Fermentation pharmaceutical wastewater pretreatment system

Abstract

The utility model relates to the technical field of pharmaceutical wastewater pretreatment, and discloses a fermentation type pharmaceutical wastewater pretreatment system. Comprising a pretreatment unit, a deamination unit, a produced water adjusting tank, a high-pressure reverse osmosis unit, an evaporation unit, a fermentation pharmaceutical wastewater inlet pipe, a pretreatment unit produced water pipe, a pretreatment unit concentrated water pipe, a deamination unit produced water pipe, an ammonium salt output pipe, a reverse osmosis unit produced water pipe, a reverse osmosis unit concentrated water pipe and an evaporated liquor outlet pipe. In the fermented pharmaceutical wastewater treated by the device disclosed by the utility model, refractory organics and antibacterial substances are greatly reduced, the biodegradability of the wastewater is improved, the concentration of the organics and the concentration of ammonia nitrogen are greatly reduced, the load of subsequent biochemical treatment is greatly reduced, the retention time is shortened, and the treatment efficiency is improved. The occupied area of a subsequent biological treatment structure is greatly reduced; and the sludge amount is reduced.

Description

TECHNICAL FIELD

[0001] The utility model relates to the technical field of pharmaceutical wastewater pretreatment, especially to a fermentation pharmaceutical wastewater pretreatment system. BACKGROUND

[0002] Fermentation pharmaceuticals are to use the nutrition, metabolism and growth characteristics of microorganisms to screen specific microorganism species, control environmental conditions to make these microorganisms ferment to obtain the required products, and then separate and purify to obtain the required drugs. With the rapid development of China's pharmaceutical industry, the pharmaceutical technology level is gradually improved, the fermentation pharmaceutical scale is continuously expanded, the drug types and output are increasing, and due to the multiple types of raw materials and low utilization rate, the effective ingredient content of the product is generally not high, after refining, a large amount of by-products, mycelium, unused raw materials, solvent residue after refining and other waste liquid are left in the fermentation wastewater to form a large amount of highly polluted wastewater. The fermentation pharmaceutical wastewater has high colority, high pollutant concentration, complex composition, and difficult biodegradation and organic solvents, antibiotics and other toxic substances with antibacterial effect.

[0003] The traditional coagulation sedimentation + anaerobic + aerobic combined process for treating fermentation pharmaceutical wastewater has the problems of long residence time, large land occupation, poor treatment effect, even unable to degrade pollutants, large sludge amount and the like, and therefore, the utility model provides a fermentation pharmaceutical wastewater pretreatment system. UTILITY MODEL CONTENT

[0004] The utility model discloses a fermentation pharmaceutical wastewater pretreatment process which has the advantages of small land occupation, good treatment effect and stable effluent quality, can greatly improve the biodegradability of fermentation pharmaceutical wastewater, reduce the subsequent biochemical treatment load and shorten the residence time.

[0005] In order to achieve the above object, the utility model adopts the following technical scheme:

[0006] The fermentation pharmaceutical wastewater pretreatment system comprises a pretreatment unit, a deamination unit, a water production adjusting tank, a high-pressure reverse osmosis unit, an evaporation unit, a fermentation pharmaceutical wastewater inlet pipe, a pretreatment unit water production pipe, a pretreatment unit concentrated water pipe, a deamination unit water production pipe, an ammonium salt output pipe, a reverse osmosis unit water production pipe, a reverse osmosis unit concentrated water pipe and an evaporation liquid outlet pipe, the pretreatment unit is connected with the fermentation pharmaceutical wastewater inlet pipe at the front end, and connected with the deamination unit through the pretreatment unit water production pipe at the rear end, and the deamination unit is connected with the water production adjusting tank through the deamination unit water production pipe.

