CN112624479B - Recycling treatment method and device for high-salt high-alcohol wastewater in heparin extraction - Google Patents
Recycling treatment method and device for high-salt high-alcohol wastewater in heparin extraction Download PDFInfo
- Publication number
- CN112624479B CN112624479B CN202011639426.3A CN202011639426A CN112624479B CN 112624479 B CN112624479 B CN 112624479B CN 202011639426 A CN202011639426 A CN 202011639426A CN 112624479 B CN112624479 B CN 112624479B
- Authority
- CN
- China
- Prior art keywords
- salt
- feed liquid
- distillation
- ethanol
- liquid conversion
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 239000002351 wastewater Substances 0.000 title claims abstract description 47
- HTTJABKRGRZYRN-UHFFFAOYSA-N Heparin Chemical compound OC1C(NC(=O)C)C(O)OC(COS(O)(=O)=O)C1OC1C(OS(O)(=O)=O)C(O)C(OC2C(C(OS(O)(=O)=O)C(OC3C(C(O)C(O)C(O3)C(O)=O)OS(O)(=O)=O)C(CO)O2)NS(O)(=O)=O)C(C(O)=O)O1 HTTJABKRGRZYRN-UHFFFAOYSA-N 0.000 title claims abstract description 34
- 229960002897 heparin Drugs 0.000 title claims abstract description 34
- 229920000669 heparin Polymers 0.000 title claims abstract description 34
- 238000000605 extraction Methods 0.000 title claims abstract description 31
- 238000004064 recycling Methods 0.000 title claims abstract description 28
- 238000000034 method Methods 0.000 title claims abstract description 21
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 123
- 239000007788 liquid Substances 0.000 claims abstract description 74
- 238000004821 distillation Methods 0.000 claims abstract description 52
- 238000006243 chemical reaction Methods 0.000 claims abstract description 48
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 47
- 238000002425 crystallisation Methods 0.000 claims abstract description 34
- 230000008025 crystallization Effects 0.000 claims abstract description 34
- 238000001704 evaporation Methods 0.000 claims abstract description 33
- 230000008020 evaporation Effects 0.000 claims abstract description 33
- 150000003839 salts Chemical class 0.000 claims abstract description 24
- 238000011084 recovery Methods 0.000 claims abstract description 19
- 239000011347 resin Substances 0.000 claims abstract description 12
- 229920005989 resin Polymers 0.000 claims abstract description 12
- 238000010828 elution Methods 0.000 claims abstract description 11
- 238000001556 precipitation Methods 0.000 claims abstract description 8
- 238000001914 filtration Methods 0.000 claims description 33
- 239000012267 brine Substances 0.000 claims description 18
- HPALAKNZSZLMCH-UHFFFAOYSA-M sodium;chloride;hydrate Chemical compound O.[Na+].[Cl-] HPALAKNZSZLMCH-UHFFFAOYSA-M 0.000 claims description 18
- 238000009833 condensation Methods 0.000 claims description 15
- 230000005494 condensation Effects 0.000 claims description 15
- 239000012528 membrane Substances 0.000 claims description 14
- 239000000047 product Substances 0.000 claims description 13
- 239000002699 waste material Substances 0.000 claims description 9
- 239000006004 Quartz sand Substances 0.000 claims description 8
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 8
- 239000000835 fiber Substances 0.000 claims description 8
- 239000000706 filtrate Substances 0.000 claims description 8
- 239000007921 spray Substances 0.000 claims description 6
- 238000010992 reflux Methods 0.000 claims description 3
- 230000001476 alcoholic effect Effects 0.000 claims description 2
- 239000000463 material Substances 0.000 abstract description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 4
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical class [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 7
- 239000013078 crystal Substances 0.000 description 6
- 239000010865 sewage Substances 0.000 description 4
- 238000002347 injection Methods 0.000 description 3
- 239000007924 injection Substances 0.000 description 3
- 238000005070 sampling Methods 0.000 description 3
- 239000011780 sodium chloride Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 2
- 230000007613 environmental effect Effects 0.000 description 2
- 239000003673 groundwater Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 125000004122 cyclic group Chemical group 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000003113 dilution method Methods 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 239000003456 ion exchange resin Substances 0.000 description 1
- 229920003303 ion-exchange polymer Polymers 0.000 description 1
- 238000011068 loading method Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 231100000331 toxic Toxicity 0.000 description 1
- 230000002588 toxic effect Effects 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/001—Processes for the treatment of water whereby the filtration technique is of importance
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/12—Halogens or halogen-containing compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
- C02F2101/34—Organic compounds containing oxygen
