility model provides a heparin sodium wastewater recovery treatment system capable of effectively recovering protein and reducing organic matters in wastewater.
In order to achieve the above purpose, the technical scheme adopted by the utility model is as follows:
a heparin sodium wastewater recovery treatment system comprises a collecting tank, a flocculation air floatation tank, an anaerobic tank, a DTRO membrane assembly and a multi-effect evaporator which are connected in sequence through pipelines; the flocculation air floatation tank comprises a flocculation reaction area, a dissolved air release area, a solid-liquid separation area and a scum collecting tank; the dross collecting tank is connected to a centrifuge and a dryer in sequence through a dross delivery pipe, thereby separating out crude protein.
Further, a three-phase separator is arranged at the top of the anaerobic tank; the three-phase separator is connected to the biogas boiler through a biogas conveying pipe and provides heating fuel for the biogas boiler; the biogas boiler respectively sends the generated high-temperature steam into the dryer and the multi-effect evaporator through the steam conveying pipe.
Further, in the flocculation floatation tank, a flocculation reaction area, a dissolved gas release area and a solid-liquid separation area are respectively separated by a baffle plate; a communicating groove is formed at the bottom of the baffle plate between the flocculation reaction area and the dissolved gas release area; and overflow grooves are arranged at the bottoms of the baffle plates between the dissolved gas release area and the solid-liquid separation area.
Further, a stirring device and a chitosan feeding pipeline are arranged in the flocculation reaction zone.
Further, the tops of the dissolved gas release area and the solid-liquid separation area are provided with slag scrapers, and scum at the tops of the dissolved gas release area and the solid-liquid separation area is scraped into a scum collecting tank through a scraping plate of the slag scrapers.
Further, a tank top pulse water distributor is arranged above the anaerobic tank, and a tank bottom hydraulic distributor is arranged at the bottom of the anaerobic tank; the inlet end of the tank top pulse water distributor is connected with the water outlet of the flocculation air floatation tank, the outlet end of the tank top pulse water distributor is connected with the tank bottom hydraulic distributor through a central pipe, and wastewater is sprayed out at a high speed through the tank bottom hydraulic distributor, so that intermittent stirring of anaerobic sludge at the tank bottom is realized.
Further, the top of the anaerobic tank is sealed by a tank top plate, the three-phase separator is arranged in a biogas storage space between the tank top and the liquid level, and anaerobic effluent is discharged by a porous water collecting pipe and is sent to a subsequent component for treatment.
Further, the rear end of the anaerobic tank is also provided with an intermediate tank for temporarily storing effluent, and the effluent is sent to a DTRO membrane assembly for further separation.
Further, a prefilter is arranged between the middle tank and the DTRO membrane assembly; the prefilter consists of a multi-medium filter and a bag filter; wherein, the lower part of the multi-medium filter adopts quartz sand filter materials, and the upper part adopts fiber ball filter materials.
Further, in the DTRO membrane assembly, the DTRO membrane adopts a convex membrane, so that the feed liquid is in a turbulent flow state when flowing; the separated clean water is discharged through the outer discharge pipe up to standard, and the concentrated water is sent into the multi-effect evaporator for evaporation treatment and solid salt is produced.
The beneficial effects are that:
the treatment system can effectively recover protein, treat wastewater by adopting an anaerobic process, recycle biogas by reducing organic matters in the wastewater, lighten the pollution of the wastewater to a membrane system, and reduce the evaporation capacity of concentrated water of the membrane system by adopting a DTRO membrane with higher recovery rate and strong anti-pollution capability. According to the characteristics of heparin sodium wastewater, the system simultaneously recovers protein, methane, salt and water resources in the wastewater treatment process, reduces pollutant discharge, reduces the wastewater treatment operation cost, and has good social and economic benefits.
Drawings
The foregoing and/or other advantages of the utility model will become more apparent from the following detailed description of the utility model when taken in conjunction with the accompanying drawings and detailed description.
Fig. 1 is a schematic diagram of the overall structure of the heparin sodium wastewater recovery treatment system.
Fig. 2 is a process flow diagram of the system for treating heparin sodium wastewater.
