CN220579095U - System for comprehensive treatment of condensation wastewater and sodium butyrate as byproduct - Google Patents
System for comprehensive treatment of condensation wastewater and sodium butyrate as byproduct Download PDFInfo
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- CN220579095U CN220579095U CN202322060197.5U CN202322060197U CN220579095U CN 220579095 U CN220579095 U CN 220579095U CN 202322060197 U CN202322060197 U CN 202322060197U CN 220579095 U CN220579095 U CN 220579095U
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- 239000002351 wastewater Substances 0.000 title claims abstract description 96
- MFBOGIVSZKQAPD-UHFFFAOYSA-M sodium butyrate Chemical compound [Na+].CCCC([O-])=O MFBOGIVSZKQAPD-UHFFFAOYSA-M 0.000 title claims abstract description 33
- 239000006227 byproduct Substances 0.000 title claims abstract description 10
- 238000009833 condensation Methods 0.000 title description 9
- 230000005494 condensation Effects 0.000 title description 7
- 239000007788 liquid Substances 0.000 claims abstract description 86
- 238000001816 cooling Methods 0.000 claims abstract description 24
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 20
- 230000003647 oxidation Effects 0.000 claims abstract description 19
- 238000001035 drying Methods 0.000 claims abstract description 10
- 238000001914 filtration Methods 0.000 claims abstract description 10
- CBENFWSGALASAD-UHFFFAOYSA-N Ozone Chemical compound [O-][O+]=O CBENFWSGALASAD-UHFFFAOYSA-N 0.000 claims abstract description 9
- 238000001704 evaporation Methods 0.000 claims description 38
- 230000008020 evaporation Effects 0.000 claims description 36
- 239000013078 crystal Substances 0.000 claims description 8
- 239000002002 slurry Substances 0.000 claims description 7
- 239000000047 product Substances 0.000 abstract description 6
- 239000002699 waste material Substances 0.000 abstract description 4
- ZTQSAGDEMFDKMZ-UHFFFAOYSA-N Butyraldehyde Chemical compound CCCC=O ZTQSAGDEMFDKMZ-UHFFFAOYSA-N 0.000 description 14
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 14
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 12
- 239000012141 concentrate Substances 0.000 description 11
- 238000004519 manufacturing process Methods 0.000 description 7
- 238000000034 method Methods 0.000 description 7
- 239000010865 sewage Substances 0.000 description 7
- 239000000243 solution Substances 0.000 description 7
- HGBOYTHUEUWSSQ-UHFFFAOYSA-N valeric aldehyde Natural products CCCCC=O HGBOYTHUEUWSSQ-UHFFFAOYSA-N 0.000 description 7
- FERIUCNNQQJTOY-UHFFFAOYSA-N Butyric acid Chemical compound CCCC(O)=O FERIUCNNQQJTOY-UHFFFAOYSA-N 0.000 description 6
- XUPYJHCZDLZNFP-UHFFFAOYSA-N butyl butanoate Chemical compound CCCCOC(=O)CCC XUPYJHCZDLZNFP-UHFFFAOYSA-N 0.000 description 6
- 238000002425 crystallisation Methods 0.000 description 5
- 230000008025 crystallization Effects 0.000 description 5
- 239000000463 material Substances 0.000 description 4
- 230000008569 process Effects 0.000 description 4
- 238000005086 pumping Methods 0.000 description 4
- 238000004065 wastewater treatment Methods 0.000 description 4
- 238000002306 biochemical method Methods 0.000 description 3
- 239000003513 alkali Substances 0.000 description 2
- 239000003814 drug Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002253 acid Substances 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- IDYWQONQVXWFQP-UHFFFAOYSA-N butan-1-ol;octan-1-ol Chemical compound CCCCO.CCCCCCCCO IDYWQONQVXWFQP-UHFFFAOYSA-N 0.000 description 1
- 230000015556 catabolic process Effects 0.000 description 1
- 239000002826 coolant Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 238000006731 degradation reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000007865 diluting Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000706 filtrate Substances 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 238000006386 neutralization reaction Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000011272 standard treatment Methods 0.000 description 1
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Abstract