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Heat Treatment Of Water, Waste Water Or Sewage (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
The invention discloses a recycling treatment method and device for high-salt high-alcohol wastewater in heparin extraction, which are characterized in that high-salt ethanol wastewater generated in the heparin extraction process is subjected to alcohol precipitation treatment, distillation treatment is performed under the action of a heat source, and then feed liquid conversion and evaporation concentration are performed until the concentration of wastewater organic matters in a feed liquid conversion device reaches the emission standard. The recycling treatment method and device for the high-salt and high-alcohol wastewater in heparin extraction provided by the invention adopt the ingenious conception of combining ethanol recovery and evaporation crystallization phase, and a set of material liquid conversion device is specially designed to be communicated with a distillation device, a single-effect crystallization evaporation device and a resin elution device, so that unnecessary operations such as manual tool unloading are reduced, automation is realized, recycling of most casing salt is realized on the basis of recycling ethanol, the use of casing salt in a heparin extraction process is reduced, unreasonable emission of salt-containing wastewater is reduced, water resources are saved, the environment is protected, and the production cost is reduced.
Description
Technical Field
The invention belongs to the technical field of high-salt high-alcohol wastewater treatment methods, and particularly relates to a recycling treatment method and device for high-salt high-alcohol wastewater in heparin extraction.
Background
The current heparin extraction mainly relies on ion exchange resin to adsorb and enrich heparin, then the heparin is eluted by saturated saline, ethanol is deposited and dried to obtain medical raw material heparin, the process can produce high-salt ethanol waste liquid, the waste liquid is mainly produced in the rear section of heparin extraction process, and the waste water quantity in the rear section is not very large compared with the whole process, and the traditional treatment method is that after ethanol is recovered, the high-salt waste water is directly diluted, and the waste water is discharged after simple sewage treatment. However, the high-salt wastewater obtained after ethanol is recovered by adopting the existing process can cause a great deal of waste of water resources in the dilution process, and the unreasonable use and discharge of a great deal of casing salt is another waste, and meanwhile, the problems of environment are brought, the salinity of groundwater is increased, and the quality of the groundwater is reduced. The traditional treatment mode can not meet the requirements of economic development, environmental protection, energy conservation and emission reduction on the production of green factories.
Disclosure of Invention
In order to solve the problems in the prior art, the invention aims to provide a recycling treatment method and device for high-salt high-alcohol wastewater in heparin extraction, which are mainly used for recycling treatment of the high-salt high-alcohol wastewater in the heparin extraction process.
In order to achieve the above purpose and achieve the above technical effects, the invention adopts the following technical scheme:
a recycling treatment method of high-salt high-alcohol wastewater in heparin extraction comprises the following steps:
1) Performing alcohol precipitation treatment on high-salt ethanol waste liquid generated in the heparin extraction process to obtain high-salt high-alcohol waste water after alcohol precipitation, performing distillation treatment under the action of a heat source to obtain ethanol gas and high-salt high-COD waste water, condensing the ethanol gas into ethanol liquid, and preserving;
2) The high-salt high-COD wastewater is subjected to feed liquid conversion through a feed liquid conversion device, then evaporated and concentrated to obtain crystallized brine and concentrated steam, the crystallized brine is subjected to step 3), and the concentrated steam is recycled to an external water tank;
3) Recovering the crystallized salt water obtained in the step 2) to a feed liquid conversion device, filtering to obtain crystallized salt and filtrate, dissolving the crystallized salt in water, delivering the dissolved crystallized salt to a resin elution device, and carrying out the step 4) on the filtrate;
4) And 3) carrying out feed liquid conversion on the filtrate obtained in the step 3), then carrying out evaporation concentration, and repeating the steps 2) -4) until the concentration of the wastewater organic matters in the feed liquid conversion device reaches the discharge standard.
Further, in step 1), the heat source is steam, and the alcohol content of the ethanol liquid is not less than 75%.