Wherein each reference numeral represents:
10, collecting a pool; 20 flocculation floatation tanks; 201 flocculation reaction zone; 202 a dissolved gas release zone; 203 a solid-liquid separation zone; 204 a dross collection tank; 205 dross feed pipe; 206 stirring means; 207 chitosan feeding line; 208 slag scraping machine; 30 anaerobic tanks; 301 three-phase separator; 302 biogas delivery pipes; 303 pool top pulse water distributor; 304 pool bottom hydraulic distributor; 40DTRO membrane modules; a 50 multiple effect evaporator; 60 centrifuges; a 70 dryer; 80 biogas boiler; 801 steam delivery pipe; 90 middle pool; 100 prefilter devices; 110 multi-media filter; 120 bag filter.
Detailed Description
The utility model will be better understood from the following examples.
The structures, proportions, sizes, etc. shown in the drawings are shown only in connection with the disclosure of the present utility model, and are not intended to limit the scope of the utility model, which is defined by the claims, but rather by the terms of modification, variation of proportions, or adjustment of sizes, without affecting the efficacy or achievement of the present utility model, should be understood as falling within the scope of the present utility model. Also, the terms such as "upper", "lower", "front", "rear", "middle", and the like are used herein for descriptive purposes only and are not intended to limit the scope of the utility model for which the utility model may be practiced or for which the relative relationships may be altered or modified without materially altering the technical context.
As shown in fig. 1, the heparin sodium wastewater recovery treatment system of the present utility model comprises a collecting tank 10, a flocculation air floatation tank 20, an anaerobic tank 30, an intermediate tank 90, a prefilter 100, a DTRO membrane module 40 and a multi-effect evaporator 50 which are connected in sequence by pipelines.
Wherein the flocculation air floatation tank 20 comprises a flocculation reaction area 201, a dissolved air release area 202, a solid-liquid separation area 203 and a scum collecting tank 204; the dross collection groove 204 is connected to the centrifuge 60 and the dryer 70 in sequence through a dross delivery pipe 205, thereby separating out crude protein.
The top of the anaerobic tank 30 is provided with a three-phase separator 301; the three-phase separator 301 is connected to the biogas boiler 80 through a biogas conveying pipe 302 to provide heating fuel for the biogas boiler 80; the biogas boiler 80 sends the generated high temperature steam to the dryer 70 and the multi-effect evaporator 50 through a steam delivery pipe 801 for protein drying and DTRO concentrate evaporation, respectively.
In the flocculation air floatation tank 20, a flocculation reaction area 201, a dissolved air release area 202 and a solid-liquid separation area 203 are respectively separated by baffles; a communicating groove is formed at the bottom of the baffle plate between the flocculation reaction area 201 and the dissolved gas release area 202; an overflow groove is arranged at the bottom of the baffle plate between the dissolved gas release area 202 and the solid-liquid separation area 203.
A stirring device 206 and a chitosan feeding line 207 are arranged in the flocculation reaction zone 201. The chitosan is added into the flocculation reaction area at the concentration of 300-1000 mg/L, and the stirring time of the flocculation reaction area is 30-60 min.
The top of the dissolved gas releasing area 202 and the top of the solid-liquid separation area 203 are provided with a slag scraping machine 208, and the scum at the top of the dissolved gas releasing area 202 and the top of the solid-liquid separation area 203 is scraped into a scum collecting tank 204 by a scraping plate of the slag scraping machine 208. The dross collection groove 204 is configured as a V-groove with a sidewall slope greater than 60 degrees to facilitate dross slip. The collected scum is pumped to a centrifugal machine 60 for dehydration, the rotating speed of the centrifugal machine 60 is not lower than 4000r/min, and the scum is dried by a dryer 70 to obtain crude protein.
A tank top pulse water distributor 303 is arranged above the anaerobic tank 30, and a tank bottom hydraulic distributor 304 is arranged at the bottom of the anaerobic tank 30; the inlet end of the tank top pulse water distributor 303 is connected with the water outlet of the flocculation air floatation tank 20, the outlet end of the tank top pulse water distributor 303 is connected with the tank bottom hydraulic distributor 304 through a central pipe, and wastewater is sprayed out at high speed through the tank bottom hydraulic distributor 304, so that intermittent stirring of anaerobic sludge at the tank bottom is realized. Adopting an anaerobic process to treat raw water, reducing COD of effluent to below 1000mg/L, reducing pollution of wastewater to a subsequent membrane system, remarkably reducing the production of concentrated mother liquor of an evaporation system and reducing overall operation cost through degradation of pollutants in wastewater; and simultaneously, the biogas generated by the anaerobic degradation of the organic matters in the wastewater is recycled.