The utility model discloses a system for comprehensively treating condensed wastewater and producing sodium butyrate as a byproduct, which comprises a condensed wastewater raw water tank, an oxidation tank, a buffer tank, a first-effect evaporator feeding preheater, a first-effect evaporator and a second-effect evaporator which are connected in sequence, wherein the oxidation tank is connected with an ozone generator; the heat source medium inlet of the second-effect evaporator is connected with the liquid-vapor outlet of the first-effect evaporator, the liquid-liquid inlet of the second-effect evaporator is connected with the liquid-liquid outlet of the first-effect evaporator, the liquid-vapor outlet of the second-effect evaporator is connected with the waste water tank through the feed preheater of the first-effect evaporator and the vapor-generating cooler, the heat source medium outlet of the second-effect evaporator is connected with the waste water tank through the secondary vapor condensate cooler, and the liquid-liquid outlet of the second-effect evaporator is sequentially connected with the waste water tank through the concentrated liquid cooler, the concentrated liquid storage tank, the cooling crystallizer and the filtering and drying integrated machine. According to the utility model, the useful components in the condensed wastewater are fully recycled, and the byproduct is obtained to obtain the sodium butyrate product with high added value, so that the resource waste is avoided to the greatest extent.
Description
Technical Field
The utility model relates to a wastewater treatment system, in particular to a system for comprehensively treating condensed wastewater and by-producing sodium butyrate.
Background
The condensed wastewater is high COD, high salt and high alkalinity wastewater generated in the production process of the butanol-octanol device condensation process, has pungent odor and is seriously harmful to health and environment. Under the condition of stable production, the COD of the condensed wastewater is 50000-60000 mg/L, the pH is 13-14, the components are complex, the water content is 94.5-95 wt%, the sodium butyrate is 4.7-5 wt%, the sodium hydroxide is 0.2-0.3 wt%, the total content of butyraldehyde and butanol is 0.1-0.14 wt%, and the total content of various substances such as small amount of octenal (EPA), butyl butyrate and C12 is also contained, wherein the total content of sodium butyrate, butyraldehyde and butanol with higher content is more than 96 percent. For the treatment of condensed wastewater, a commonly adopted method in the industry is a biochemical method, but the COD of the wastewater is high and the alkalinity is strong, so that the tolerance limit of strains used in the existing sewage treatment plant is seriously exceeded. Therefore, the pH of the condensed wastewater needs to be adjusted by adding acid, and the condensed wastewater can enter a biochemical system through a large number of diluting methods, so that the total amount of wastewater to be treated is greatly increased, the wastewater treatment load of a sewage treatment plant is increased, and the treatment of other wastewater in a park is indirectly influenced. In addition, the biochemical method is used for treating the condensed wastewater, and organic components with high added values in the condensed wastewater are subjected to indiscriminate biochemical degradation, so that resource waste is caused to a certain extent.
Disclosure of Invention
The utility model aims to overcome the defects in the prior art and provides a system for comprehensively treating condensed wastewater and by-producing sodium butyrate. The utility model carries out a series of pretreatment such as ozone oxidation, evaporation concentration, cooling crystallization and the like on the condensed wastewater, recycles useful components in the condensed wastewater, byproducts sodium butyrate with high added value, and then delivers the residual wastewater with greatly reduced COD and weakened alkalinity to a wastewater treatment plant for standard treatment by a biochemical method.
The aim of the utility model is achieved by the following technical scheme.
