Energy-saving wine brewing wastewater zero-discharge treatment system

Abstract

The invention discloses an energy-saving wine brewing wastewater zero-discharge treatment system. The energy-saving wine brewing wastewater zero-discharge treatment system comprises winery wastewater pretreatment, anaerobic digestion treatment, membrane treatment, sludge treatment and biogas treatment, the winery wastewater comprises high-concentration wastewater, vinasse residue water, low-concentration wastewater, factory domestic sewage and circulating cooling water; the first output end of the anaerobic digestion treatment is connected with the first input end of the membrane treatment; a second output end of the anaerobic digestion treatment device is connected with a first input end of the sludge treatment device; a first output end for sludge treatment outputs stabilized sludge; the output end of the membrane treatment is connected with the second input end of the sludge treatment, and the second output end of the sludge treatment is connected with the second input end of the anaerobic digestion treatment; the third output end of the anaerobic digestion treatment is connected with the input end of the biogas treatment, and the output end of the biogas treatment is connected with the second input end of the membrane treatment. The waste heat generated by the system can be fully utilized to reduce the energy consumption in the operation stage, and the stability of the system is improved.

Description

Technical Field

[0001] The present application relates to the technical field of sewage treatment, and in particular to an energy-saving zero-discharge treatment system for brewing wastewater. Background Art

[0002] The production wastewater of brewing process mainly includes distillation pot bottom water, primary pot washing water, tank residue filtrate, raw material soaking water, pipeline and equipment washing water, cooling circulating water, etc. It is rich in protein, amino acids, low-carbon alcohols (ethanol and amyl alcohol, etc.) and fatty acids, and belongs to high-concentration organic wastewater. This type of wastewater has the characteristics of low pH, high chemical oxygen demand (COD), high suspended solids (SS) concentration, strong biodegradability and complex composition, and is difficult to treat.

[0003] The anaerobic process has the advantages of low investment, high efficiency, low energy consumption, and high load. It can also use the generated biogas for heating and power generation, and is suitable for the treatment of high-concentration organic wastewater. However, the removal effect of microorganisms on total phosphorus and ammonia nitrogen in anaerobic environments is limited, and further treatment by aerobic methods is required. However, aerobic treatment also has problems such as large footprint and high energy consumption. In order to meet the current winery wastewater treatment standards, the effluent still needs to be deeply treated. In summary, the current winery wastewater treatment process has problems such as difficulty in meeting effluent quality standards, large footprint, and high operating energy consumption. Therefore, it is urgent to develop a new energy-saving winery wastewater zero-discharge treatment system. Summary of the invention

[0004] The embodiment of the present application solves the problems of substandard water quality, large footprint and high operating energy consumption in the prior art of winery wastewater treatment by providing an energy-saving zero-discharge treatment system for brewing wastewater, thereby achieving "zero-discharge" standard reuse of winery wastewater. It can not only make full use of the waste heat generated by the system itself to reduce energy consumption in the operation stage, but also reduce the system's footprint and increase the stability of the system.

[0005] An embodiment of the present invention provides an energy-saving zero-discharge treatment system for brewing wastewater, comprising brewery wastewater, pretreatment, anaerobic digestion treatment, membrane treatment, sludge treatment and biogas treatment; the brewery wastewater comprises high-concentration wastewater and wine slag water; the high-concentration wastewater and the wine slag water both enter the pretreatment section through the first input end of the pretreatment; the first output end of the pretreatment is connected to the first input end of the anaerobic digestion treatment, and the first output end of the anaerobic digestion treatment is connected to the first input end of the membrane treatment; the second output end of the anaerobic digestion treatment is connected to the first input end of the sludge treatment; the first output end of the sludge treatment outputs stabilized sludge; the output end of the membrane treatment is connected to the second input end of the sludge treatment, and the second output end of the sludge treatment is connected to the second input end of the anaerobic digestion treatment; the third output end of the anaerobic digestion treatment is connected to the input end of the biogas treatment, and the output end of the biogas treatment is connected to the second input end of the membrane treatment.

[0006] In a possible implementation, the membrane treatment includes a forward osmosis membrane bioreactor, a membrane distillation reactor and a clear water tank; the winery wastewater also includes circulating cooling water; the first input end of the forward osmosis membrane bioreactor is connected to the first output end of the anaerobic digestion treatment; the first output end of the forward osmosis membrane bioreactor is connected to the first input end of the membrane distillation reactor; the circulating cooling water is input into the membrane distillation reactor through the second input end of the membrane distillation reactor; the first output end of the membrane distillation reactor is connected to the clear water tank; the second input end of the forward osmosis membrane bioreactor is connected to the second output end of the membrane distillation reactor; the output end of the clear water tank is respectively connected to the third input end of the membrane distillation reactor and the third input end of the forward osmosis membrane bioreactor; the second output end of the forward osmosis membrane bioreactor is connected to the second input end of the sludge treatment; the third output end of the forward osmosis membrane bioreactor is connected to the third input end of the anaerobic digestion treatment; the first output end of the biogas treatment is connected to the fourth input end of the membrane distillation reactor; the second output end of the biogas treatment is connected to the fourth input end of the forward osmosis membrane bioreactor.

[0007] In a possible implementation, the sludge treatment includes a bar thickener; the second output end of the forward osmosis membrane bioreactor is connected to the input end of the bar thickener, and the output end of the bar thickener is connected to the second input end of the anaerobic digestion treatment.