The top of the anaerobic tank 30 is sealed by a tank top plate, the three-phase separator 301 is arranged in a biogas storage space between the tank top and the liquid level, and anaerobic effluent is discharged by a porous water collecting pipe and sent to a subsequent component for treatment.
The rear end of the anaerobic tank 30 is also provided with an intermediate tank 90 for temporarily storing effluent, and the effluent of the anaerobic tank 30 is naturally settled and then sent to the DTRO membrane assembly 40 for further separation.
A prefilter device 100 is also arranged between the intermediate tank 90 and the DTRO membrane assembly 40; the prefilter 100 consists of a glass fiber reinforced plastic multi-media filter 110 and a 5 μm bag filter 120; wherein, the lower part of the multi-medium filter 110 adopts quartz sand filter material, and the thickness of the filter layer is 80-100 cm; the upper part adopts a fiber ball filter material, the thickness of a filter layer is 80-100 m, the filtering speed of the multi-medium filter 110 is 10-15 m/h, and the filtering precision of the bag filter 120 is 5 mu m.
In the DTRO membrane assembly 40, a convex membrane is adopted as a DTRO membrane, and the aperture is 0.1-0.4 nm, so that the feed liquid is in a turbulent flow state when flowing; the separated clean water is discharged through the outer discharge pipe to reach the standard, and the concentrated water is sent into the multi-effect evaporator 50 for evaporation treatment and solid salt generation. The DTRO membrane is adopted to separate heparin sodium wastewater, the highest working pressure of the inlet water of the DTRO membrane reaches 120bar, the water yield of the wastewater with the salt content of 30000-40000 mg/L can reach 50% -70%, and the DTRO membrane adopts a convex design, so that the feed liquid is in a turbulent state when flowing, and the anti-pollution capability of a membrane element is improved.
Referring to fig. 2, the heparin sodium wastewater treatment process of the utility model comprises the following steps:
(1) Lifting the wastewater to a flocculation air floatation tank 20, adding chitosan (300-1000 mg/L) for adsorption flocculation, allowing flocculation reaction time to be 30-60 min, allowing the effluent to enter an air floatation area, and reducing most of protein and part of COD in the wastewater through air floatation treatment; the air-floating effluent enters an anaerobic tank 30, and coarse proteins are separated by centrifugation and drying after scum is discharged.
(2) Anaerobic effluent enters a membrane filtration system, and anaerobic biogas is sent into a biogas boiler after being desulfurized by a water seal.
(3) The anaerobic effluent is separated by a pre-filtering device through a DTRO membrane, the water produced by the DTRO membrane is discharged, the concentrated water enters a multi-effect evaporation system, the water production rate of the DTRO membrane is 50% -70%, and the maximum working pressure of the water inlet is 120bar;
(4) The steam of the biogas boiler is sent into a multi-effect evaporator and a dryer for concentrated water evaporation and crude protein drying.
(5) And (5) recycling the evaporated condensate, recycling salt, and separating and recycling crude protein.
According to the characteristics of heparin sodium wastewater, the treatment system simultaneously recovers protein, methane, salt and water resources in the wastewater treatment process, reduces pollutant emission, reduces the wastewater treatment operation cost, and has good social and economic benefits.
The utility model provides a thought and a method for a heparin sodium wastewater recovery treatment system, and the method and the way for realizing the technical scheme are more specific, the above is only a preferred embodiment of the utility model, and it should be pointed out that a plurality of improvements and modifications can be made by those skilled in the art without departing from the principle of the utility model, and the improvements and modifications are also considered as the protection scope of the utility model. The components not explicitly described in this embodiment can be implemented by using the prior art.
Claims (10)
1. The heparin sodium wastewater recovery treatment system is characterized by comprising a collecting tank (10), a flocculation air floatation tank (20), an anaerobic tank (30), a DTRO membrane assembly (40) and a multi-effect evaporator (50) which are connected in sequence through pipelines; the flocculation floatation tank (20) comprises a flocculation reaction zone (201), a dissolved gas release zone (202), a solid-liquid separation zone (203) and a scum collecting tank (204); the scum collection tank (204) is connected to a centrifuge (60) and a dryer (70) in sequence through a scum conveying pipe (205), thereby separating crude proteins.
2. The heparin sodium wastewater recycling system according to claim 1, wherein a three-phase separator (301) is arranged at the top of the anaerobic tank (30); the three-phase separator (301) is connected to the biogas boiler (80) through a biogas conveying pipe (302) to provide heating fuel for the biogas boiler (80); the biogas boiler (80) sends the generated high-temperature steam into the dryer (70) and the multi-effect evaporator (50) through the steam conveying pipe (801).
3. The heparin sodium wastewater recycling system according to claim 1, wherein in the flocculation air floatation tank (20), a flocculation reaction area (201), a dissolved air release area (202) and a solid-liquid separation area (203) are respectively separated by baffles; a communicating groove is formed at the bottom of a baffle plate between the flocculation reaction area (201) and the dissolved gas release area (202); and overflow grooves are arranged at the bottoms of the baffles between the dissolved gas release area (202) and the solid-liquid separation area (203).
4. A heparin sodium wastewater recycling system according to claim 3, wherein a stirring device (206) and a chitosan feeding pipeline (207) are arranged in the flocculation reaction zone (201).
5. The heparin sodium wastewater recycling system according to claim 3, wherein a slag scraping machine (208) is arranged at the top of the dissolved gas releasing area (202) and the top of the solid-liquid separation area (203), and scum at the top of the dissolved gas releasing area (202) and the top of the solid-liquid separation area (203) is scraped into a scum collecting groove (204) by a scraping plate of the slag scraping machine (208).
6. The heparin sodium wastewater recovery treatment system according to claim 1, wherein a tank top pulse water distributor (303) is arranged above the anaerobic tank (30), and a tank bottom hydraulic distributor (304) is arranged at the bottom of the anaerobic tank (30); the inlet end of the tank top pulse water distributor (303) is connected with the water outlet of the flocculation air floatation tank (20), the outlet end of the tank top pulse water distributor (303) is connected with the tank bottom hydraulic distributor (304) through a central pipe, and wastewater is sprayed out at a high speed through the tank bottom hydraulic distributor (304) to realize intermittent stirring of anaerobic sludge at the tank bottom.
7. The heparin sodium wastewater recycling system according to claim 2, wherein the top of the anaerobic tank (30) is sealed by a tank top plate, the three-phase separator (301) is arranged in a biogas storage space between the tank top and the liquid level, and anaerobic effluent is discharged by a porous water collecting pipe and sent to a subsequent component for treatment.
8. The heparin sodium wastewater recycling system according to claim 1, wherein an intermediate tank (90) for temporarily storing effluent is further arranged at the rear end of the anaerobic tank (30), and then the effluent is sent to the DTRO membrane module (40) for further separation.
9. The heparin sodium wastewater recovery treatment system of claim 8, wherein a prefilter device (100) is further arranged between the intermediate tank (90) and the DTRO membrane module (40); the prefilter device (100) is composed of a multi-media filter (110) and a bag filter (120); wherein, the lower part of the multi-medium filter (110) adopts quartz sand filter materials, and the upper part adopts fiber ball filter materials.
10. The heparin sodium wastewater recycling system according to claim 1, wherein in the DTRO membrane module (40), a convex membrane is adopted for the DTRO membrane, so that the feed liquid is in a turbulent flow state when flowing; the separated clean water is discharged through the outer discharge pipe up to standard, and the concentrated water is sent into the multi-effect evaporator (50) for evaporation treatment and solid salt generation.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321326498.1U CN219807872U (en) | 2023-05-26 | 2023-05-26 | Heparin sodium wastewater recovery treatment system |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202321326498.1U CN219807872U (en) | 2023-05-26 | 2023-05-26 | Heparin sodium wastewater recovery treatment system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN219807872U true CN219807872U (en) | 2023-10-10 |
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ID=88216822
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202321326498.1U Active CN219807872U (en) | 2023-05-26 | 2023-05-26 | Heparin sodium wastewater recovery treatment system |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN219807872U (en) |
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2023
- 2023-05-26 CN CN202321326498.1U patent/CN219807872U/en active Active
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