Further, in the step 2), the concentrated steam is recycled to an external water tank through a water jet vacuum pump.
The invention discloses a recycling treatment device for high-salt high-alcohol wastewater in heparin extraction, which is characterized in that the recycling treatment device for the high-salt high-alcohol wastewater in heparin extraction is used for recycling treatment by adopting a recycling treatment method for the high-salt high-alcohol wastewater in heparin extraction, the recycling treatment device for the high-salt high-alcohol wastewater in heparin extraction comprises a distillation device, a condensation device, an ethanol recovery device, a finished product storage device, a feed liquid conversion device, a single-effect crystallization evaporation device, a resin elution device and a water jet vacuum pump, the distillation device is not communicated with the ethanol recovery device and the finished product storage device at the same time through the condensation device, the ethanol recovery device is communicated with the distillation device and is used for recovering ethanol, the distillation device is communicated with the single-effect crystallization evaporation device through the feed liquid conversion device, the feed liquid conversion device is communicated with the resin elution device, the single-effect crystallization evaporation device is communicated with the water jet vacuum pump, the water jet vacuum pump is communicated with an external water pool, a spray ball device is arranged at the inner side of the top of the feed liquid conversion device, and a crystallized salt water filtering device is arranged in the feed liquid conversion device.
Further, the distillation device comprises a distillation kettle and a distillation tower positioned above the distillation kettle, a return-shaped condensing pipe is arranged in the distillation kettle, a steam heat source is arranged in the return-shaped condensing pipe, and the distillation kettle is sequentially communicated with the distillation tower and the condensing device and is not simultaneously communicated with the ethanol recovery device and the finished product storage device.
Further, a gas-liquid separator is arranged between the single-effect crystallization evaporation device and the water jet vacuum pump.
Further, the crystallized brine filtering device sequentially comprises a filtering membrane layer, a quartz sand filtering layer and a biochar fiber layer which are in an inverted cone-shaped structure from top to bottom.
Further, the membrane interception molecular weight of the filtering membrane layer is 2000-15000Da.
Compared with the prior art, the invention has the beneficial effects that:
The ingenious conception of combining ethanol recovery and evaporation crystallization phase is adopted, on the basis of recycling ethanol, the cyclic utilization of most casing salt is realized, the use of casing salt in a heparin extraction process is reduced, unreasonable emission of salt-containing wastewater is reduced, water resources are saved, the environment is protected, and the production cost is reduced;
A set of material liquid conversion device is specially designed, two technologies of ethanol recovery and evaporation crystallization are perfectly connected, a distillation device, a single-effect crystallization evaporation device and a resin elution device in a heparin extraction process are communicated, meanwhile, operations such as unnecessary manual tool unloading and the like in an intermediate link are reduced, automation can be realized, and the purpose of recycling casing salt is fulfilled; a set of crystallization salt water filtering device is specially designed in the middle of the feed liquid conversion device and is used for separating sodium chloride crystals and wastewater;
the main increase cost of the invention is the steam consumption required by crystallization and evaporation operation, but the content of sodium chloride and other salts in the initial wastewater is close to saturation, the evaporation and crystallization are the optimal choice, and the cost of saved casing salt and unnecessary dilution water is considered, especially the most important environmental protection, so the process has the progress significance;
The water jet vacuum pump is selected to provide vacuum degree, and has the following advantages: the water jet vacuum pump can play a role in condensing while providing vacuum degree, the circulating water can absorb bad smell in the secondary steam and avoid directly discharging the bad smell into the atmosphere, and after the production is finished, water in an external water pool is discharged into the existing sewage treatment plant, so that the method is simple and efficient;
All processes are completed in the equipment through the specially designed feed liquid conversion tank and pipeline connection design, so that the labor loading and unloading cost is not required to be increased, and the automation degree is high.
Drawings
FIG. 1 is a schematic diagram of the structure of the present invention;
Fig. 2 is a schematic structural view of a crystallized brine filtering device of the present invention.
Detailed Description
The following embodiments of the present invention are described in detail so that the advantages and features of the present invention may be more readily understood by those skilled in the art, thereby making a clearer and more definite definition of the scope of the present invention.