[0008] In a possible implementation, the anaerobic digestion treatment includes a CSTR reactor, a sedimentation tank, a homogenization regulating tank, a UASB reactor and a hydrolysis acidification tank; the first input end of the CSTR reactor is connected to the first output end of the pretreatment, and the second input end of the CSTR reactor is connected to the output end of the bar thickener; the first output end of the CSTR reactor is connected to the input end of the sedimentation tank, and the second output end of the CSTR reactor is connected to the biogas treatment; the first output end of the sedimentation tank is connected to the first input end of the homogenization regulating tank, and the output end of the homogenization regulating tank is connected to the UASB reactor. The first output end of the UASB reactor is connected to the input end of the SB reactor, the first output end of the UASB reactor is connected to the hydrolysis acidification tank, and the first output end of the hydrolysis acidification tank is connected to the first input end of the forward osmosis membrane bioreactor; the second output end of the sedimentation tank is respectively connected to the third input end of the CSTR reactor and the first input end of the sludge treatment; the second output end of the UASB reactor is connected to the first input end of the sludge treatment; the second output end of the hydrolysis acidification tank is connected to the first input end of the sludge treatment; the third output end of the forward osmosis membrane bioreactor is connected to the second input end of the homogenization regulating tank.

[0009] In a possible implementation, the winery wastewater also includes low-concentration wastewater and domestic sewage from the factory; both the low-concentration wastewater and the domestic sewage from the factory enter the pretreatment section through the second input end of the pretreatment; the second output end of the pretreatment is connected to the third input end of the homogenization regulating tank.

[0010] In a possible implementation, the third output end of the UASB reactor is connected to the input end of the biogas treatment; the third output end of the hydrolysis acidification tank is connected to the input end of the biogas treatment.

[0011] In a possible implementation, the sludge treatment also includes a sludge thickening tank and a sludge dewatering room; the second output end of the sedimentation tank, the second output end of the UASB reactor and the second output end of the hydrolysis acidification tank are all connected to the input end of the sludge thickening tank; the first output end of the sludge thickening tank is connected to the input end of the sludge dewatering room, and the first output end of the sludge dewatering room outputs stabilized sludge; the second output end of the sludge thickening tank and the second output end of the sludge dewatering room are both connected to the fourth input end of the homogenization regulating tank.

[0012] In a possible implementation, the biogas treatment includes a biogas storage cabinet, a water removal and purification device, a desulfurization purification device and a biogas utilization device; the second output end of the CSTR reactor, the third output end of the UASB reactor and the third output end of the hydrolysis acidification tank are all connected to the input end of the biogas storage cabinet; the output end of the biogas storage cabinet is connected to the input end of the water removal and purification device, and the first output end of the water removal and purification device is connected to the input end of the desulfurization purification device; the first output end of the desulfurization purification device is connected to the biogas utilization device, and the waste heat of the biogas utilization device is used for heating the feed liquid of the membrane distillation reactor; the second output end of the water removal and purification device and the second output end of the desulfurization purification device are both connected to the fourth input end of the forward osmosis membrane bioreactor.

[0013] In one possible implementation, the pretreatment includes a first grid, a second grid, a cooling tower and a water collection tank; the high-concentration wastewater and the wine lees water are input to the input end of the first grid; the output end of the first grid is connected to the input end of the cooling tower, the output end of the cooling tower is connected to the input end of the water collection tank, and the output end of the water collection tank is connected to the first input end of the CSTR reactor; the low-concentration wastewater and the factory domestic sewage are input to the input end of the second grid; the output end of the second grid is connected to the third input end of the homogenization regulating tank.

[0014] In a possible implementation, the pretreatment also includes a first sedimentation tank, a second sedimentation tank, a first neutralization tank, a second neutralization tank and a septic tank; the high-concentration wastewater is input into the input end of the first sedimentation tank, the output end of the first sedimentation tank is connected to the first input end of the first neutralization tank, and the output end of the first neutralization tank is connected to the input end of the first grid; the wine lees water is input into the input end of the second sedimentation tank, and the output end of the second sedimentation tank is connected to the second input end of the first neutralization tank; the low-concentration wastewater is input into the input end of the second neutralization tank, and the output end of the second neutralization tank is connected to the first input end of the second grid; the domestic sewage from the factory is input into the input end of the septic tank, and the output end of the septic tank is connected to the second input end of the second grid.

[0015] One or more technical solutions provided by this application have at least the following technical effects: The embodiment of the present invention adopts an energy-saving zero-discharge treatment system for brewing wastewater, including brewery wastewater, pretreatment, anaerobic digestion treatment, membrane treatment, sludge treatment and biogas treatment; the first output end of the anaerobic digestion treatment is connected to the first input end of the membrane treatment; the membrane treatment has excellent wastewater treatment effect, can ensure that the effluent water quality meets the standard, and the membrane treatment section has high integration, small footprint, and can reduce infrastructure costs; the second output end of the anaerobic digestion treatment is connected to the first input end of the sludge treatment; the first output end of the sludge treatment outputs stabilized sludge; a large amount of sludge generated by the anaerobic digestion treatment section can be used as fertilizer after sludge treatment. The output end of the membrane treatment is connected to the second input end of the sludge treatment, and the second output end of the sludge treatment is connected to the second input end of the anaerobic digestion treatment; the sludge generated by the membrane treatment section is passed into the anaerobic digestion treatment section for treatment; the third output end of the anaerobic digestion treatment is connected to the input end of the biogas treatment, and the output end of the biogas treatment is connected to the second input end of the membrane treatment. Part of the sludge generated by the anaerobic digestion treatment section is used as fertilizer after sludge treatment, and the biogas energy generated by the other part of the sludge can be used to power the membrane treatment section after passing through the biogas treatment section, thereby reducing the energy consumption of the wastewater treatment system. In addition, the remaining biogas energy can also be used for boiler heating or for power generation. The present application solves the problems of substandard water quality, large floor space and high operating energy consumption in the prior art of winery wastewater treatment, and realizes the "zero discharge" standard reuse of winery wastewater. It can not only make full use of the waste heat generated by the system itself to reduce the energy consumption in the operation stage, but also reduce the floor space of the system and increase the stability of the system. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] In order to more clearly illustrate the technical solutions of the embodiments of the present invention, the drawings required for use in the description of the embodiments of the present application will be briefly introduced below. Obviously, the drawings described below are some embodiments of the present application. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0017] Figure 1 A schematic diagram of an energy-saving brewing wastewater zero-discharge treatment system provided in an embodiment of the present application. DETAILED DESCRIPTION

[0018] The following will be combined with the drawings in the embodiments of the present application to clearly and completely describe the technical solutions in the embodiments of the present application. Obviously, the described embodiments are part of the embodiments of the present application, not all of the embodiments. Based on the embodiments in the present application, all other embodiments obtained by ordinary technicians in this field without creative work are within the scope of protection of this application.