The utility model relates to a system for comprehensively treating condensed wastewater and producing sodium butyrate as a byproduct, which comprises a condensed wastewater raw water tank, an oxidation tank, a buffer tank, a first-effect evaporator feeding preheater, a first-effect evaporator and a second-effect evaporator which are sequentially connected through pipelines, wherein the oxidation tank is connected with an ozone generator through a pipeline;
the heat source medium inlet of the two-effect evaporator is connected to the feed liquid evaporation gas outlet at the top of the one-effect evaporator through a pipeline, the feed liquid inlet of the two-effect evaporator is connected to the feed liquid outlet at the bottom of the one-effect evaporator through a pipeline, the feed liquid evaporation gas outlet at the top of the two-effect evaporator is connected to the wastewater tank through a pipeline sequentially through the feed preheater of the one-effect evaporator and the evaporation gas-producing cooler, the heat source medium outlet of the two-effect evaporator is connected to the wastewater tank through a pipeline through the secondary steam condensate cooler, and the feed liquid outlet at the bottom of the two-effect evaporator is connected to the wastewater tank through a pipeline sequentially through the concentrate cooler, the concentrate storage tank, the cooling crystallizer and the filtration drying integrated machine.
The waste water treatment device is characterized in that a condensation waste water feeding pump is arranged on a pipeline connected between a condensation waste water raw water tank and an oxidation tank, a buffer tank feeding pump is arranged on a pipeline connected between the oxidation tank and the buffer tank, an effective evaporator feeding pump is arranged on a pipeline connected between the buffer tank and an effective evaporator feeding preheater, a cooling crystallizer feeding pump is arranged on a pipeline connected between a concentrated solution storage tank and a cooling crystallizer, a crystal slurry pump is arranged on a pipeline connected between the cooling crystallizer and a filtering and drying integrated machine, and a waste water transfer pump is arranged at a liquid outlet of the waste water tank.
The feed preheater of the one-effect evaporator is of a shell-and-tube structure, a feed liquid inlet of the feed preheater of the one-effect evaporator is connected to a liquid outlet of the buffer tank through a pipeline, a feed liquid outlet of the feed preheater of the one-effect evaporator is connected to a feed liquid inlet of the one-effect evaporator through a pipeline, a heat source inlet of the feed preheater of the one-effect evaporator is connected to a feed liquid evaporation gas outlet at the top of the two-effect evaporator through a pipeline, and a heat source outlet of the feed preheater of the one-effect evaporator is connected to the evaporation gas-producing cooler through a pipeline.
The shell side inlet and the shell side outlet of the one-effect evaporator are respectively used as a heat source medium inlet and a heat source medium outlet, and the tube side inlet, the top tube side outlet and the bottom tube side outlet of the one-effect evaporator are respectively used as a feed liquid inlet, a feed liquid evaporation gas outlet and a feed liquid outlet; the feed liquid inlet of the first-effect evaporator is connected to the feed liquid outlet of the feed preheater of the first-effect evaporator through a pipeline, the feed liquid evaporation gas outlet at the top of the first-effect evaporator is connected to the heat source medium inlet of the second-effect evaporator through a pipeline, and the feed liquid outlet at the bottom of the first-effect evaporator is connected to the feed liquid inlet of the second-effect evaporator through a pipeline.
The double-effect evaporator is in a shell-and-tube structure, steam passes through a shell side, feed liquid passes through a tube side, a shell side inlet and a shell side outlet of the double-effect evaporator are respectively used as a heat source medium inlet and a heat source medium outlet, and a tube side inlet, a top tube side outlet and a bottom tube side outlet of the double-effect evaporator are respectively used as a feed liquid inlet, a feed liquid evaporation gas outlet and a feed liquid outlet.
Compared with the prior art, the technical scheme of the utility model has the following beneficial effects:
(1) The utility model realizes the comprehensive treatment of the condensed wastewater, simultaneously recycles the useful components as much as possible, and the byproduct obtains the sodium butyrate product with high added value, thereby avoiding the waste of resources, enriching the product structure of enterprises and bringing considerable economic benefits to the enterprises.