As shown in fig. 1-2, a recycling treatment device for high-salt and high-alcohol wastewater in heparin extraction comprises a distillation device, a condensation device 7, an ethanol recovery device 9, a finished product storage device 10, a feed liquid conversion device 15, a single-effect crystallization evaporation device 18, a resin elution device 19 and a water injection vacuum pump 21, wherein the distillation device is not communicated with the ethanol recovery device 9 and the finished product storage device 10 at the same time through the condensation device 7, the ethanol recovery device 9 is communicated with the distillation device and is used for recovering ethanol, the distillation device is communicated with the single-effect crystallization evaporation device 18 through the feed liquid conversion device 15, the feed liquid conversion device 15 is communicated with the resin elution device 19, a second pump 13 is arranged between the feed liquid conversion device 15 and the resin elution device 19, a gas-liquid separator 20 is arranged between the single-effect crystallization evaporation device 18 and the water injection vacuum pump 21, the water injection vacuum pump 21 is communicated with an external water tank 24, a spray ball device 16 is arranged on the inner side of the top of the feed liquid conversion device 15, a plurality of groups of spray ball devices 16 can be arranged, and a crystallized salt water filtering device 14 is arranged in the feed liquid conversion device 15.
The distillation device comprises a distillation kettle 1 and a distillation tower 6 positioned above the distillation kettle 1, wherein a liquid inlet 3 for pouring high-salt high-alcohol wastewater after alcohol precipitation is arranged at the top of the distillation kettle 1, a plurality of sequentially arranged return-shaped condensation pipes 2 are arranged in the distillation kettle 1, the distance between two adjacent return-shaped condensation pipes 2 is 0.3-0.5mm, a steam heat source is arranged in each return-shaped condensation pipe 2, the steam heat source enters the return-shaped condensation pipe 2 from a steam inlet 4 at one end of the return-shaped condensation pipe 2, and steam in the return-shaped condensation pipe 2 exchanges heat with materials in the distillation kettle 1 and is condensed and discharged from a condensate water outlet 5 at one end of the return-shaped condensation pipe 2.
The distillation still 1 is sequentially communicated with the distillation tower 6 and the condensing device 7 and is not simultaneously communicated with the ethanol recovery device 9 and the finished product storage device 10, a sampling port 8 is arranged on a U-shaped pipeline between the top of the distillation tower 6 and the condensing device 7, ethanol gas (containing partial vapor) in the distillation still 1 is upwards diffused into the distillation tower 6 to be condensed, the water vapor in the ethanol gas is condensed into liquid and then flows into the distillation still 1 again, the ethanol gas continues to move upwards to the condensing device 7 to be condensed, the concentration of the ethanol in the ethanol gas is measured through the sampling port 8, if the concentration of the ethanol exceeds 75%, the ethanol liquid condensed by the condensing device 7 is stored into the finished product storage device 10, otherwise, the ethanol liquid condensed by the condensing device 7 is continuously flown into the ethanol recovery device 9 and then enters the distillation still 1 to be distilled again.
A valve 11 and a first pump 12 are arranged between the distillation still 1 and the feed liquid conversion device 15, and waste liquid in the distillation still 1 is pumped into the feed liquid conversion device 15 through the first pump 12 for feed liquid conversion.
The crystallization brine filtering device 14 is detachably arranged in the feed liquid conversion device 15, and is convenient to detach and clean, the crystallization brine filtering device 14 sequentially comprises a filtering membrane layer 25, a quartz sand filtering layer 26 and a biochar fiber layer 27 which are in an inverted cone-shaped structure from top to bottom, the membrane interception molecular weight of the filtering membrane layer 25 is 2000-15000Da, and the thicknesses of the quartz sand filtering layer 26 and the biochar fiber layer 27 are 3-6mm respectively. The vertical distance between the filtering membrane layer 25 and the quartz sand filtering layer 26 and the vertical distance between the quartz sand filtering layer 26 and the biochar fiber layer 27 are respectively 0.4-0.9mm.
A third pump 17 is arranged between the feed liquid conversion device 15 and the single-effect crystallization evaporation device 18, and is used for pumping the salt crystallization substances generated in the single-effect crystallization evaporation device 18 into the feed liquid conversion device 15.
The water or the like in the external water tank 24 is pumped into the water jet vacuum pump 21 by the fourth pump 22.