[0019] In the description of the embodiments of the present application, it should be noted that the terms "center", "up", "down", "left", "right", "vertical", "horizontal", "inside", "outside", etc. indicate positions or positional relationships based on the positions or positional relationships shown in the accompanying drawings, which are only for the convenience of describing the embodiments of the present application and simplifying the description, and do not indicate or imply that the devices or elements referred to must have a specific orientation, be constructed and operated in a specific orientation, and therefore cannot be understood as limitations on the present application. The terms "first", "second", and "third" are used for descriptive purposes only and cannot be understood as indicating or implying relative importance. In addition, the terms "installed", "connected", and "connected" should be understood in a broad sense, for example, it can be a fixed connection, a detachable connection, or an integral connection; it can be a mechanical connection or an electrical connection; it can be a direct connection, or it can be indirectly connected through an intermediate medium, or it can be a connection between the two elements. For those of ordinary skill in the art, the specific meanings of the above terms in the embodiments of the present application can be understood according to the specific circumstances.

[0020] The embodiment of the present invention provides an energy-saving brewing wastewater zero-discharge treatment system, such as Figure 1 As shown, it includes winery wastewater, pretreatment, anaerobic digestion treatment, membrane treatment, sludge treatment and biogas treatment; the winery wastewater includes high-concentration wastewater and wine slag water; the high-concentration wastewater and wine slag water both enter the pretreatment section through the first input end of the pretreatment; the first output end of the pretreatment is connected to the first input end of the anaerobic digestion treatment, and the first output end of the anaerobic digestion treatment is connected to the first input end of the membrane treatment; the second output end of the anaerobic digestion treatment is connected to the first input end of the sludge treatment; the first output end of the sludge treatment outputs stabilized sludge; the output end of the membrane treatment is connected to the second input end of the sludge treatment, and the second output end of the sludge treatment is connected to the second input end of the anaerobic digestion treatment; the third output end of the anaerobic digestion treatment is connected to the input end of the biogas treatment, and the output end of the biogas treatment is connected to the second input end of the membrane treatment.

[0021] Exemplarily, high-concentration wastewater includes distillation bottom water and pot washing water, and wine slag water is the residue of wine fermentation.

[0022] For example, the pH value and temperature of high-concentration wastewater and distiller's grains water can be adjusted through pretreatment; part of the sludge produced in the anaerobic digestion treatment section is output as stabilized sludge after sludge treatment and can be used as fertilizer, and the biogas energy produced by the other part of the sludge can be used to power the membrane treatment section after passing through the biogas treatment section, thereby reducing the energy consumption of the wastewater treatment system. The remaining biogas energy can also be used for boiler heating or for power generation.

[0023] In the present application embodiment, Figure 1As shown, the membrane treatment includes a forward osmosis membrane bioreactor, a membrane distillation reactor and a clear water tank; the winery wastewater also includes circulating cooling water; the first input end of the forward osmosis membrane bioreactor is connected to the first output end of the anaerobic digestion treatment; the first output end of the forward osmosis membrane bioreactor is connected to the first input end of the membrane distillation reactor, and the circulating cooling water is input into the membrane distillation reactor through the second input end of the membrane distillation reactor; the first output end of the membrane distillation reactor is connected to the clear water tank; the second input end of the forward osmosis membrane bioreactor is connected to the second output end of the membrane distillation reactor; the output end of the clear water tank is respectively connected to the third input end of the membrane distillation reactor and the third input end of the forward osmosis membrane bioreactor; the second output end of the forward osmosis membrane bioreactor is connected to the second input end of the sludge treatment; the third output end of the forward osmosis membrane bioreactor is connected to the third input end of the anaerobic digestion treatment; the first output end of the biogas treatment is connected to the fourth input end of the membrane distillation reactor; the second output end of the biogas treatment is connected to the fourth input end of the forward osmosis membrane bioreactor.

[0024] Exemplarily, the forward osmosis membrane bioreactor is composed of a raw liquid, a forward osmosis membrane and an extract liquid, wherein the raw liquid is wastewater after anaerobic digestion treatment, the forward osmosis membrane is a hollow fiber polyamide composite membrane, and the initial extract liquid is a sodium chloride solution. The wastewater after anaerobic digestion treatment enters the forward osmosis membrane bioreactor by gravity for treatment. The forward osmosis membrane bioreactor is a device that can simultaneously have the interception effect of the forward osmosis membrane and the degradation effect of activated sludge; the basic working principle of the forward osmosis membrane bioreactor is that under the action of the osmotic pressure difference, the wastewater spontaneously passes through the forward osmosis membrane from the low osmotic pressure raw liquid into the high osmotic pressure extract liquid, thereby realizing the interception and decomposition of pollutants, and after being treated by the forward osmosis membrane bioreactor, a diluted extract liquid and a concentrated raw liquid can be obtained.

[0025] Exemplarily, the initial sodium chloride solution concentration is 1.5 mol / L-2 mol / L.

[0026] Exemplarily, an aeration device is provided on the feed liquid side of the forward osmosis membrane bioreactor, so as to degrade organic matter in the wastewater and remove nitrogen and phosphorus.