(2) The utility model oxidizes butyraldehyde and butanol in the wastewater into butyric acid, and generates sodium butyrate by reacting with sodium hydroxide in the wastewater, thereby not only improving the content of sodium butyrate, but also consuming alkali in the wastewater and lowering the pH. After extracting sodium butyrate from waste water, the COD of sodium butyrate is reduced from 50000-60000 mg/L to less than 3000mg/L, and the pH is reduced from 13-14 to 11-12. The rest waste water is treated by the sewage treatment plant, and can be directly biochemically treated without dilution by adding water, so that the water is saved, the total amount of the waste water to be treated is greatly reduced, and the treatment load of the sewage treatment plant is lightened. In addition, the cost of the medicament for adjusting the pH value when the waste water enters the biochemical system can be saved due to the reduction of the pH value of the residual waste water; the COD total amount is reduced, so that the treatment difficulty and the treatment time can be reduced.
Drawings
FIG. 1 is a schematic diagram of a system for comprehensively treating condensed wastewater and by-producing sodium butyrate.
Reference numerals: 1-condensation wastewater raw water tank, 2-condensation wastewater feed pump, 3-oxidation tank, 4-ozone generator, 5-buffer tank feed pump, 6-buffer tank, 7-one-effect evaporator feed pump, 8-one-effect evaporator feed preheater, 9-one-effect evaporator, 10-two-effect evaporator, 11-evaporation gas-generating cooler, 12-concentrate cooler, 13-secondary steam condensate cooler, 14-concentrate storage tank, 15-cooling crystallizer feed pump, 16-cooling crystallizer, 17-crystal slurry pump, 18-filtration drying integrated machine, 19-wastewater tank, 20-wastewater transfer pump.
Detailed Description
The utility model is further described below with reference to the accompanying drawings.
The utility model is further described below with reference to the accompanying drawings.
As shown in FIG. 1, the system for comprehensively treating condensed wastewater and producing sodium butyrate as a byproduct comprises a condensed wastewater raw water tank 1, a condensed wastewater feed pump 2, an oxidation tank 3, an ozone generator 4, a buffer tank feed pump 5, a buffer tank 6, a first-effect evaporator feed pump 7, a first-effect evaporator feed preheater 8, a first-effect evaporator 9, a second-effect evaporator 10, an evaporation gas-producing cooler 11, a concentrate cooler 12, a secondary steam condensate cooler 13, a concentrate storage tank 14, a cooling crystallizer feed pump 15, a cooling crystallizer 16, a crystal slurry pump 17, a filtering and drying integrated machine 18, a wastewater tank 19, a wastewater transfer pump 20 and related connecting pipelines.
The device is characterized in that a condensation wastewater inlet pump 2 is connected between a discharge port of a condensation wastewater raw water tank 1 and a feed port of an oxidation tank 3 through a pipeline, an ozone generator 4 is connected with the oxidation tank 3 through a pipeline, a buffer tank feed pump 5 is connected between a discharge port of the oxidation tank 3 and a feed port of a buffer tank 6 through a pipeline, and an effective evaporator feed pump 7 is connected between a discharge port of the buffer tank 6 and a feed liquid inlet of an effective evaporator feed preheater 8 through a pipeline. The feed liquid outlet of the feed preheater 8 of the first-effect evaporator is connected to the feed liquid inlet of the first-effect evaporator 9 through a pipeline, the feed liquid evaporation gas outlet at the top of the first-effect evaporator 9 is connected to the heat source medium inlet of the second-effect evaporator 10 through a pipeline, the feed liquid outlet at the bottom of the first-effect evaporator 9 is connected to the feed liquid inlet of the second-effect evaporator 10 through a pipeline, the heat source medium inlet of the first-effect evaporator 9 enters steam, and condensed steam condensate is recovered through the heat source medium outlet of the first-effect evaporator 9. The feed liquid evaporation gas outlet at the top of the two-effect evaporator 10 is connected to a wastewater tank 19 through a pipeline sequentially through a first-effect evaporator feed preheater 8 and an evaporation gas production cooler 11, the heat source medium outlet of the two-effect evaporator 10 is connected to the wastewater tank 19 through a pipeline through a secondary steam condensate cooler 13, and the feed liquid outlet at the bottom of the two-effect evaporator 10 is connected to the wastewater tank 19 through a pipeline sequentially through a concentrate cooler 12, a concentrate storage tank 14, a cooling crystallizer feed pump 15, a cooling crystallizer 16, a crystal slurry pump 17 and a filtering and drying integrated machine 18. Wherein the filter and dryer unit 18 is capable of producing sodium butyrate. The liquid outlet of the wastewater tank 19 is provided with a wastewater transfer pump 20, and wastewater in the wastewater tank 19 is sent to a sewage treatment plant for standard discharge through the wastewater transfer pump 20.
In the above system, the evaporative gas cooler 11, the concentrate cooler 12 and the secondary steam condensate cooler 13 may all use circulating water as cooling medium.
In the system, the feeding preheater 8 of the one-effect evaporator is arranged in a shell-and-tube structure, a heat source passes through a shell pass, and a feed liquid passes through a tube pass. The feed liquid inlet of the first-effect evaporator feed preheater 8 is connected to the liquid outlet of the buffer tank 6 through a pipeline, the feed liquid outlet of the first-effect evaporator feed preheater 8 is connected to the feed liquid inlet of the first-effect evaporator 9 through a pipeline, the heat source inlet of the first-effect evaporator feed preheater 8 is connected to the feed liquid evaporation gas outlet at the top of the second-effect evaporator 10 through a pipeline, and the heat source outlet of the first-effect evaporator feed preheater 8 is connected to the evaporation gas-producing cooler 11 through a pipeline. Meanwhile, a first steam pipeline for use in a starting stage is further connected to a heat source inlet of the first-effect evaporator feed preheater 8, a first steam condensate pipeline for use in the starting stage is further connected to a heat source outlet of the first-effect evaporator feed preheater 8, and steam used in the first-effect evaporator feed preheater can be low-pressure steam of an existing production system, the gauge pressure is 0.2-0.3MPa, and the temperature is 140-160 ℃. In the start-up stage, when no material is generated at the top of the two-effect evaporator 10, the steam can be used for preheating the feed in the feed preheater 8 of the one-effect evaporator; when the flow is completed and material evaporation gas is generated at the top of the two-effect evaporator 10, the one-effect evaporator feeding preheater 8 can stop steam as a heat source, switch to a normal heat exchange flow and use the evaporation gas at the top of the two-effect evaporator 10 as the heat source. In addition, in order to meet the above switching process, valves may be provided on the pipes connecting the heat source inlet and the heat source outlet of the primary evaporator feed preheater 8.
In the above system, the first-effect evaporator 9 and the second-effect evaporator 10 are both arranged in a shell-and-tube structure, and the steam passes through the shell pass and the feed liquid passes through the tube pass. The shell side inlet and the shell side outlet of the first-effect evaporator 9 are respectively used as a heat source medium inlet and a heat source medium outlet and are respectively connected with a second steam pipeline and a second steam condensate pipeline. The tube side inlet, the top tube side outlet and the bottom tube side outlet of the first-effect evaporator 9 are respectively used as a feed liquid inlet, a feed liquid evaporation gas outlet and a feed liquid outlet. The two-effect evaporator 10 is arranged into a shell-and-tube structure, the steam passes through a shell side, the feed liquid passes through a tube side, a shell side inlet and a shell side outlet of the two-effect evaporator 10 are respectively used as a heat source medium inlet and a heat source medium outlet, and a tube side inlet, a top tube side outlet and a bottom tube side outlet of the two-effect evaporator 10 are respectively used as a feed liquid inlet, a feed liquid evaporation gas outlet and a feed liquid outlet. The steam used by the first-effect evaporator 9 can be from low-pressure steam of the existing production system on site, the gauge pressure is 0.4-0.6 MPa, the temperature is 200-220 ℃, steam condensate is recycled to the production system, the steam generated at the top of the first-effect evaporator 9 is used as secondary steam to provide a heat source for the second-effect evaporator 10, the non-evaporated feed liquid at the bottom of the first-effect evaporator 9 enters the second-effect evaporator 10 for further evaporation and concentration, and the steam generated at the top of the second-effect evaporator 10 is conveyed to the first-effect evaporator feed preheater 8 to be used as a heat source to preheat the feed of the first-effect evaporator 9.
Based on the system for comprehensively treating the condensed wastewater and by-producing sodium butyrate, the method for comprehensively treating the condensed wastewater and by-producing sodium butyrate provided by the utility model comprises the following specific implementation processes:
the first step: starting a condensed wastewater feeding pump 2, and pumping the condensed wastewater in a condensed wastewater raw water tank 1 into an oxidation tank 3 until the effective volume of the condensed wastewater is 70-80%. The ozone generator 4 is started, ozone is introduced into the oxidation tank 3 for oxidation for 3-7 hours, the ozone concentration in the feed liquid is controlled at 200-300 ppm, butyraldehyde and butanol in the wastewater are oxidized into butyric acid as much as possible, and then the butyric acid and the sodium hydroxide originally existing in the wastewater are subjected to neutralization reaction to generate sodium butyrate, so that the concentration of the sodium butyrate is improved, part of alkali is consumed, and the pH of the wastewater is reduced. And starting a buffer tank feeding pump 5 to pump all the oxidized feed liquid in the oxidation tank 3 into a buffer tank 6.
Wherein, COD of the condensed wastewater raw water is 50000-60000 mg/L, pH is 13-14, water content is 94.5-95 wt%, sodium butyrate is 4.7-5 wt%, sodium hydroxide is 0.2-0.3 wt%, butyraldehyde and butanol are 0.1-0.14 wt% in total, and trace amount of octenal (EPA), butyl butyrate, C12 and other substances are contained.
And a second step of: starting a first-effect evaporator feed pump 7, pumping the feed liquid in the buffer tank 6 into a first-effect evaporator feed preheater 8, preheating to 50-80 ℃, then conveying to a first-effect evaporator 9 for primary evaporation, and evaporating part of water in the wastewater and unreacted light components such as butyraldehyde, butanol and the like. The vaporized gas enters the two-effect evaporator 10 as secondary steam from the top of the one-effect evaporator 9 to provide a heat source for the two-effect evaporator. The feed liquid which is not evaporated at the bottom of the first-effect evaporator 9 flows into the second-effect evaporator 10 to be evaporated and concentrated continuously, and part of water and residual light components such as butyraldehyde, butanol and the like are further evaporated. The gas evaporated from the top of the two-effect evaporator 10 is fed into the preheater 8 and the evaporation gas-generating cooler 11 through the one-effect evaporator in sequence, and then cooled to 30-40 ℃ and enters the wastewater tank 19. The main components of the concentrated solution at the bottom of the two-effect evaporator 10 are sodium butyrate, water and trace butyl butyrate, EPA, C12 and other heavy components, and the concentrated solution is cooled to 15-25 ℃ by a concentrated solution cooler 12 and enters a concentrated solution storage tank 14. The secondary steam condensate of the two-effect evaporator 10 is cooled to 30-40 ℃ by a secondary steam condensate cooler 13 and enters a wastewater tank 19.
Wherein, in the starting stage, when no material is generated at the top of the two-effect evaporator 10, the steam provided by the first steam pipeline can be used for preheating the feed in the feed preheater 8 of the one-effect evaporator; when the flow is completed and material evaporation gas is generated at the top of the two-effect evaporator 10, the one-effect evaporator feeding preheater 8 can stop the steam provided by the first steam pipeline as a heat source, switch to a normal heat exchange flow and use the evaporation gas at the top of the two-effect evaporator 10 as the heat source.
Wherein, the heat source used by the first-effect evaporator 9 is derived from low-pressure steam (0.4-0.6 MPa, 200-220 ℃) of the existing production system on site, and the steam condensate returns to the system. The operating pressure of the first-effect evaporator 9 can be 0.02-0.04 MPa, and the operating pressure of the second-effect evaporator 10 can be-0.02-0 MPa. The feeding flow of the first-effect evaporator 9 can be 2-3 t/h, the evaporation capacity (namely, the secondary steam flow) of the feed liquid evaporation gas of the first-effect evaporator 9 can be 1.2-1.8 t/h, the evaporation capacity (namely, the steam flow generated at the top of the second-effect evaporator 10) of the feed liquid evaporation gas of the second-effect evaporator 10 can be 0.6-0.9 t/h, the concentrated solution flow can be 0.2-0.3 t/h, and the mass fraction of sodium butyrate in the concentrated solution can be 45-47%. The medium pressure is measured by a gauge pressure meter.
And a third step of: the cooling crystallizer feed pump 15 is started and a certain amount of concentrate in the concentrate tank 14 is pumped to the cooling crystallizer 16 for cooling crystallization. To ensure the crystallization effect, a certain amount of solid sodium butyrate may be added as seed crystals to the cooling crystallizer 16.
Wherein, the feed liquid adding amount of the cooling crystallizer 16 can be 60-70% of the effective volume, the cooling crystallization temperature can be-8 ℃ to-2 ℃, the cooling crystallization time can be 2-4 h, and the seed crystal adding amount can be 0.1-0.2% of the total mass of the feed liquid.
Fourth step: and starting a crystal slurry pump 17, pumping all the slurry crystallized in the cooling crystallizer 16 into a filtering and drying integrated machine 18 for filtering and drying for 1-2 hours to obtain a sodium butyrate product with the purity of more than 99%, and flowing the filtrate into a wastewater tank 19.
Fifth step: starting a waste water transfer pump 20, and pumping the residual waste water (COD is less than 3000mg/L, pH is 11-12) in the waste water tank 19 to a sewage treatment plant for continuous biochemical treatment, and discharging the waste water reaching the standard. Wherein, the flow rate of the waste water transfer pump 20 can be 1.9-2.9 t/h.
In the working process of the field actual operation, the first step, the third step and the fourth step can be batch operation, and the second step and the fifth step can be continuous operation.
According to the utility model, the useful components in the condensed wastewater are fully recycled, and the byproduct is obtained to obtain a sodium butyrate product with high added value, so that the resource waste is avoided to the greatest extent, the product structure of enterprises is enriched, considerable economic benefits are brought to the enterprises, the residual wastewater enters a sewage treatment plant to be directly biochemically treated without being diluted by adding water, the water is saved, the medicament cost for regulating the pH is saved, the treatment difficulty is reduced, and the treatment time is shortened.
Although the function and operation of the present utility model has been described above with reference to the accompanying drawings, the present utility model is not limited to the above-described specific functions and operations, but the above-described specific embodiments are merely illustrative, not restrictive, and many forms can be made by those having ordinary skill in the art without departing from the spirit of the present utility model and the scope of the appended claims, which are included in the protection of the present utility model.
Claims (5)
1. The system for comprehensively treating the condensed wastewater and producing sodium butyrate as a byproduct is characterized by comprising a condensed wastewater raw water tank (1), an oxidation tank (3), a buffer tank (6), a first-effect evaporator feeding preheater (8), a first-effect evaporator (9) and a second-effect evaporator (10) which are sequentially connected through pipelines, wherein the oxidation tank (3) is connected with an ozone generator (4) through a pipeline;
the heat source medium inlet of the two-effect evaporator (10) is connected to the feed liquid evaporation gas outlet at the top of the one-effect evaporator (9) through a pipeline, the feed liquid inlet of the two-effect evaporator (10) is connected to the feed liquid outlet at the bottom of the one-effect evaporator (9) through a pipeline, the feed liquid evaporation gas outlet at the top of the two-effect evaporator (10) is sequentially connected to the waste water tank (19) through the one-effect evaporator feed preheater (8) and the evaporation gas-generating cooler (11) through a pipeline, the heat source medium outlet of the two-effect evaporator (10) is connected to the waste water tank (19) through the pipeline through the secondary steam condensate cooler (13), and the feed liquid outlet at the bottom of the two-effect evaporator (10) is sequentially connected to the waste water tank (19) through the concentrated liquid cooler (12), the concentrated liquid storage tank (14), the cooling crystallizer (16) and the filtration and drying integrated machine (18) through pipelines.
2. The system for comprehensively treating condensed wastewater and by-producing sodium butyrate according to claim 1, wherein a condensed wastewater feed pump (2) is arranged on a pipeline connected between a condensed wastewater raw water tank (1) and an oxidation tank (3), a buffer tank feed pump (5) is arranged on a pipeline connected between the oxidation tank (3) and a buffer tank (6), an effective evaporator feed pump (7) is arranged on a pipeline connected between the buffer tank (6) and an effective evaporator feed preheater (8), a cooling crystallizer feed pump (15) is arranged on a pipeline connected between a concentrated solution storage tank (14) and a cooling crystallizer (16), a crystal slurry pump (17) is arranged on a pipeline connected between the cooling crystallizer (16) and a filtering and drying integrated machine (18), and a wastewater transfer pump (20) is arranged at a liquid outlet of the wastewater tank (19).
3. The system for comprehensively treating condensed wastewater and producing sodium butyrate as per claim 1, wherein the feed preheater (8) of the first-effect evaporator is arranged in a shell-and-tube structure, the feed liquid inlet of the feed preheater (8) of the first-effect evaporator is connected to the liquid outlet of the buffer tank (6) through a pipeline, the feed liquid outlet of the feed preheater (8) of the first-effect evaporator is connected to the feed liquid inlet of the first-effect evaporator (9) through a pipeline, the heat source inlet of the feed preheater (8) of the first-effect evaporator is connected to the feed liquid evaporation gas outlet at the top of the second-effect evaporator (10) through a pipeline, and the heat source outlet of the feed preheater (8) of the first-effect evaporator is connected to the evaporation gas-producing cooler (11) through a pipeline.
4. The system for comprehensively treating condensed wastewater and producing sodium butyrate as per claim 1, wherein the one-effect evaporator (9) is in a shell-and-tube structure, a steam shell side and a feed liquid shell side, a shell side inlet and a shell side outlet of the one-effect evaporator (9) are respectively used as a heat source medium inlet and a heat source medium outlet, and a tube side inlet, a top tube side outlet and a bottom tube side outlet of the one-effect evaporator (9) are respectively used as a feed liquid inlet, a feed liquid evaporation gas outlet and a feed liquid outlet; the feed liquid inlet of the first-effect evaporator (9) is connected to the feed liquid outlet of the first-effect evaporator feed preheater (8) through a pipeline, the feed liquid evaporation gas outlet at the top of the first-effect evaporator (9) is connected to the heat source medium inlet of the second-effect evaporator (10) through a pipeline, and the feed liquid outlet at the bottom of the first-effect evaporator (9) is connected to the feed liquid inlet of the second-effect evaporator (10) through a pipeline.
5. The system for comprehensively treating condensed wastewater and producing sodium butyrate as per claim 1, wherein the two-effect evaporator (10) is of a shell-and-tube structure, a steam shell pass and a feed liquid shell pass, a shell pass inlet and a shell pass outlet of the two-effect evaporator (10) are respectively used as a heat source medium inlet and a heat source medium outlet, and a tube pass inlet, a top tube pass outlet and a bottom tube pass outlet of the two-effect evaporator (10) are respectively used as a feed liquid inlet, a feed liquid evaporation gas outlet and a feed liquid outlet.
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