[0007] Preferably, the pretreatment unit comprises a raw water buffer tank, a ceramic membrane water inlet pump, a ceramic membrane filter, a ceramic membrane water production tank, a nanofiltration membrane water inlet pump, a nanofiltration membrane filter, a heat exchanger, an alkali adding device, a pipeline mixer and a pretreatment unit water production tank, and the raw water buffer tank, the ceramic membrane water inlet pump, the ceramic membrane filter, the ceramic membrane water production tank, the nanofiltration membrane water inlet pump, the nanofiltration membrane filter, the heat exchanger, the pipeline mixer and the pretreatment unit water production tank are sequentially connected through pipelines; wherein the concentrated water outlet of the ceramic membrane filter is connected with the concentrated water backflow port of the raw water buffer tank, the concentrated water outlet of the nanofiltration membrane filter is connected with the pretreatment unit concentrated water pipe, the dosing port of the pipeline mixer is connected with the alkali adding device, and the water outlet of the pretreatment unit water production tank is connected with the pretreatment unit water production pipe.

[0008] Preferably, the deamination unit comprises a deamination membrane water inlet pump, a PTFE deamination membrane assembly, an absorption liquid circulating tank, an absorption liquid circulating pump and an ammonium salt output pump, the water inlet port of the deamination membrane water inlet pump is connected with the pretreatment unit water production pipe, the water outlet port is connected with the water inlet port of the PTFE deamination membrane assembly, the water production port of the deamination membrane assembly is connected with the deamination unit water production pipe, the water outlet port of the absorption liquid circulating tank is connected with the absorption liquid inlet port of the PTFE deamination membrane assembly through the absorption liquid circulating pump, the absorption liquid backflow port of the absorption liquid circulating tank is connected with the absorption liquid outlet port of the PTFE deamination membrane assembly, and the ammonium salt outlet port of the absorption liquid circulating tank is connected with the ammonium salt output pipe through the ammonium salt output pump.

[0009] Preferably, the high-pressure reverse osmosis unit comprises a reverse osmosis raw water tank, a reverse osmosis water inlet pump, a reverse osmosis device, a reverse osmosis concentrated water tank and a reverse osmosis concentrated water output pump, the water inlet of the reverse osmosis raw water tank is connected with the concentrated water pipe of the pretreatment unit, the water outlet of the reverse osmosis raw water tank is connected with the reverse osmosis device through the reverse osmosis water inlet pump, the water outlet of the reverse osmosis device is connected with the reverse osmosis unit water pipe, the concentrated water outlet of the reverse osmosis device is connected with the water inlet of the reverse osmosis concentrated water tank, and the water outlet of the reverse osmosis concentrated water tank is connected with the reverse osmosis unit concentrated water pipe through the reverse osmosis concentrated water output pump.

[0010] Preferably, the evaporation unit comprises an evaporator and a condenser, the feed inlet of the evaporator is connected with the reverse osmosis unit concentrated water pipe, the steam outlet of the evaporator is connected with the steam inlet of the condenser, and the evaporated liquid outlet of the condenser is connected with the evaporated liquid outlet pipe.

[0011] Preferably, the PTFE deamination membrane assembly is internally filled with PTFE hollow fiber membrane filaments, the inside of the membrane filaments is a wastewater channel, the outside of the membrane filaments is an absorption liquid channel, and only free ammonia in the wastewater is allowed to pass through the membrane holes from the wastewater channel on the inside of the membrane filaments to the absorption liquid channel on the outside of the membrane filaments, so that the ammonia nitrogen in the wastewater is absorbed by the absorption liquid, and the wastewater and the absorption liquid on the inside and outside of the membrane filaments cannot pass through the membrane holes and can only flow in the channels.

[0012] Compared with the prior art, the beneficial effects of the present application are:

[0013] After the fermentation pharmaceutical wastewater is treated, the biodegradable organic matter and bacteriostatic substances are greatly reduced, the biodegradability of the wastewater is improved, the organic matter concentration and the ammonia nitrogen concentration are greatly reduced, the load of subsequent biochemical treatment is greatly reduced, the residence time is shortened, the land occupation area of subsequent biological treatment structures is greatly reduced, and the sludge amount is reduced;

[0014] Secondly, the PTFE deamination membrane is used for treating high-concentration ammonia nitrogen in fermentation pharmaceutical wastewater, the membrane performance is stable, the adaptability to water quality and environmental conditions is strong, and the ammonia nitrogen removal rate is high. BRIEF DESCRIPTION OF DRAWINGS

[0015] Figure 1 A composition schematic diagram of a fermentation pharmaceutical wastewater pretreatment system is provided for the present application.