[0027] Exemplarily, the third output end of the forward osmosis membrane bioreactor is connected to the third input end of the anaerobic digestion treatment, so that the concentrated raw liquid can be sent back to the anaerobic digestion treatment section for further treatment, and the diluted extracted liquid can flow into the membrane distillation reactor for treatment by gravity; the residual sludge in the forward osmosis membrane bioreactor is returned to the anaerobic digestion treatment section for treatment after sludge treatment.

[0028] Exemplarily, the circulating cooling water comes from the cooling water of the wine making workshop. The system sends the diluted draw liquid and the circulating cooling water together as the feed liquid into the membrane distillation reactor for treatment. The system uses the biogas produced by the anaerobic digestion treatment section to continuously heat the feed liquid in the membrane distillation reactor, so that the temperature of the feed liquid is maintained at 45°C-50°C, thereby achieving continuous evaporation of the feed liquid. The water vapor is cooled and condensed through the hydrophobic membrane to obtain concentrated feed liquid and distillate. The concentrated feed liquid is returned to the forward osmosis membrane bioreactor to supplement the draw liquid of the forward osmosis membrane bioreactor. The draw liquid can keep the forward osmosis membrane bioreactor running continuously, and after the distillate enters the clear water tank for disinfection, a part of it can be used to clean the membrane distillation reactor and the forward osmosis membrane bioreactor, and the rest is discharged or reused.

[0029] Exemplarily, the membrane distillation reactor consists of a feed liquid, a hydrophobic membrane and a distillate, wherein the feed liquid is the diluted extract obtained from the forward osmosis membrane bioreactor, and the hydrophobic membrane is a polytetrafluoroethylene membrane; the system utilizes the distillation waste heat generated by the brewing process or the biogas generated in the anaerobic digestion treatment to continuously heat the feed liquid, so that the temperature of the feed liquid is maintained at 45°C-50°C.

[0030] In the present application embodiment, Figure 1 As shown, the sludge treatment includes a bar thickener; the second output end of the forward osmosis membrane bioreactor is connected to the input end of the bar thickener, and the output end of the bar thickener is connected to the second input end of the anaerobic digestion treatment.

[0031] Exemplarily, the excess sludge in the forward osmosis membrane bioreactor is treated by a bar thickener and then returned to the anaerobic digestion treatment section.

[0032] In the present application embodiment, Figure 1 As shown, the anaerobic digestion treatment includes a CSTR reactor, a sedimentation tank, a homogenization regulating tank, a UASB reactor and a hydrolysis acidification tank; the first input end of the CSTR reactor is connected to the first output end of the pretreatment, and the second input end of the CSTR reactor is connected to the output end of the bar thickener; the first output end of the CSTR reactor is connected to the input end of the sedimentation tank, and the second output end of the CSTR reactor is connected to the biogas treatment; the first output end of the sedimentation tank is connected to the first input end of the homogenization regulating tank, the output end of the homogenization regulating tank is connected to the input end of the UASB reactor, the first output end of the UASB reactor is connected to the hydrolysis acidification tank, and the first output end of the hydrolysis acidification tank is connected to the first input end of the forward osmosis membrane bioreactor; the second output end of the sedimentation tank is respectively connected to the third input end of the CSTR reactor and the first output end of the sludge treatment; the second output end of the UASB reactor is connected to the first input end of the sludge treatment; the second output end of the hydrolysis acidification tank is connected to the first input end of the sludge treatment; the third output end of the forward osmosis membrane bioreactor is connected to the second input end of the homogenization regulating tank.

[0033] Exemplarily, the CSTR reactor is a fully mixed anaerobic reactor. After the high-concentration wastewater and distiller's grains water are treated in the pretreatment section, they first enter the CSTR reactor for treatment. The wastewater treated by the CSTR reactor flows into the sedimentation tank by gravity for mud-water separation. The supernatant in the sedimentation tank enters the homogenization regulating tank, and part of the sludge in the sedimentation tank flows back to the CSTR reactor. The remaining sludge enters the sludge treatment section for treatment. The system can also send the biogas generated in the CSTR reactor to the biogas treatment section for temporary storage.

[0034] For example, after the water volume and water quality of high-concentration wastewater and distiller's grains water are adjusted in the homogenization regulating tank, the wastewater enters the UASB reactor for treatment. The wastewater treated in the UASB reactor enters the hydrolysis acidification tank by gravity for treatment. The remaining sludge in the UASB reactor enters the sludge treatment section for treatment, and the biogas generated in the UASB reactor is sent to the biogas treatment section for temporary storage.

[0035] For example, the temperature of the CSTR reactor is controlled at 55°C ± 2°C, and the volume load is controlled at 6 kg / (m 3 .d)-10kg / (m 3 .d); The temperature of the UASB reactor was controlled at 35℃±2℃, and the volume load was controlled at 5kg / (m 3 .d)-7kg / (m 3 .d); The hydrolysis acidification tank is an upflow hydrolysis acidification tank, the reaction temperature is 25℃±2℃, and the volume load is controlled at 2.3kg / (m 3 .d)-4.5kg / (m 3 .d); The sedimentation tank can separate the waste water from the CSTR reactor and remove the suspended solids. The sludge in the sedimentation tank is returned to the CSTR reactor at a return ratio of 150%-300%, which can replenish the bacteria lost in the CSTR reactor. Finally, the remaining sludge in the sedimentation tank enters the sludge treatment section for treatment. The surface load of the sedimentation tank is controlled at 0.6m 3 / (m 2 .h)~0.8m 3 / (m 2 .h), and the precipitation time is 2h-4h.

[0036] In the present application embodiment, Figure 1 As shown, the winery wastewater also includes low-concentration wastewater and domestic sewage in the factory area; the low-concentration wastewater and domestic sewage in the factory area both enter the pretreatment section through the second input end of the pretreatment; the second output end of the pretreatment is connected to the third input end of the homogenization regulating tank.

[0037] Exemplarily, the pretreated low-concentration wastewater and factory domestic sewage enter the homogenization regulating tank, and the supernatant in the sedimentation tank also enters the homogenization regulating tank. The pretreated low-concentration wastewater and factory domestic sewage can be mixed with the supernatant in the sedimentation tank in the homogenization regulating tank.

[0038] Exemplarily, low-concentration wastewater includes raw material soaking water, filtered water, pipeline washing water and equipment washing water; factory domestic sewage comes from bathing wastewater, canteen wastewater and toilet sewage.

[0039] In the present application embodiment, Figure 1 As shown, the third output end of the UASB reactor is connected to the input end of the biogas treatment; the third output end of the hydrolysis acidification tank is connected to the input end of the biogas treatment.

[0040] In the present application embodiment, Figure 1 As shown, the sludge treatment also includes a sludge thickening tank and a sludge dewatering room; the second output end of the sedimentation tank, the second output end of the UASB reactor and the second output end of the hydrolysis acidification tank are all connected to the input end of the sludge thickening tank; the first output end of the sludge thickening tank is connected to the input end of the sludge dewatering room, and the first output end of the sludge dewatering room outputs stabilized sludge; the second output end of the sludge thickening tank and the second output end of the sludge dewatering room are both connected to the fourth input end of the homogenization regulating tank.

[0041] Exemplarily, the residual sludge discharged from the CSTR reactor, UASB reactor and hydrolysis acidification tank is sent to the sludge thickening tank and sludge dewatering room for thickening and dehydration treatment, and then the sludge concentrate and filtrate produced in the sludge thickening tank and sludge dewatering room are sent back to the homogenization regulating tank for further treatment. Finally, the mud cake produced by the thickening and dehydration treatment is composted and dried and used as fertilizer.

[0042] In the present application embodiment, Figure 1 As shown, the biogas treatment includes a biogas storage cabinet, a water removal and purification device, a desulfurization and purification device and a biogas utilization device; the second output end of the CSTR reactor, the third output end of the UASB reactor and the third output end of the hydrolysis and acidification tank are all connected to the input end of the biogas storage cabinet; the output end of the biogas storage cabinet is connected to the input end of the water removal and purification device, and the first output end of the water removal and purification device is connected to the input end of the desulfurization and purification device; the first output end of the desulfurization and purification device is connected to the biogas utilization device, and the waste heat of the biogas utilization device is used for heating the feed liquid of the membrane distillation reactor; the second output end of the water removal and purification device and the second output end of the desulfurization and purification device are both connected to the fourth input end of the forward osmosis membrane bioreactor.

[0043] Exemplarily, the biogas produced in the CSTR reactor, the UASB reactor and the hydrolysis acidification tank are all sent to a biogas storage cabinet for temporary storage.

[0044] Exemplarily, as needed, the biogas temporarily stored in the biogas storage cabinet is sent to a water removal purification device and a desulfurization purification device for treatment. The biogas utilization device includes a boiler. Specifically, the treated biogas can be used for boiler heating or for power generation. The wastewater generated in the water removal purification device and the desulfurization purification device is sent to a forward osmosis membrane bioreactor for treatment.

[0045] In the present application embodiment, Figure 1 As shown, the pretreatment includes a first grid, a second grid, a cooling tower and a water collection tank; high-concentration wastewater and wine lees water are input to the input end of the first grid; the output end of the first grid is connected to the input end of the cooling tower, the output end of the cooling tower is connected to the input end of the water collection tank, and the output end of the water collection tank is connected to the first input end of the CSTR reactor; low-concentration wastewater and factory domestic sewage are input to the input end of the second grid; the output end of the second grid is connected to the third input end of the homogenization regulating tank.

[0046] In the present application embodiment, Figure 1 As shown, the pretreatment also includes a first sedimentation tank, a second sedimentation tank, a first neutralization tank, a second neutralization tank and a septic tank; high-concentration wastewater is input into the input end of the first sedimentation tank, the output end of the first sedimentation tank is connected to the first input end of the first neutralization tank, and the output end of the first neutralization tank is connected to the input end of the first grid; wine slag water is input into the input end of the second sedimentation tank, and the output end of the second sedimentation tank is connected to the second input end of the first neutralization tank; low-concentration wastewater is input into the input end of the second neutralization tank, and the output end of the second neutralization tank is connected to the first input end of the second grid; domestic sewage from the factory is input into the input end of the septic tank, and the output end of the septic tank is connected to the second input end of the second grid.

[0047] Exemplarily, high-concentration wastewater is first sent to the first primary sedimentation tank for treatment, and the supernatant of the first primary sedimentation tank enters the first neutralization tank. Alkali solution is added in the first neutralization tank to adjust the pH value of the wastewater to 6.5-8. The alkali solution is sodium hydroxide or quicklime. The wastewater is then passed into the first grid, which can remove larger floating objects in the wastewater. The wastewater is then passed into a cooling tower, which can adjust the temperature of the wastewater to 45°C-55°C. The wastewater is then passed into a collection tank to adjust the water volume.

[0048] Exemplarily, after the wine slag water is precipitated in the second primary sedimentation tank, it enters the first neutralization tank to adjust the pH value, and the wine slag water is mixed with high-concentration wastewater in the first neutralization tank; the remaining residue in the second primary sedimentation tank is used as feed or fertilizer.

[0049] Exemplarily, low-concentration wastewater is sent to the second neutralization tank, where the pH value is adjusted to 6.5-8 by adding alkali solution, and then the wastewater is passed into the second grid, which is used to remove large suspended particles and floating materials in the wastewater. The wastewater treated by the second grid is passed into the homogenization adjustment tank for treatment.

[0050] For example, after the domestic sewage from the factory is treated in the septic tank, it is passed into the second screen for treatment. The second screen can remove large suspended particles and floating materials in the wastewater. The domestic sewage from the factory is mixed with low-concentration wastewater and then passed into the homogenization regulating tank for treatment.

[0051] The embodiment of the present invention provides an energy-saving zero-discharge treatment system for brewing wastewater. Taking the wastewater treatment of a domestic winery as an example, the treatment system of the present invention is used to treat the wastewater of the winery: The inlet and outlet water quality concentrations of the key water quality indicators of the winery's wastewater are shown in the following table.

[0052]

[0053] It should be noted that, except for pH, all units in the table are mg / L.

[0054] 1. Pretreatment of high-concentration wastewater: The high-concentration wastewater is sent to the first primary sedimentation tank, the supernatant of the first primary sedimentation tank enters the first neutralization tank and 5% lime milk solution is added to the first neutralization tank to adjust the pH value of the wastewater in the first neutralization tank to 8. The wastewater in the first neutralization tank then enters the first grid to remove larger floating objects, and then the wastewater is sent to the cooling tower by the outlet water lifting pump of the first grid. The temperature of the wastewater after treatment in the cooling tower is controlled at 55°C, and then the wastewater is passed into the collection tank to adjust the water volume.

[0055] 2. Pretreatment of wine slag water: After the wine slag water is precipitated in the second primary sedimentation tank, the wastewater is input into the first neutralization tank and mixed with the high-concentration wastewater; among them, the residue in the second primary sedimentation tank can be used as feed.

[0056] 3. Pretreatment of low-concentration wastewater: The low-concentration wastewater is sent to the second neutralization tank and 5% lime milk solution is added to the second neutralization tank to adjust the pH value of the second neutralization tank to 8. The wastewater in the second neutralization tank then enters the second grid to remove large suspended particles and floating materials, and then the outlet pump of the second grid is used to send the wastewater to the homogenization regulating tank for subsequent treatment.

[0057] 4. Pretreatment of domestic sewage in factory area: The domestic sewage from the factory is treated in the septic tank and then sent to the second screen. The second screen is used to remove large suspended particles and floating materials in the wastewater. The wastewater treated by the second screen is mixed with the low-concentration wastewater and then sent into the homogenization regulating tank for subsequent treatment.

[0058] 5. Anaerobic digestion treatment: After the high-concentration wastewater and wine dregs water are adjusted in the water collection tank, they first enter the CSTR reactor for treatment. The temperature of the CSTR reactor is controlled at 55°C and its volume load is controlled at 8kg / (m 3 ·d) Significantly reduce the concentration of COD and BOD5 in the CSTR reactor.

[0059] The wastewater output from the CSTR reactor flows into the sedimentation tank by gravity for mud-water separation. The supernatant in the sedimentation tank enters the homogenization regulating tank and is mixed with the pre-treated low-concentration wastewater and domestic sewage in the plant area. The precipitated sludge in the sedimentation tank is transported to the CSTR reactor at a return ratio of 200%, and the remaining sludge in the sedimentation tank enters the sludge thickening tank. The surface load of the sedimentation tank is 0.7m 3 / (m 2 .h), the residence time is 4h, and the biogas produced in the CSTR reactor is sent to the biogas storage cabinet for temporary storage.

[0060] After the pre-treatment, the high-concentration wastewater, wine dregs water, low-concentration wastewater and domestic sewage in the factory area are adjusted in water quantity and quality in the homogenization regulating tank, and then enter the UASB reactor for treatment. The temperature of the UASB reactor is 35℃, and its volume load is 6kg / (m 3 .d) The concentration of COD and BOD5 in the wastewater can be further reduced in the UASB reactor. The wastewater output from the UASB reactor enters the upflow hydrolysis acidification tank for treatment by gravity, the residual sludge from the UASB reactor enters the sludge concentration tank for subsequent treatment, and the biogas generated in the UASB reactor is sent to the biogas storage cabinet for temporary storage.

[0061] It should be noted that the wastewater is treated by an upflow hydrolysis acidification tank, which can decompose the refractory substances. The reaction temperature of the upflow hydrolysis acidification tank is 25°C and its volume load is 3.0kg / (m 3 .d), the wastewater output from the hydrolysis and acidification tank enters the membrane treatment section for treatment, and the remaining sludge is discharged into the sludge concentration tank for subsequent treatment, and the biogas produced in the upflow hydrolysis and acidification tank is sent to the biogas storage cabinet for temporary storage.

[0062] 6. Membrane treatment: After anaerobic digestion treatment, the wastewater enters the forward osmosis membrane bioreactor for treatment as the raw liquid by gravity. The water quality of the wastewater output after treatment by the forward osmosis membrane bioreactor is as follows: SS≤50mg / L, COD≤100mg / L, BOD5≤30mg / L, NH3-N≤20mg / L, TP≤1mg / L.

[0063] The forward osmosis membrane bioreactor consists of a raw liquid, a forward osmosis membrane and an extract liquid. The raw liquid is wastewater after anaerobic digestion, the forward osmosis membrane is a hollow fiber polyamide composite membrane, the initial extract liquid is a 2 mol / L sodium chloride solution, and an aeration stirring device is provided on the raw liquid side. The aeration intensity is 3m 3 / (m 2 .h), so that the organic matter in the wastewater can be degraded and nitrogen and phosphorus can be removed. After the forward osmosis membrane bioreactor is treated, a diluted draw liquid and a concentrated raw material liquid can be obtained; the concentrated raw material liquid is sent back to the homogenization regulating tank for further treatment, and the diluted draw liquid can flow into the membrane distillation reactor by gravity for treatment. The residual sludge discharged from the forward osmosis membrane bioreactor is concentrated by the bar concentrator and then returned to the CSTR reactor for anaerobic digestion treatment.

[0064] The diluted draw liquid and circulating cooling water are sent to the membrane distillation reactor as feed liquid for further treatment. The quality of the wastewater output after treatment by the membrane distillation reactor is as follows: SS≤30mg / L, COD≤50mg / L, BOD5≤10mg / L, NH3-N≤5mg / L, TP≤0.2mg / L.

[0065] The membrane distillation reactor consists of a feed liquid, a hydrophobic membrane and a distillate, wherein the feed liquid is the diluted draw liquid obtained from the forward osmosis membrane bioreactor, and the hydrophobic membrane is a polytetrafluoroethylene membrane. It should be noted that the temperature of the feed liquid is maintained at 45°C.

[0066] After being treated in the membrane distillation reactor, a distillate and a concentrated feed liquid are obtained, wherein the concentrated feed liquid is returned to the forward osmosis membrane bioreactor to supplement the draw liquid required by the forward osmosis membrane bioreactor, and the distillate enters the clean water tank and is disinfected with liquid chlorine. A part of it is used to clean the forward osmosis membrane bioreactor and the membrane distillation reactor, and the rest is discharged or reused.

[0067] 7. Sludge treatment: The residual sludge discharged from the CSTR reactor, UASB reactor and hydrolysis acidification tank is sent to the sludge thickening tank and sludge dewatering room for thickening and dehydration treatment, and then the sludge concentrate and filtrate produced in the sludge thickening tank and sludge dewatering room are sent back to the homogenization regulating tank for further treatment. Finally, the mud cake produced by the thickening and dehydration treatment is composted and dried and used as fertilizer.

[0068] It should be noted that the sludge thickening tank is a gravity sludge thickening tank with a sludge solid load of 40kg / (m 2 .d), the concentration time is 12h, a plate and frame filter press is installed in the sludge dewatering room, the sludge dewatering load is 200kg / (mh), and ventilation facilities are installed in the sludge dewatering room, and the ventilation frequency can be 8 times / h.

[0069] The residual sludge discharged from the forward osmosis membrane bioreactor is concentrated by the bar concentrator and then returned to the CSTR reactor for anaerobic digestion treatment.

[0070] 8. Biogas treatment: The biogas in the biogas storage cabinet is sent to a water removal purification device and a desulfurization purification device for treatment. The treated biogas is used for boiler heating or for power generation; and the wastewater generated in the water removal purification device and the desulfurization purification device is sent to a forward osmosis membrane bioreactor for treatment.

[0071] This application aims at the characteristics of winery wastewater and can combine different treatment processes to make the entire wastewater treatment system scientific and reasonable with a compact structure. The treatment system of this application can achieve zero discharge of winery wastewater, and the wastewater treatment system achieves "zero discharge" and meets the reuse standards, which can not only reduce the amount of external water in the entire treatment system, but also increase the stability of the wastewater treatment system, which is a significant improvement.

[0072] Furthermore, the present invention adopts a membrane treatment method of a forward osmosis membrane bioreactor and a membrane distillation reactor, wherein the forward osmosis membrane bioreactor does not need to be driven by an external pressure, thereby reducing the energy consumption of the wastewater treatment system, and the treatment method of the forward osmosis membrane bioreactor and the membrane distillation reactor has a good wastewater treatment effect, which can ensure that the effluent water quality meets the standard. Since the membrane treatment section has a high degree of integration and a small footprint, the capital construction cost of the wastewater treatment system can be reduced.

[0073] The present application also avoids the treatment costs caused by the large amount of sludge generated by the wastewater treatment system and avoids secondary pollution to the environment. The sludge generated by the present application can be used as fertilizer after stabilization treatment.

[0074] The present application makes full use of the waste heat from the plant and the biogas energy generated during the treatment process to power the membrane treatment section, thereby avoiding energy waste, and the membrane treatment section does not require external drive, thereby reducing the energy consumption of the wastewater treatment system.

[0075] The various embodiments in this specification are described in a progressive manner, and the same or similar parts between the various embodiments can be referenced to each other. Each embodiment focuses on the differences from other embodiments.

[0076] The above embodiments are only used to illustrate the technical solutions of the present application, rather than to limit the present application. Although the present application has been described in detail with reference to the aforementioned embodiments, a person of ordinary skill in the art should understand that the technical solutions described in the aforementioned embodiments may still be modified, or some or all of the technical features thereof may be replaced by equivalents. However, these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the present application.

Claims

1. An energy-saving brewing wastewater zero-discharge treatment system, characterized in that: Including winery wastewater, pretreatment, anaerobic digestion, membrane treatment, sludge treatment and biogas treatment; The winery wastewater includes high-concentration wastewater and wine tank slag water; The high-concentration wastewater and the wine lees water both enter the pretreatment section through the first input end of the pretreatment; The first output end of the pretreatment is connected to the first input end of the anaerobic digestion treatment, and the first output end of the anaerobic digestion treatment is connected to the first input end of the membrane treatment; The second output end of the anaerobic digestion treatment is connected to the first input end of the sludge treatment; The first output end of the sludge treatment outputs stabilized sludge; The output end of the membrane treatment is connected to the second input end of the sludge treatment, and the second output end of the sludge treatment is connected to the second input end of the anaerobic digestion treatment; The third output end of the anaerobic digestion treatment is connected to the input end of the biogas treatment, and the output end of the biogas treatment is connected to the second input end of the membrane treatment.

2. The energy-saving brewing wastewater zero-discharge treatment system according to claim 1 is characterized in that: The membrane treatment includes a forward osmosis membrane bioreactor, a membrane distillation reactor and a clear water tank; The winery wastewater also includes circulating cooling water; The first input end of the forward osmosis membrane bioreactor is connected to the first output end of the anaerobic digestion treatment; the first output end of the forward osmosis membrane bioreactor is connected to the first input end of the membrane distillation reactor; The circulating cooling water is input into the membrane distillation reactor through the second input end of the membrane distillation reactor; the first output end of the membrane distillation reactor is connected to the clean water tank; The second input end of the forward osmosis membrane bioreactor is connected to the second output end of the membrane distillation reactor; The output end of the clear water tank is connected to the third input end of the membrane distillation reactor and the third input end of the forward osmosis membrane bioreactor respectively; The second output end of the forward osmosis membrane bioreactor is connected to the second input end of the sludge treatment; The third output end of the forward osmosis membrane bioreactor is connected to the third input end of the anaerobic digestion process; The first output end of the biogas treatment is connected to the fourth input end of the membrane distillation reactor; The second output end of the biogas treatment is connected to the fourth input end of the forward osmosis membrane bioreactor.

3. The energy-saving brewing wastewater zero-discharge treatment system according to claim 2 is characterized in that: The sludge treatment includes a bar thickener; The second output end of the forward osmosis membrane bioreactor is connected to the input end of the bar concentrator, and the output end of the bar concentrator is connected to the second input end of the anaerobic digestion treatment.

4. The energy-saving brewing wastewater zero-discharge treatment system according to claim 3 is characterized in that: The anaerobic digestion treatment includes a CSTR reactor, a sedimentation tank, a homogenization regulating tank, a UASB reactor and a hydrolysis acidification tank; The first input end of the CSTR reactor is connected to the first output end of the pretreatment, and the second input end of the CSTR reactor is connected to the output end of the grid thickener; The first output end of the CSTR reactor is connected to the input end of the sedimentation tank, and the second output end of the CSTR reactor is connected to the biogas treatment; The first output end of the sedimentation tank is connected to the first input end of the homogenization regulating tank, the output end of the homogenization regulating tank is connected to the input end of the UASB reactor, the first output end of the UASB reactor is connected to the hydrolysis acidification tank, and the first output end of the hydrolysis acidification tank is connected to the first input end of the forward osmosis membrane bioreactor; The second output end of the sedimentation tank is connected to the third input end of the CSTR reactor and the first input end of the sludge treatment respectively; The second output end of the UASB reactor is connected to the first input end of the sludge treatment; The second output end of the hydrolysis acidification tank is connected to the first input end of the sludge treatment; The third output end of the forward osmosis membrane bioreactor is connected to the second input end of the homogenization regulating tank.

5. The energy-saving brewing wastewater zero-discharge treatment system according to claim 4 is characterized in that: The winery wastewater also includes low-concentration wastewater and domestic sewage in the factory area; The low-concentration wastewater and the factory domestic sewage both enter the pretreatment section through the second input end of the pretreatment; The second output end of the pretreatment is connected to the third input end of the homogeneous regulating tank.

6. The energy-saving brewing wastewater zero-discharge treatment system according to claim 4 is characterized in that: The third output end of the UASB reactor is connected to the input end of the biogas treatment; The third output end of the hydrolysis acidification tank is connected to the input end of the biogas treatment.

7. The energy-saving brewing wastewater zero-discharge treatment system according to claim 4 is characterized in that: The sludge treatment also includes a sludge thickening tank and a sludge dewatering room; The second output end of the sedimentation tank, the second output end of the UASB reactor and the second output end of the hydrolysis acidification tank are all connected to the input end of the sludge thickening tank; The first output end of the sludge thickening tank is connected to the input end of the sludge dewatering room, and the first output end of the sludge dewatering room outputs stabilized sludge; The second output end of the sludge thickening tank and the second output end of the sludge dehydration room are both connected to the fourth input end of the homogenization regulating tank.

8. The energy-saving zero-discharge treatment system for brewing wastewater according to claim 4 is characterized in that: The biogas treatment includes a biogas storage cabinet, a water removal and purification device, a desulfurization and purification device, and a biogas utilization device; The second output end of the CSTR reactor, the third output end of the UASB reactor and the third output end of the hydrolysis acidification tank are all connected to the input end of the biogas storage cabinet; The output end of the biogas storage cabinet is connected to the input end of the water removal and purification device, and the first output end of the water removal and purification device is connected to the input end of the desulfurization purification device; The first output end of the desulfurization purification device is connected to the biogas utilization device; the waste heat of the biogas utilization device is used to heat the feed liquid in the membrane distillation reactor; The second output end of the water removal purification device and the second output end of the desulfurization purification device are both connected to the fourth input end of the forward osmosis membrane bioreactor.

9. The energy-saving brewing wastewater zero-discharge treatment system according to claim 5 is characterized in that: The pretreatment includes a first grid, a second grid, a cooling tower and a water collection tank; The high-concentration wastewater and the wine lees water are input into the input end of the first grid; The output end of the first grid is connected to the input end of the cooling tower, the output end of the cooling tower is connected to the input end of the water collection tank, and the output end of the water collection tank is connected to the first input end of the CSTR reactor; The input end of the second grid inputs the low-concentration wastewater and the factory domestic sewage; The output end of the second grid is connected to the third input end of the homogeneous regulating tank.

10. The energy-saving brewing wastewater zero-discharge treatment system according to claim 9 is characterized in that: The pretreatment also includes a first sedimentation tank, a second sedimentation tank, a first neutralization tank, a second neutralization tank and a septic tank; The high-concentration wastewater is input into the input end of the first sedimentation tank, the output end of the first sedimentation tank is connected to the first input end of the first neutralization tank, and the output end of the first neutralization tank is connected to the input end of the first grid; The wine tank slag water is input into the input end of the second sedimentation tank, and the output end of the second sedimentation tank is connected to the second input end of the first neutralization tank; The low-concentration wastewater is input into the input end of the second neutralization tank, and the output end of the second neutralization tank is connected to the first input end of the second grid; The domestic sewage from the factory is input into the input end of the septic tank, and the output end of the septic tank is connected to the second input end of the second grid.

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