A steam inlet 23 is arranged at one side of the single-effect crystallization and evaporation device 18, and external steam enters the single-effect crystallization and evaporation device 18 through the steam inlet 23 and is used as a heat source for the post crystallization, evaporation and concentration operation.
A recycling treatment method of high-salt high-alcohol wastewater in heparin extraction comprises the following steps:
1) Carrying out alcohol precipitation treatment on high-salt ethanol waste liquid generated in the heparin extraction process to obtain high-salt high-alcohol waste water after alcohol precipitation, carrying out distillation treatment under the action of a steam heat source in a reflux condenser tube 2 to realize gas-liquid separation, obtaining ethanol gas and high-salt high-COD waste water, leaving the high-salt high-COD waste water at the bottom of a distillation kettle 1, allowing the ethanol gas to enter a distillation tower 6 for dewatering operation, then allowing the ethanol gas to enter a condensing device 7 for condensation into ethanol liquid, measuring the alcohol concentration in the ethanol gas through a sampling port 8, if the alcohol concentration exceeds 75%, storing the ethanol liquid condensed by the condensing device 7 into a finished product storage device 10, otherwise, continuously allowing the ethanol liquid condensed by the condensing device 7 to flow into an ethanol recovery device 9 and then allowing the ethanol liquid to enter the distillation kettle 1 for re-distillation operation;
2) The high-salt high-COD wastewater is pumped into a feed liquid conversion device 15 through a first pump 12 to be subjected to feed liquid conversion, then enters a single-effect crystallization evaporation device 18 through a second pump 13 to be subjected to evaporation crystallization concentration, crystallized brine and concentrated steam are obtained after concentration and evaporation, the crystallized brine such as sodium chloride is left at the bottom of a single-effect crystallization pot of the single-effect crystallization evaporation device 18, the crystallized brine is subjected to step 3), the concentrated steam is subjected to gas-liquid separation through a gas-liquid separator 20, and the separated gas enters a water jet vacuum pump 21 by utilizing pressure difference and is recycled to an external water tank 24, and then is discharged into a sewage treatment plant;
3) When the crystal brine at the bottom of the single-effect crystallization pot is excessive, the third pump 17 is started, the crystal brine at the bottom of the single-effect crystallization pot is pumped into the material liquid conversion device 15 through the third pump 17, flows through the filtering membrane layer 25, the quartz sand filtering layer 26 and the biochar fiber layer 27 in sequence for filtering, removing large particles and the like, and can remove toxic and harmful substances and the like through the biochar fiber layer 27, so that the water quality is improved, the water quality reaches the standard more quickly, the filtered crystal salt is left on the crystal brine filtering device 14, the crystal salt is dissolved after being sprayed by the spray ball device 16, and is sent to the resin eluting device 19, and the filtered filtrate is subjected to the step 4) and flows downwards to the bottom of the material liquid conversion device 15;
4) The filtrate obtained in the step 3) is subjected to feed liquid conversion, then is subjected to evaporation concentration, and is repeatedly executed according to the steps 2) -4) until the concentration of organic matters in the wastewater in the feed liquid conversion device 15 reaches the discharge standard, the evaporation crystallization operation is finished, and then the wastewater in the feed liquid conversion device 15 is discharged to a sewage treatment plant through a second pump 13.
In the step 1), the heat source is steam, and the alcoholic strength of the ethanol liquid is not lower than 75%.
In step 2), the concentrated steam is recovered to the external water tank 24 by the water jet vacuum pump 21.
The condensing device 7 adopts a condenser, a condensed water inlet and a condensed water outlet are formed in the condensing device, the ethanol recovery device 9, the finished product storage device 10 and the resin elution device 19 can adopt containers such as storage barrels, the feed liquid conversion device 15 is a container capable of containing waste liquid, the single-effect crystallization evaporation device 18 is of a cylindrical structure with spherical two ends, and the existing products or the existing technology can be adopted, so that details are omitted.
The part of the invention which is not specifically described is only required to adopt the prior art, and is not described in detail herein.
The foregoing description is only illustrative of the present invention and is not intended to limit the scope of the invention, and all equivalent structures or equivalent processes or direct or indirect application in other related technical fields are included in the scope of the present invention.