[0016] In the figure: 1, pretreatment unit; 2, deamination unit; 3, water production conditioning tank; 4, high-pressure reverse osmosis unit; 5, evaporation unit; 6, fermentation pharmaceutical wastewater inlet pipe; 7, pretreatment unit water production pipe; 8, pretreatment unit concentrated water pipe; 9, deamination unit water production pipe; 10, ammonium salt output pipe; 11, reverse osmosis unit water production pipe; 12, reverse osmosis unit concentrated water pipe; 13, evaporation liquid outlet pipe; 101, raw water buffer tank; 102, ceramic membrane inlet pump; 103, ceramic membrane filter; 104, ceramic membrane water production tank; 105, nanofiltration membrane inlet pump; 106, nanofiltration membrane filter; 107, heat exchanger; 108, alkali adding device; 109, pipeline mixer; 110, pretreatment unit water production tank; 201, deamination membrane inlet pump; 202, PTFE deamination membrane assembly; 203, absorption liquid circulating tank; 204, absorption liquid circulating pump; 205, ammonium salt output pump; 401, reverse osmosis raw water tank; 402, reverse osmosis inlet pump; 403, reverse osmosis device; 404, reverse osmosis concentrated water tank; 405, reverse osmosis concentrated water output pump; 501, evaporator; 502, condenser. DETAILED DESCRIPTION

[0017] The technical solutions in the embodiments of the utility model will be clearly and completely described below with reference to the drawings in the embodiments of the utility model. Obviously, the described embodiments are only part of the embodiments of the utility model, rather than all the embodiments.

[0018] Reference Figure 1 A fermentation pharmaceutical wastewater pretreatment system, comprising: a pretreatment unit 1, a deamination unit 2, a water production conditioning tank 3, a high-pressure reverse osmosis unit 4, an evaporation unit 5, a fermentation pharmaceutical wastewater inlet pipe 6, a pretreatment unit water production pipe 7, a pretreatment unit concentrated water pipe 8, a deamination unit water production pipe 9, an ammonium salt output pipe 10, a reverse osmosis unit water production pipe 11, a reverse osmosis unit concentrated water pipe 12, an evaporation liquid outlet pipe 13, the pretreatment unit 1 is connected with the fermentation pharmaceutical wastewater inlet pipe 6 at the front end, and is connected with the deamination unit 2 at the rear end through the pretreatment unit water production pipe 7; the deamination unit 2 is connected with the water production conditioning tank 3 through the deamination unit water production pipe 9; the high-pressure reverse osmosis unit 4 is connected with the pretreatment unit 1 at the front end through the pretreatment unit concentrated water pipe 8, and is connected with the water production conditioning tank 3 at the rear end through the reverse osmosis unit water production pipe 11; the evaporation unit 5 is connected with the deamination unit 2 and the high-pressure reverse osmosis unit 4 at the front end through the ammonium salt output pipe 10 and the reverse osmosis unit concentrated water pipe 12 respectively, and is connected with the water production conditioning tank 3 at the rear end through the evaporation liquid outlet pipe 13.

[0019] In this embodiment, the pretreatment unit 1 is composed of raw water buffer tank 101, ceramic membrane water inlet pump 102, ceramic membrane filter 103, ceramic membrane water tank 104, nanofiltration membrane water inlet pump 105, nanofiltration membrane filter 106, heat exchanger 107, alkali adding device 108, pipeline mixer 109 and pretreatment unit water tank 110. The raw water buffer tank 101, ceramic membrane water inlet pump 102, ceramic membrane filter 103, ceramic membrane water tank 104, nanofiltration membrane water inlet pump 105, nanofiltration membrane filter 106, heat exchanger 107, pipeline mixer 109 and pretreatment unit water tank 110 are sequentially connected in the above order, and the outlet of the former is sequentially connected with the inlet of the latter. In addition, the concentrated water outlet of the ceramic membrane filter 103 is connected with the concentrated water return port of the raw water buffer tank 101, the concentrated water outlet of the nanofiltration membrane filter 106 is connected with the pretreatment unit concentrated water pipe 8, the dosing port of the pipeline mixer 109 is connected with the alkali adding device 108, and the outlet of the pretreatment unit water tank 110 is connected with the pretreatment unit water outlet pipe 7.

[0020] In this embodiment, the alkali solution added by the alkali adding device 108 is one of sodium hydroxide and potassium hydroxide solution, and the addition amount is to increase the pH of the incoming water to above 11.5. Under the above temperature and pH conditions, more than 98% of the ammonium ions (NH4+) in the water are converted into free ammonia (NH3), which is removed in the subsequent ammonia removal unit 2.

[0021] In this embodiment, the ammonia removal unit 2 is composed of ammonia removal membrane water inlet pump 201, PTFE ammonia removal membrane assembly 202, absorption liquid circulating tank 203, absorption liquid circulating pump 204 and ammonium salt output pump 205. The water inlet of the ammonia removal membrane water inlet pump 201 is connected with the pretreatment unit water outlet pipe 7, the water outlet is connected with the water inlet of the PTFE ammonia removal membrane assembly 202, the water outlet of the ammonia removal membrane assembly 202 is connected with the ammonia removal unit water outlet pipe 9, the water outlet of the absorption liquid circulating tank 203 is connected with the absorption liquid inlet of the PTFE ammonia removal membrane assembly 202 through the absorption liquid circulating pump 204, the absorption liquid return port of the absorption liquid circulating tank 203 is connected with the absorption liquid outlet of the PTFE ammonia removal membrane assembly 202, and the ammonium salt outlet of the absorption liquid circulating tank 203 is connected with the ammonium salt output pipe 10 through the ammonium salt output pump 205.

[0022] In this embodiment, the PTFE ammonia removal membrane assembly 202 is filled with PTFE hollow fiber membrane filaments inside. The inside of the membrane filaments is a wastewater channel, and the outside of the membrane filaments is an absorption liquid channel. The membrane filaments only allow free ammonia in the wastewater to pass through the membrane holes from the wastewater channel inside the membrane filaments to the absorption liquid channel outside the membrane filaments, so that the ammonia nitrogen in the wastewater is absorbed by the absorption liquid. The wastewater and the absorption liquid on both sides of the membrane filaments cannot pass through the membrane holes and can only flow in their respective channels.

[0023] In this embodiment, the high-pressure reverse osmosis unit 4 is composed of a reverse osmosis raw water tank 401, a reverse osmosis water inlet pump 402, a reverse osmosis device 403, a reverse osmosis concentrated water tank 404, and a reverse osmosis concentrated water output pump 405. The water inlet of the reverse osmosis raw water tank 401 is connected to the concentrated water pipe 8 of the pretreatment unit, the water outlet of the reverse osmosis raw water tank 401 is connected to the reverse osmosis device 403 through the reverse osmosis water inlet pump 402, the water outlet of the reverse osmosis device 403 is connected to the reverse osmosis unit water pipe 11, the concentrated water outlet of the reverse osmosis device 403 is connected to the water inlet of the reverse osmosis concentrated water tank 404, and the water outlet of the reverse osmosis concentrated water tank 404 is connected to the reverse osmosis unit concentrated water pipe 12 through the reverse osmosis concentrated water output pump 405.

[0024] In this embodiment, the evaporation unit 5 is composed of an evaporator 501 and a condenser 502. The feed inlet of the evaporator 501 is connected to the reverse osmosis unit concentrated water pipe 12 and the ammonium salt output pipe 10, the steam outlet of the evaporator 501 is connected to the steam inlet of the condenser 502, and the evaporated liquid outlet of the condenser 502 is connected to the evaporated liquid outlet pipe 13.

[0025] In this embodiment, the absorption liquid is a dilute sulfuric acid solution. When the ammonia consumed by the absorption of sulfuric acid is converted into ammonium sulfate, new sulfuric acid is supplemented to the absorption liquid circulating tank 203.

[0026] Working principle:

[0027] The fermentation pharmaceutical wastewater enters the raw water buffer tank 101 through the fermentation pharmaceutical wastewater inlet pipe 6, and after adjusting the water quality and quantity, it is transported to the ceramic membrane filter 103 by the ceramic membrane water inlet pump 102 to remove suspended impurities in the wastewater, improve the water quality and protect the subsequent treatment unit. The concentrated water produced by the ceramic membrane filter 103 is returned to the raw water buffer tank 101. As the concentration of suspended solids in the raw water buffer tank 101 increases, the suspended particles collide and coagulate with each other and settle, and are discharged from the bottom of the raw water buffer tank 101. The filtered water produced by the ceramic membrane filter 103 enters the ceramic membrane water tank 104, and is transported to the nanofiltration filter 106 by the nanofiltration membrane water inlet pump 105. The filtered water produced by the nanofiltration filter 106 is divided into two streams: concentrated water and produced water.

[0028] The water produced by the nanofiltration membrane filter 106 is heated to 40-45 DEG C by a heat exchanger 107, the heated wastewater is mixed with liquid alkali added by an alkali adding device 108 in a pipeline mixer 109, the pH of the wastewater is adjusted to above 11.5, after the temperature and pH of the wastewater are adjusted to the preset conditions by pretreatment, more than 98% of the ammonium ions in the wastewater are converted into free ammonia, then the wastewater enters a pretreatment device water tank 110, is transported to a PTFE deamination membrane assembly 202 by a deamination membrane feed pump 201, the wastewater flows in the inner side of the membrane filaments of the PTFE deamination membrane assembly 202, mass transfer occurs between the wastewater and the absorbent liquid in the outer side of the membrane filaments, the free ammonia in the wastewater penetrates the membrane filament surface and enters the outer side of the membrane filaments to be absorbed by the absorbent liquid, and the absorbed water is discharged into a water production adjusting tank.

[0029] The concentrated water of the nanofiltration membrane filter 106 enters a reverse osmosis unit raw water tank 401 through a pretreatment unit concentrated water pipe 8, is transported to a reverse osmosis device 403 by a reverse osmosis feed pump 402, and is treated, the treated reverse osmosis water enters the water production adjusting tank 3 through a reverse osmosis unit water pipe 11, and the produced reverse osmosis concentrated water enters an evaporation unit 5 for treatment.

[0030] The water produced by the deamination unit 2, the water produced by the high-pressure reverse osmosis unit 4 and the evaporation liquid produced by the evaporation unit 5 enter the water production adjusting tank 3 to adjust the water quality and quantity, then the pH can be adjusted to neutral to enter a subsequent biological treatment unit for further treatment.

[0031] Compared with the prior art, the biopharmaceutical wastewater treated by the system has a large reduction in the content of refractory organic matter and bacteriostatic substances, the biodegradability of the wastewater is improved, the content of organic matter and ammonia nitrogen is greatly reduced, the load of subsequent biochemical treatment is greatly reduced, the residence time is shortened, the land area of subsequent biological treatment structures is greatly reduced, and the sludge amount is reduced.

[0032] The above merely describes a preferred specific embodiment of the present application, but the protection scope of the present application is not limited to this, any person skilled in the art can make equivalent replacement or change according to the technical scheme and the inventive concept of the present application within the technical range disclosed by the present application, which should be covered in the protection scope of the present application.

Claims

1. A pretreatment system for fermentation-based pharmaceutical wastewater, characterized in that: include: The system comprises a pretreatment unit, an ammonia removal unit, a product water equalization tank, a high-pressure reverse osmosis unit, an evaporation unit, a fermentation pharmaceutical wastewater inlet pipe, a pretreatment unit product water pipe, a pretreatment unit concentrate pipe, an ammonia removal unit product water pipe, an ammonium salt outlet pipe, a reverse osmosis unit product water pipe, a reverse osmosis unit concentrate pipe, and an evaporator outlet pipe. The pretreatment unit is connected to the fermentation pharmaceutical wastewater inlet pipe at its front end and to the ammonia removal unit at its rear end via the pretreatment unit product water pipe. The ammonia removal unit is connected to the product water equalization tank via the ammonia removal unit product water pipe. The high-pressure reverse osmosis unit is connected to the pretreatment unit at its front end via the pretreatment unit concentrate pipe and to the product water equalization tank via the reverse osmosis unit product water pipe. The evaporation unit is connected to the ammonia removal unit and the high-pressure reverse osmosis unit at its front end via the ammonium salt outlet pipe and the reverse osmosis unit concentrate pipe, respectively, and to the product water equalization tank at its rear end via the evaporator outlet pipe.

2. The pretreatment system for fermentation-based pharmaceutical wastewater according to claim 1, characterized in that: The pretreatment unit includes a raw water buffer tank, a ceramic membrane feed pump, a ceramic membrane filter, a ceramic membrane product water tank, a nanofiltration membrane feed pump, a nanofiltration membrane filter, a heat exchanger, an alkali addition device, a pipeline mixer, and a pretreatment unit product water tank. The raw water buffer tank, the ceramic membrane feed pump, the ceramic membrane filter, the ceramic membrane product water tank, the nanofiltration membrane feed pump, the nanofiltration membrane filter, the heat exchanger, the pipeline mixer, and the pretreatment unit product water tank are connected sequentially by pipelines. The concentrate outlet of the ceramic membrane filter is connected to the concentrate return outlet of the raw water buffer tank; the concentrate outlet of the nanofiltration membrane filter is connected to the concentrate pipe of the pretreatment unit; the chemical dosing port of the pipeline mixer is connected to the alkali addition device; and the outlet of the pretreatment unit product water tank is connected to the pretreatment unit product water pipe.

3. The pretreatment system for fermentation-based pharmaceutical wastewater according to claim 1, characterized in that: The ammonia removal unit includes an ammonia removal membrane inlet pump, a PTFE ammonia removal membrane module, an absorbent circulation tank, an absorbent circulation pump, and an ammonium salt output pump. The inlet of the ammonia removal membrane inlet pump is connected to the pretreatment unit's product water pipe, and the outlet is connected to the inlet of the PTFE ammonia removal membrane module. The product water outlet of the ammonia removal membrane module is connected to the ammonia removal unit's product water pipe. The outlet of the absorbent circulation tank is connected to the absorbent inlet of the PTFE ammonia removal membrane module through the absorbent circulation pump. The absorbent reflux port of the absorbent circulation tank is connected to the absorbent outlet of the PTFE ammonia removal membrane module. The ammonium salt outlet of the absorbent circulation tank is connected to the ammonium salt output pipe through the ammonium salt output pump.

4. The pretreatment system for fermentation-based pharmaceutical wastewater according to claim 2, characterized in that: The high-pressure reverse osmosis unit includes a reverse osmosis raw water tank, a reverse osmosis feed pump, a reverse osmosis device, a reverse osmosis concentrate tank, and a reverse osmosis concentrate output pump. The inlet of the reverse osmosis raw water tank is connected to the concentrate pipe of the pretreatment unit. The outlet of the reverse osmosis raw water tank is connected to the reverse osmosis device through the reverse osmosis feed pump. The product water outlet of the reverse osmosis device is connected to the product water pipe of the reverse osmosis unit. The concentrate outlet of the reverse osmosis device is connected to the inlet of the reverse osmosis concentrate tank. The outlet of the reverse osmosis concentrate tank is connected to the concentrate pipe of the reverse osmosis unit through the reverse osmosis concentrate output pump.

5. The pretreatment system for fermentation-based pharmaceutical wastewater according to claim 1, characterized in that: The evaporation unit includes an evaporator and a condenser. The feed inlet of the evaporator is connected to the concentrate pipe of the reverse osmosis unit, the steam outlet of the evaporator is connected to the steam inlet of the condenser, and the evaporator liquid outlet is connected to the evaporator liquid outlet pipe.

6. The pretreatment system for fermentation-based pharmaceutical wastewater according to claim 3, characterized in that: The PTFE deammoniation membrane module is filled with PTFE hollow fiber membrane filaments. The inner side of the membrane filaments is a wastewater channel, and the outer side of the membrane filaments is an absorbent channel. Only free ammonia in the wastewater is allowed to pass through the membrane pores from the wastewater channel on the inner side of the membrane filaments into the absorbent channel on the outer side of the membrane filaments. This allows the ammonia nitrogen in the wastewater to be absorbed by the absorbent, while the wastewater and absorbent on both sides of the membrane filaments cannot pass through the membrane pores and can only flow in their respective channels.

7. The pretreatment system for fermentation-based pharmaceutical wastewater according to claim 6, characterized in that: The absorbent is a dilute sulfuric acid solution. After the sulfuric acid is absorbed and the ammonia is consumed and converted into ammonium sulfate, new sulfuric acid is added to the absorbent circulation tank.

8. The pretreatment system for fermentation-based pharmaceutical wastewater according to claim 2, characterized in that: The alkali solution added by the alkali addition device is either sodium hydroxide or potassium hydroxide solution.

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