Claims (6)
1. The recycling treatment method of the high-salt high-alcohol wastewater in heparin extraction is characterized by comprising the following steps of:
1) Performing alcohol precipitation treatment on high-salt ethanol waste liquid generated in the heparin extraction process to obtain high-salt high-alcohol waste water after alcohol precipitation, performing distillation treatment under the action of a heat source to obtain ethanol gas and high-salt high-COD waste water, condensing the ethanol gas into ethanol liquid, and preserving;
2) The high-salt high-COD wastewater is subjected to feed liquid conversion through a feed liquid conversion device, a spray ball device is arranged on the inner side of the top of the feed liquid conversion device, a crystallized brine filtering device is arranged in the feed liquid conversion device, the crystallized brine filtering device sequentially comprises a filtering membrane layer, a quartz sand filtering layer and a biochar fiber layer which are in an inverted cone-shaped structure from top to bottom, the membrane interception molecular weight of the filtering membrane layer is 2000-15000Da, then evaporation concentration is carried out to obtain crystallized brine and concentrated steam, the crystallized brine is subjected to step 3), and the concentrated steam is recycled to an external water tank;
3) Recovering the crystallized salt water obtained in the step 2) to a feed liquid conversion device, filtering to obtain crystallized salt and filtrate, dissolving the crystallized salt in water, delivering the dissolved crystallized salt to a resin elution device, and carrying out the step 4) on the filtrate;
4) And 3) carrying out feed liquid conversion on the filtrate obtained in the step 3), then carrying out evaporation concentration, and repeating the steps 2) -4) until the concentration of the wastewater organic matters in the feed liquid conversion device reaches the discharge standard.
2. The method for recycling high-salt and high-alcohol wastewater generated in heparin extraction according to claim 1, wherein in the step 1), the heat source is steam, and the alcoholic strength of the ethanol liquid is not lower than 75%.
3. The method for recycling high-salt and high-alcohol wastewater in heparin extraction according to claim 1, wherein in the step 2), the concentrated steam is recycled to an external water tank through a water jet vacuum pump.
4. The recycling treatment device for the high-salt high-alcohol wastewater in heparin extraction is characterized by being used for carrying out recycling treatment on the recycling treatment method for the high-salt high-alcohol wastewater in heparin extraction according to any one of claims 1-3, the recycling treatment device for the high-salt high-alcohol wastewater in heparin extraction comprises a distillation device, a condensation device, an ethanol recovery device, a finished product storage device, a feed liquid conversion device, a single-effect crystallization evaporation device, a resin elution device and a water jet vacuum pump, the distillation device is not communicated with the ethanol recovery device and the finished product storage device through the condensation device, the ethanol recovery device is communicated with the distillation device and carries out ethanol recovery, the distillation device is communicated with the single-effect crystallization evaporation device through the feed liquid conversion device, the feed liquid conversion device is communicated with an external water jet vacuum pump, a spray ball device is arranged on the inner side of the top of the feed liquid conversion device, the feed liquid conversion device is internally provided with a crystalline brine filtering device, the crystalline brine filtering device sequentially comprises a filtering membrane layer, a quartz sand filtering layer and a biochar fiber layer which are in inverted cone structures from top to bottom, and the membrane interception molecular weight of the filtering membrane layer is 2000-15000Da.
5. The recycling device for the high-salt and high-alcohol wastewater generated in heparin extraction according to claim 4, wherein the distillation device comprises a distillation kettle and a distillation tower positioned above the distillation kettle, a reflux condenser is arranged in the distillation kettle, a steam heat source is arranged in the reflux condenser, and the distillation kettle is sequentially communicated with the distillation tower and the condensation device and is not simultaneously communicated with the ethanol recovery device and the finished product storage device.
6. The recycling device for high-salt and high-alcohol wastewater in heparin extraction according to claim 4, wherein a gas-liquid separator is arranged between the single-effect crystallization evaporation device and the water jet vacuum pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011639426.3A CN112624479B (en) | 2020-12-31 | 2020-12-31 | Recycling treatment method and device for high-salt high-alcohol wastewater in heparin extraction |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202011639426.3A CN112624479B (en) | 2020-12-31 | 2020-12-31 | Recycling treatment method and device for high-salt high-alcohol wastewater in heparin extraction |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN112624479A CN112624479A (en) | 2021-04-09 |
| CN112624479B true CN112624479B (en) | 2024-06-11 |
Family
ID=75290439
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN202011639426.3A Active CN112624479B (en) | 2020-12-31 | 2020-12-31 | Recycling treatment method and device for high-salt high-alcohol wastewater in heparin extraction |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN112624479B (en) |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN214528548U (en) * | 2020-12-31 | 2021-10-29 | 无锡优普克生物科技有限公司 | Resourceful treatment device for high-salt and high-alcohol wastewater in heparin extraction |
Family Cites Families (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104085933A (en) * | 2014-07-22 | 2014-10-08 | 北京金泰天成科技有限责任公司 | High-salinity and high organic matter wastewater treatment process |
| CN105923822B (en) * | 2016-05-31 | 2019-06-14 | 江苏京源环保股份有限公司 | Desulfurization wastewater divides mud, divides salt technique of zero discharge |
| CN110697959B (en) * | 2019-10-15 | 2022-02-25 | 齐鲁工业大学 | Resource recycling method for high-salt high-ammonia nitrogen wastewater |
| CN111995698A (en) * | 2020-08-07 | 2020-11-27 | 无锡海思瑞科技有限公司 | Method for simultaneously extracting heparin sodium and intestinal membrane protein peptide based on enzymolysis method |
-
2020
- 2020-12-31 CN CN202011639426.3A patent/CN112624479B/en active Active
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN214528548U (en) * | 2020-12-31 | 2021-10-29 | 无锡优普克生物科技有限公司 | Resourceful treatment device for high-salt and high-alcohol wastewater in heparin extraction |
Also Published As
| Publication number | Publication date |
|---|---|
| CN112624479A (en) | 2021-04-09 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN103709016B (en) | A kind of pervaporation method refines technique and the device of glycol dimethyl ether | |
| CN103387306A (en) | Garbage leachate processing system and processing technology thereof | |
| CN205773874U (en) | A kind of Novel desulphurization waste water zero discharge device | |
| CN202038886U (en) | Treatment system for high-concentration industrial ammonia-nitrogen waste water | |
| CN106365369A (en) | Biogas slurry concentration and nutrient enrichment system for large biogas project and application method thereof | |
| CN104860460A (en) | Processing device for aniline intermediate production waste water | |
| CN203360209U (en) | Treatment system for garbage leachate | |
| CN102336650B (en) | Stripping process and device for removing organic impurities in brufen sodium salt | |
| CN214528548U (en) | Resourceful treatment device for high-salt and high-alcohol wastewater in heparin extraction | |
| CN112624479B (en) | Recycling treatment method and device for high-salt high-alcohol wastewater in heparin extraction | |
| CN206204081U (en) | A kind of phenmethylol produces the circulation production device of wastewater utilization | |
| CN101704818A (en) | Method for extracting caffeine from methylated mother through adsorption separation | |
| CN101670191A (en) | Adsorption concentration method and device of volatile organic matter in solution | |
| CN205109056U (en) | Sour vapor removal recovery unit of red fuming nitric acid (RFNA) production | |
| CN205258214U (en) | Phenyl amines midbody waste water's processing apparatus | |
| CN102764559B (en) | Combined technique of separating and recycling VOCS (volatile organic compounds) from industrial waste gas by adsorption-desorption-rectification-pervaporation | |
| CN214990744U (en) | Multi-stage membrane permeation structure for wastewater purification | |
| CN212769939U (en) | Treatment system for cellulose production wastewater | |
| CN107673511A (en) | A kind of tower draws chinic acid recovery method in standby gallic acid waste liquid | |
| CN102295380A (en) | Processing and recovering method of aromatic nitro-compound wastewater | |
| CN206767852U (en) | A kind of recycling and processing device of carboxylate industrial production wastewater | |
| CN207047053U (en) | A kind of rubbish percolation liquid membrane concentrate advanced treatment apparatus | |
| CN206680228U (en) | Electroosmose process reuse high-salt wastewater device | |
| CN212770294U (en) | Macroporous resin adsorption treatment o-toluidine waste water and material recovery device | |
| CN104478767B (en) | Method for processing beta salt mother liquor through low temperature acid separation technology |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |