CN108083579B - Modular integrated system and process for treating non-fermented soybean product production wastewater - Google Patents
Modular integrated system and process for treating non-fermented soybean product production wastewater Download PDFInfo
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Abstract
本发明涉及一种处理非发酵类豆制品生产废水的模块化集成系统及工艺，包括一级预处理模块、二级生化模块和三级深度处理模块，一级预处理模块设置细网格筛和气浮隔油沉淀调节水池，去除悬浮物、浮油和调节水量水质；二级生化模块设置厌氧单元和好氧单元，去除废水中主要污染物；三级深度处理模块设置微砂沉淀池、活性砂滤池、动态膜过滤系统和紫外线消毒反应器，去除SS和消毒。针对高浓度非发酵类豆制品生产废水，进行工艺集成与参数化设计，根据进水水质条件，选择运行不同单元。本发明工艺具有灵活、高效、便捷、智能等特点，能够保证废水处理设施经济、有效、稳定的运行。
The invention relates to a modularized integrated system and process for treating non-fermented soybean product production wastewater, comprising a first-stage pretreatment module, a second-stage biochemical module and a third-stage advanced treatment module. The first-stage pretreatment module is provided with a fine mesh screen and a gas filter. Floating oil separation sedimentation adjustment tank to remove suspended solids, oil slick and adjust water quality and water quality; the secondary biochemical module is equipped with anaerobic unit and aerobic unit to remove major pollutants in wastewater; Sand filters, dynamic membrane filtration systems and UV disinfection reactors for SS removal and disinfection. For high-concentration non-fermented soybean product production wastewater, process integration and parametric design are carried out, and different units are selected to operate according to the water quality conditions. The process of the invention has the characteristics of flexibility, high efficiency, convenience, intelligence and the like, and can ensure the economical, effective and stable operation of the wastewater treatment facility.
Description
Technical Field
The invention relates to the technical field of integrated treatment of high-concentration organic wastewater, in particular to a modular integrated system and a process for treating non-fermented bean product production wastewater.
Background
In recent years, the bean product industry in China develops rapidly, a large number of enterprises for producing and processing bean products are developed, and the existing workshop-type production mode is changed. By 2010, more than 2000 bean product processing enterprises in China, 117 enterprises with daily processing capacity of 500t/d and 12 enterprises with annual processing capacity of 180 ten thousand tons worldwide occupy 6 China.
The bean products are mainly divided into two main types, one is a fermented bean product, and the other is a non-fermented bean product. The fermented bean product is prepared from soybean by microbial fermentation, such as soy sauce, fermented bean curd, semen Sojae Preparatum, and bean cotyledon. The non-fermented bean product is prepared from soybean and other mixed beans by a certain process, such as bean curd, soybean milk, etc.
A production process of non-fermented bean products takes bean curd as an example and comprises the following steps: the method comprises the steps of primary selection, washing, soaking, grinding, boiling, brine adding, filter pressing and finishing. Wherein waste water is generated after water washing and filter pressing. The non-fermented bean product wastewater is high-concentration organic wastewater, contains a large amount of protein, fat, starch and other organic matters, and has higher COD value and BOD value and higher total nitrogen and ammonia nitrogen. The yellow slurry discharged in the processing process has a solid content of more than 1%, wherein the protein content is about 0.3%, the fat content is about 0.08%, and the reducing sugar content is about 0.15%. In addition, the wastewater also contains various functional components such as soybean isoflavone, soyasaponin and the like, and most enterprises in China directly discharge the soybean milk at present, so that resources are wasted, the environment is polluted, and the soybean milk is not beneficial to clean production and increase of the processing additional value of soybeans.
The treatment of bean product wastewater is studied from 60 s in the 20 th century abroad and applied to engineering practice, and China also starts a great deal of research and application to practice in the 70 th. The treatment of bean product wastewater can be divided into three methods, namely an anaerobic biological treatment method, an aerobic biological treatment method and an anaerobic-aerobic combined treatment process. Among them, anaerobic bioprocess is most studied and applied. The anaerobic treatment process mainly adopted comprises the following steps: AB (anaerobic filter bed) process, UASB (upflow anaerobic sludge blanket) process, AFB (anaerobic fluidized bed) feeding process, ABR (anaerobic baffled reactor) process, two-phase anaerobic treatment process and the like. However, the effluent after anaerobic treatment needs to be supplemented with aerobic treatment to meet the discharge standard. The aerobic treatment process mainly adopted comprises an AB method, a traditional activated sludge method, an SBR (sequencing batch reactor) method and an MBR (membrane bioreactor) method. At present, the treatment process applied to the non-fermented bean product wastewater has various types and achieves certain effect, but the following problems exist:
(1) current water treatment systems are difficult to accommodate for particularly large variations in water volume. The waste water produced by the non-fermented bean products has obvious seasonal characteristics, namely light and strong seasons, and some factories stop production in the light seasons, so that the discharge amount of the waste water produced by the non-fermented bean products is greatly changed in one year; the treatment system adopted at present is basically designed according to the average water quantity or the maximum water quantity, and the design has the consequence that when the water quantity is low, the load of the system is insufficient, so that a great amount of microorganisms die; when the water quantity is high, the system load is too high, and the effluent quality does not reach the standard.
(2) The current water treatment system is difficult to adapt to the condition of large water quality change. The quality of the wastewater produced by non-fermented bean products is different due to different production and processing technologies, and even in the same enterprise, the quality of the wastewater in different processing stages is also very different. Sometimes the COD of the waste water is in the range of 1500-3000, sometimes up to 8000-20000. Therefore, in the design, the same set of system is generally adopted to treat wastewater with greatly changed water quality, and the obvious change of the water quality can generate impact load on a sewage treatment system, so that the system becomes unstable, and the effluent index also becomes poor.
(3) Seasonal wastewater impacts an anaerobic system, and burdens enterprises. The non-fermented soybean product production wastewater is typical organic wastewater, an anaerobic and aerobic combined treatment system is adopted in a general biochemical stage, but the non-fermented soybean product production wastewater has seasonal characteristics, the anaerobic system is greatly influenced under the condition of no water in winter, anaerobic bacteria can be completely killed, the anaerobic system needs to be restarted in the next year, and the treatment burden of an enterprise is increased.
(4) The resource recovery utilization rate is low. The bean product wastewater contains carbon, nitrogen, phosphorus and trace metal elements required by the production of the oxidized yeast. The yeast can completely decompose the saccharide into carbon dioxide and water under the condition of sufficient oxygen, and simultaneously produce a large amount of protein-containing mycelium which can be recovered as feed protein. When the bean product wastewater is treated by an anaerobic method, 0.6-0.8 m can be obtained every time 1kgCOD is removed3The marsh gas can be used for power generation or fuel gas after being processed. However, in the currently adopted treatment process, the treatment of water is mainly regarded as important, and the recycling rate of the part of resources is very low.
Therefore, the invention provides a modularized integrated process, aiming at the characteristics of non-fermented bean product production wastewater and the problems of the existing treatment system, the invention provides an advanced treatment process with excellent screening effect, energy conservation and consumption reduction, and the process coupling integration and the parametric design are carried out to realize the process modularization, the intellectualization and the integration.
Disclosure of Invention
In order to solve the technical problems, the invention provides a modular integrated process method for treating non-fermentation bean product production wastewater, which comprises a primary pretreatment module, a secondary biochemical module and a tertiary advanced treatment module, wherein the primary pretreatment module is provided with a fine mesh sieve and an air floatation oil separation precipitation regulating water tank for removing suspended matters, floating oil and regulating water quantity and water quality; the secondary biochemical module is provided with an anaerobic unit and an aerobic unit to remove main pollutants in the wastewater; the three-stage advanced treatment module is provided with a micro-sand sedimentation tank, an active sand filter, a dynamic membrane filtration system and an ultraviolet disinfection reactor, and is used for removing SS and disinfecting. Aiming at the high-concentration non-fermented bean product production wastewater, process integration and parametric design are carried out, and different units are selected to operate according to the water quality condition of inlet water. The process has the characteristics of flexibility, high efficiency, convenience, intelligence and the like, and can ensure economic, effective and stable operation of wastewater treatment facilities.
According to the characteristics of the production wastewater and the requirements of the wastewater treatment process, and the principles of mature and reliable technology, stable operation, convenient maintenance and management and economic applicability are adhered to, the non-fermented bean product production wastewater treatment process is optimized and integrated, and a set of operation method suitable for different water quality is developed. The bean product wastewater is wastewater with high organic matter content, the BOD/COD ratio is up to 0.55-0.65, and the C, N, P ratio is 100:4.7: 0.2. The pH value is low, and the waste water basically does not contain toxic and harmful substances. Therefore, the bean product wastewater is suitable for being treated by a biological method.
The specific technical scheme is as follows:
the modularized integrated system for treating the non-fermented bean product production wastewater comprises a primary pretreatment module, a secondary biochemical module and a tertiary advanced treatment module; the primary pretreatment module is provided with a fine mesh sieve and an air floatation oil removal sedimentation regulating water tank; the secondary biochemical module is provided with an anaerobic unit and an aerobic unit, the anaerobic unit comprises an anaerobic fluidized bed reactor and an anaerobic continuous stirring reactor, and the aerobic unit comprises a biological contact oxidation reactor and an anoxic-aerobic aeration biological filter reactor; the three-stage advanced treatment module is provided with a micro-sand sedimentation tank, an active sand filter, a dynamic membrane filtration system and an ultraviolet disinfection reactor.
The inlet of the fine mesh sieve of the primary pretreatment module is connected with a non-fermentation bean product production wastewater inlet, and the outlet of the fine mesh sieve of the primary pretreatment module is connected with the inlet of the air floatation oil separation sedimentation regulating water tank; the outlet of the air floatation oil separation sedimentation adjusting water tank is connected with the inlet of the secondary biochemical module;
an anaerobic unit inlet of the second-stage biochemical module is connected with an outlet of the first-stage pretreatment module air floatation oil separation sedimentation regulating water tank; the inlet of the anaerobic fluidized bed is connected with the inlet of the anaerobic unit, the outlet of the anaerobic fluidized bed is connected with the outlet of the anaerobic unit, the inlet of the anaerobic continuous stirring reactor is connected with the inlet of the anaerobic unit, and the outlet of the anaerobic continuous stirring reactor is connected with the outlet of the anaerobic unit; the outlet of the anaerobic unit is connected with the inlet of the aerobic unit; the outlet of the aerobic unit is connected with the inlet of the three-stage advanced treatment module, the inlet of the biological contact oxidation reactor is connected with the inlet of the aerobic unit, the outlet of the biological contact oxidation reactor is connected with the outlet of the aerobic unit, the inlet of the anoxic-aerobic biological aerated filter is connected with the inlet of the aerobic unit, and the outlet of the anoxic-aerobic biological aerated filter is connected with the outlet of the aerobic unit;
the inlet of the micro-sand sedimentation tank of the three-level advanced treatment module is connected with the outlet of the secondary biochemical treatment module, and the outlet of the micro-sand sedimentation tank is connected with the inlet of the active sand filter; the outlet of the active sand filter is connected to the inlet of the dynamic membrane filtration system; the outlet of the dynamic membrane filtration system is connected with the inlet of the ultraviolet disinfection reactor; the outlet of the ultraviolet disinfection reactor is connected to the main outlet of the water treatment system;
a monitoring device and an electric valve are arranged in front of inlets of the anaerobic fluidized bed reactor, the anaerobic continuous stirring reactor, the biological contact oxidation reactor, the anoxic-aerobic biological aerated filter and the dynamic membrane filtration system, and different units are automatically selected to operate according to the operating water quality condition;
the modular integrated process for treating the non-fermented bean product production wastewater comprises the following steps:
(1) starting and operating a primary pretreatment module, introducing non-fermentation bean product production wastewater into a total sewage treatment system, and removing larger substances in the wastewater through a fine mesh sieve;
(2) starting an air floatation oil separation precipitation adjusting water tank, removing oil and suspended matters in water and adjusting water quality and water quantity;
(3) on-line monitoring and analyzing COD value of wastewater in air floatation oil removal precipitation regulation pool, and combining actual water quantity QFruit of Chinese wolfberryAnd the design water quantity QIs provided withSelecting different operation units according to the relation;
(4) when Q isFruit of Chinese wolfberry≥1/2QIs provided withAnd when the COD is more than or equal to 2000mg/L, the step (5) is operated, otherwise, the step (6) is operated;
(5) starting the anaerobic continuous stirring reactor to remove pollutants in water, and operating the step (7);
(6) starting the anaerobic fluidized bed reactor to remove pollutants in water;
(7) monitoring and analyzing the COD value, BOD value and ammonia nitrogen value of the effluent of the anaerobic unit on line, entering the step (8) when the COD is more than 500mg/L, or the BOD is more than 300mg/L, or the ammonia nitrogen is more than 40mg/L, and entering the step (10) if not;
(8) starting the anoxic-aerobic biological aerated filter to remove pollutants in water;
(9) monitoring and analyzing the COD value, BOD value and ammonia nitrogen value of the effluent of the anaerobic fluidized bed reactor on line, entering the step (10) when the COD is more than 100mg/L, or the BOD is more than 30mg/L, or the ammonia nitrogen is more than 15mg/L, and entering the step (11) if not;
(10) starting a biological contact oxidation reactor to remove pollutants in water;
(11) starting a micro-sand sedimentation tank, and carrying out sedimentation and sludge discharge on the wastewater;
(12) starting the active sand filter to filter the wastewater;
(13) according to the requirement of the effluent quality, when the SS of the effluent quality is less than 15mg/L, the step (14) is carried out, otherwise, the step (15) is carried out;
(14) starting a dynamic membrane filtration system to filter the wastewater;
(15) starting the ultraviolet disinfection reactor to disinfect the wastewater.
The design grid size of the fine grid sieve adopts 10 mm; in the air flotation oil separation sedimentation regulating water tank, the designed retention time of a reaction zone of an air flotation zone is 5min, the designed flow velocity of a contact chamber of the air flotation zone is 0.05m/s, the designed retention time of the contact chamber is 2min, and the surface load of a separation chamber of the air flotation zone is 6-8 m3/(m2H); in the oil separation area, a 2-stage oil separation lower baffle, a 1-stage oil separation upper baffle and 1 floater oil skimmer are designed, and the floater oil skimmer is arranged in front of the oil separation upper baffle; the settling zone comprises 2-4 sediment hoppers and 1 set of a slag discharge system; the designed retention time of the regulating pool is 12-24 h.
The design load of the anaerobic fluidized bed reactor is 5-8 kgCOD/(m)3D), designing the maximum ascending flow velocity to be 8-10 m/h; the anaerobic continuous stirred reactor is designed to have a residence time of 20 d; the BOD load of the biological contact oxidation reactor is 1.5 kg/(m)3D); in the anoxic-aerobic biological aerated filter reactor, the retention time of an anoxic zone is 3h, the reflux ratio of nitrifying liquid is 200%, and the BOD load is 1.8-2.0 kgBOD/(m)3·d)。
The design surface load of the micro-sand sedimentation tank is 10-14 m3/(m2H); the average filtering speed of the active sand filter is designed to be 6 m/h; the dynamic membrane filtration system is designed to have a filtration speed of 12-15 m/h; the film forming material comprises a nylon screen, a terylene non-woven fabric and diatomite, wherein the nylon screen is 1cm x 1cm in size, the designed mesh size is 10 meshes, the terylene non-woven fabric is 1cm x 1cm in size, and the unit area mass is 250-300 g/m2The designed permeability of the diatomite is 0.15-0.25 Darcy, and the mass ratio of the nylon screen mesh, the polyester non-woven fabric and the diatomite is 10:1: 5.
The method has the advantages that:
(1) the method is suitable for treating high-concentration wastewater in a non-fermentation bean product production field with large water quality and water quantity change; can solve the technical problem that the waste water of the non-fermented bean product production has seasonal characteristics.
(2) The invention adopts a plurality of units in series connection, automatically controls the conversion process by changing the operation parameters of the equipment, can adapt to a system with larger change of water quality and water quantity, and simultaneously saves the operation energy consumption and cost; the floor area is saved to the maximum extent, and meanwhile, the manufacturing cost is saved; the process combination has high modularization degree, is beneficial to the technology to be converted into integrated equipment, and saves space; the process combination technology is advanced and stable and reaches the standard.
(3) In the primary pretreatment module, a fine mesh screen is arranged at the inlet of an air floatation oil separation precipitation regulating water tank and is used for removing suspended matters which possibly block a water pump unit and pipeline valves and ensuring that subsequent treatment facilities can normally run; the air floatation oil removal precipitation adjusting water tank has the functions of removing oil, removing suspended matters and adjusting water quality and water quantity.
(4) The anaerobic unit in the secondary biochemical module adopts an anaerobic fluidized bed reactor and an anaerobic continuous stirring reactor. An anaerobic fluidized bed reactor is a high-efficiency biomembrane method, and substances with large surface area, such as sand, and the like are used as carriers. Anaerobic microorganisms are bonded on the surface of sand or other carriers in a membrane form and flow in sewage, and the microorganisms and organic matters in the sewage are contacted, adsorbed and decomposed, so that the treatment purpose is achieved, compared with the traditional anaerobic reactor, the anaerobic fluidized bed reactor has a good removal effect on organic wastewater and low-load organic wastewater under a low-temperature condition, and therefore, an additional heat preservation system is not needed, and the anaerobic fluidized bed reactor can be more suitable for a water treatment system with large water quality and water quantity change; an anaerobic continuous stirring reactor, which is an anaerobic treatment technology that makes fermentation raw materials and microorganisms in a complete mixing state, completes the fermentation of feed liquid and the production of methane in a closed tank body, a stirring device is arranged in a digester to make the fermentation raw materials and the microorganisms in a complete mixing state, a feeding mode adopts constant-temperature continuous feeding or semi-continuous feeding operation, newly-entered raw materials are quickly mixed with all fermentation liquid strains in the fermentor due to the stirring effect, so that the concentration of fermentation substrates is always kept in a relatively low state, the anaerobic continuous stirring reactor can treat the raw materials with high suspended solid content, the materials in the digester are uniformly distributed, the layering state is avoided, the opportunity of contact between the materials and the microorganisms is increased, the heat preservation heating system outside the reactor is preserved by utilizing the waste heat generated by methane power generation, the gas production rate and the investment utilization rate are greatly improved, meanwhile, the reactor can work normally all the year round, and the occupied area and the operation cost are reduced.
The aerobic unit in the secondary biochemical module adopts a biological contact oxidation reactor and an anoxic-aerobic aeration biological filter reactor. The biological contact oxidation reactor is a biological reactor for aerobic treatment of sewage, a certain amount of filler is filled in the biological contact oxidation reactor, and pollutants are removed by utilizing a biological film growing on the filler and sufficient oxygen supply; an anoxic-aerobic biological aerated filter reactor is characterized in that an anoxic unit is arranged in front of the reactor on the basis of a traditional biological aerated filter reactor, and a nitrifying liquid reflux system is arranged behind the biological aerated filter reactor.
(5) The anaerobic processes adopted in the secondary biochemical module are all quick-start type, and the advanced anaerobic process without an external heating system is suitable for a wastewater treatment system which is shut down in winter when no water exists and is quickly started after shut down, and the operation cost is greatly reduced; the anaerobic continuous stirring reactor system is adopted to fully utilize the characteristics of the non-fermentation bean product production wastewater, generate biogas resources and realize recycling, improve the resource recycling rate and reduce the operation cost.
(6) In the three-stage advanced treatment module, a micro-sand precipitation process is a compact, efficient and flexible rapid precipitation technology, and is characterized in that micro-sand and a polymeric flocculant are utilized to act together, so that pollutants and micro-sand are polymerized into large-particle flocs with the diameter of more than 150 microns to accelerate precipitation separation, and meanwhile, the inclined plate precipitation principle is combined to reduce the area of a precipitation tank and the precipitation time, so that a good and stable water outlet effect is kept; the active sand filter tank is continuous contact filtering equipment integrating flocculation, clarification and filtering, and aims to further realize sludge-water separation of precipitated sewage and ensure that effluent SS reaches the standard; the dynamic membrane filtration system realizes solid-liquid separation by utilizing micro-mesh materials with micron-sized pore diameters, and the interception capacity of the dynamic membrane filtration system can reach the microfiltration or ultrafiltration level; ultraviolet disinfection, wherein ultraviolet rays with proper wavelength can destroy the molecular structure of DNA (deoxyribonucleic acid) or RNA (ribonucleic acid) in microbial organism cells to cause death of growing cells and/or death of regenerative cells, thereby achieving the effect of sterilization and disinfection.
(7) The invention has high resource recovery and utilization rate, energy saving and consumption reduction and is environment-friendly.
Drawings
FIG. 1 is a process scheme of the present invention;
FIG. 2 is a schematic view of an air flotation oil removal sedimentation regulating water tank according to the present invention.
In the figure, 1-a primary pretreatment module; 2-a secondary biochemical module; 3-three-level advanced treatment module; 4, adjusting the water tank; 5, water inlet pipe; 6-an air flotation reaction zone; 7-a stirrer; 8-a contacting chamber; 9-water for dissolving gas; 10-an air flotation separation chamber; 11-oil removal zone; 12-oil separation lower baffle; 13-oil separation upper baffle; 14-floater skimmer; 15-a settling zone; 16-a sediment hopper; 17-a slag discharge system; 18-a sewage pump; 19-water outlet pipe.
Detailed Description
The present invention will be described in detail below with reference to the accompanying drawings, but the scope of the present invention is not limited by the embodiments.
FIG. 1 is a process route diagram of the present invention, and is a diagram showing a modular integrated system for treating non-fermented soybean product production wastewater, which comprises a primary pretreatment module 1, a secondary biochemical module 2 and a tertiary advanced treatment module 3; the primary pretreatment module 1 is provided with a fine mesh sieve and an air floatation oil separation sedimentation regulating water tank; the secondary biochemical module 2 is provided with an anaerobic unit and an aerobic unit, the anaerobic unit comprises an anaerobic fluidized bed reactor and an anaerobic continuous stirring reactor, and the aerobic unit comprises a biological contact oxidation reactor and an anoxic-aerobic aeration biological filter reactor; the third-level advanced treatment module 3 is provided with a micro-sand sedimentation tank, an active sand filter, a dynamic membrane filtration system and an ultraviolet disinfection reactor.
The inlet of the fine mesh sieve of the primary pretreatment module 1 is connected with the inlet of non-fermentation bean product production wastewater, and the outlet of the fine mesh sieve is connected with the inlet of an air floatation oil separation sedimentation regulating water tank; the outlet of the air floatation oil removal sedimentation regulating water tank is connected with the inlet of the secondary biochemical module;
an anaerobic unit inlet of the second-stage biochemical module 2 is connected with an outlet of the first-stage pretreatment module air-flotation oil-separation precipitation regulating water tank; the inlet of the anaerobic fluidized bed is connected with the inlet of the anaerobic unit, the outlet of the anaerobic fluidized bed is connected with the outlet of the anaerobic unit, the inlet of the anaerobic continuous stirring reactor is connected with the inlet of the anaerobic unit, and the outlet of the anaerobic continuous stirring reactor is connected with the outlet of the anaerobic unit; the outlet of the anaerobic unit is connected with the inlet of the aerobic unit; the outlet of the aerobic unit is connected with the inlet of the three-stage advanced treatment module, the inlet of the biological contact oxidation reactor is connected with the inlet of the aerobic unit, the outlet of the biological contact oxidation reactor is connected with the outlet of the aerobic unit, the inlet of the anoxic-aerobic biological aerated filter is connected with the inlet of the aerobic unit, and the outlet of the anoxic-aerobic biological aerated filter is connected with the outlet of the aerobic unit;
the inlet of the micro-sand sedimentation tank of the third-level advanced treatment module 3 is connected with the outlet of the second-level biochemical treatment module, and the outlet is connected with the inlet of the active sand filter; the outlet of the active sand filter is connected to the inlet of the dynamic membrane filtration system; the outlet of the dynamic membrane filtration system is connected with the inlet of the ultraviolet disinfection reactor; the outlet of the ultraviolet disinfection reactor is connected to the main outlet of the water treatment system;
the anaerobic fluidized bed reactor, the anaerobic continuous stirring reactor, the biological contact oxidation reactor, the anoxic-aerobic biological aerated filter and the dynamic membrane filtration system are provided with a monitoring device and an electric valve in front of the inlet, and different units can be automatically selected to operate according to the water quality condition.
The modular integrated process for treating the non-fermented bean product production wastewater comprises the following steps:
(1) starting and operating a primary pretreatment module, introducing non-fermentation bean product production wastewater into a total sewage treatment system, and removing larger substances in the wastewater through a fine mesh sieve;
(2) starting an air floatation oil separation precipitation adjusting water tank, removing oil and suspended matters in water and adjusting water quality and water quantity;
(3) on-line monitoring and analyzing COD value of wastewater in air floatation oil removal precipitation regulation pool, and combining actual water quantity QFruit of Chinese wolfberryAnd the design water quantity QIs provided withSelecting different operation units according to the relation;
(4) when Q isFruit of Chinese wolfberry≥1/2QIs provided withAnd when the COD is more than or equal to 2000mg/L, the step (5) is operated, otherwise, the step (6) is operated;
(5) starting the anaerobic continuous stirring reactor to remove pollutants in water, and operating the step (7);
(6) starting the anaerobic fluidized bed reactor to remove pollutants in water;
(7) monitoring and analyzing the COD value, BOD value and ammonia nitrogen value of the effluent of the anaerobic unit on line, entering the step (8) when the COD is more than 500mg/L, or the BOD is more than 300mg/L, or the ammonia nitrogen is more than 40mg/L, and entering the step (10) if not;
(8) starting the anoxic-aerobic biological aerated filter to remove pollutants in water;
(9) monitoring and analyzing the COD value, BOD value and ammonia nitrogen value of the effluent of the anaerobic fluidized bed reactor on line, entering the step (10) when the COD is more than 100mg/L, or the BOD is more than 30mg/L, or the ammonia nitrogen is more than 15mg/L, and entering the step (11) if not;
(10) starting a biological contact oxidation reactor to remove pollutants in water;
(11) starting a micro-sand sedimentation tank, and carrying out sedimentation and sludge discharge on the wastewater;
(12) starting the active sand filter to filter the wastewater;
(13) according to the requirement of the effluent quality, when the SS of the effluent quality is less than 15mg/L, the step (14) is carried out, otherwise, the step (15) is carried out;
(14) starting a dynamic membrane filtration system to filter the wastewater;
(15) starting the ultraviolet disinfection reactor to disinfect the wastewater.
Example 1:
in this embodiment, the modular integrated process system and method shown in fig. 1 are used to treat wastewater from a non-fermented bean product processing plant, and in the treatment process: the design grid size of the fine grid sieve adopts 10 mm; the designed residence time of the reaction zone in the air flotation zone is 5min, the designed flow rate of the contact chamber in the air flotation zone is 0.05m/s, the designed residence time of the contact chamber is 2min, and the surface load of the separation chamber in the air flotation zone is 6m3/(m2H); in the oil separation area, a 2-stage oil separation lower baffle, a 1-stage oil separation upper baffle and 1 floater oil skimmer are designed, and the floater oil skimmer is arranged in front of the oil separation upper baffle; the sedimentation zone comprises 2 sediment hoppers and 1 set of slag discharge system; regulating deviceThe retention time of the water-saving tank is designed to be 12 hours;
the design load of the anaerobic fluidized bed reactor is 5 kgCOD/(m)3D), designing the maximum ascending flow velocity to be 8 m/h; the designed residence time of the anaerobic continuous stirred reactor is 20 d; the BOD load of the biological contact oxidation reactor is designed to be 1.5 kg/(m)3D); the anaerobic-aerobic aeration biological filter reactor has an anoxic zone with a designed retention time of 3h and a nitrifying liquid reflux ratio of 200 percent and a designed BOD load of 1.8 kgBOD/(m)3·d)；
The design surface load of the micro-sand sedimentation tank is 10m3/(m2H); the average filtering speed of the active sand filter is 6 m/h.
The water quality test results of the wastewater treated by the integrated process system and the method of the embodiment are shown in table 1.
TABLE 1
| Item | Unit of | Inflow water | Discharging water |
| COD | mg/L | 3500 | 100 |
| BOD | mg/L | 1500 | 20 |
| SS | mg/L | 1000 | 50 |
| pH | 4.5—6.5 | 6—9 | |
| TP | mg/ |
10 | 0.5 |
| Ammonia nitrogen | mg/L | 45 | 15 |
Example 2:
in this embodiment, the modular integrated process system and method shown in fig. 1 are used to treat wastewater from a non-fermented bean product processing plant, and in the treatment process: the design grid size of the fine grid sieve adopts 10 mm; the designed residence time of the reaction zone of the air flotation zone is 5min, the designed flow rate of the contact chamber of the air flotation zone is 0.05m/s, the designed residence time of the contact chamber is 2min, and the surface load of the separation chamber of the air flotation zone is 7m3/(m2H); in the oil separation area, a 2-stage oil separation lower baffle, a 1-stage oil separation upper baffle and 1 floater oil skimmer are designed, and the floater oil skimmer is arranged in front of the oil separation upper baffle; the sedimentation zone comprises 3 sediment hoppers and 1 set of slag discharge system; adjusting the designed retention time of the water pool to be 20 h;
the design load of the anaerobic fluidized bed reactor is 6 kgCOD/(m)3D), designing the maximum ascending flow velocity to be 9 m/h; the BOD load of the biological contact oxidation reactor is designed to be 1.5 kg/(m)3·d)；
The design surface load of the micro-sand sedimentation tank is 10-14 m3/(m2H); the average filtering speed of the active sand filter is designed to be 6 m/h; a dynamic membrane filtration system, wherein the designed filtration speed is 13 m/h; the film forming material comprises nylon screen, terylene non-woven fabric and diatomite, wherein the nylon screen is 1cm x 1cm, the designed mesh size is 10 meshes, the terylene non-woven fabric is 1cm x 1cm, and the unit area mass is 270g/m2The designed permeability of the diatomite is 0.2Darcy, and the mass ratio of the nylon screen mesh, the polyester non-woven fabric and the diatomite is 10:1: 5.
The water quality testing results of the wastewater treated by the integrated process system and the method of the embodiment are shown in table 2.
TABLE 2
| Item | Unit of | Inflow water | Discharging water |
| COD | mg/L | 1500 | 100 |
| BOD | mg/ |
500 | 20 |
| SS | mg/L | 600 | 10 |
| pH | 4.5—6.5 | 6—9 | |
| TP | mg/L | 4.5 | 0.5 |
| Ammonia nitrogen | mg/L | 40 | 15 |
Example 3:
in this embodiment, the modular integrated process system and method shown in fig. 1 are used to treat wastewater from a non-fermented bean product processing plant, and in the treatment process: the design grid size of the fine grid sieve adopts 10 mm; the designed residence time of the reaction zone of the air flotation zone is 5min, the designed flow rate of the contact chamber of the air flotation zone is 0.05m/s, the designed residence time of the contact chamber is 2min, and the surface load of the separation chamber of the air flotation zone is 8m3/(m2H); in the oil separation area, a 2-stage oil separation lower baffle, a 1-stage oil separation upper baffle and 1 floater oil skimmer are designed, and the floater oil skimmer is arranged in front of the oil separation upper baffle; the sedimentation zone comprises 4 sediment hoppers and 1 set of slag discharge system; adjusting the designed retention time of the water pool to 24 h;
the design load of the anaerobic fluidized bed reactor is 8 kgCOD/(m)3D), designing the maximum ascending flow velocity to be 10 m/h; the designed residence time of the anaerobic continuous stirred reactor is 20 d; the BOD load of the biological contact oxidation reactor is designed to be 1.5 kg/(m)3D); the anaerobic-aerobic aeration biological filter reactor has an anoxic zone with a designed retention time of 3h and return of nitrified liquidThe flow ratio is 200 percent, and the BOD load is designed to be 2.0 kgBOD/(m)3·d)；
The design surface load of the micro-sand sedimentation tank is 14m3/(m2H); the average filtering speed of the active sand filter is designed to be 6 m/h; a dynamic membrane filtration system, wherein the designed filtration speed is 15 m/h; the film forming material comprises nylon screen, terylene non-woven fabric and diatomite, wherein the nylon screen is 1cm x 1cm, the designed mesh size is 10 meshes, the terylene non-woven fabric is 1cm x 1cm, and the unit area mass is 300g/m2The designed permeability of the diatomite is 0.25Darcy, and the mass ratio of the nylon screen mesh, the polyester non-woven fabric and the diatomite is 10:1: 5.
The water quality testing results of the wastewater treated by the integrated process system and method of the embodiment are shown in table 3.
TABLE 3
| Item | Unit of | Inflow water | Discharging water |
| COD | mg/ |
2000 | 100 |
| BOD | mg/L | 900 | 20 |
| SS | mg/L | 650 | 15 |
| pH | 4.5—6.5 | 6—9 | |
| TP | mg/ |
10 | 0.5 |
| Ammonia nitrogen | mg/L | 45 | 15 |
Although embodiments of the present invention have been shown and described above, it is understood that the above embodiments are exemplary and should not be construed as limiting the present invention, and that variations, modifications, substitutions and alterations can be made to the above embodiments by those of ordinary skill in the art within the scope of the present invention.
Claims (5)
1. Handle non-fermentation class bean products waste water's modularization integrated system, its characterized in that: the device comprises a primary pretreatment module, a secondary biochemical module and a tertiary advanced treatment module; the primary pretreatment module is provided with a fine mesh sieve and an air floatation oil removal sedimentation regulating water tank; the secondary biochemical module is provided with an anaerobic unit and an aerobic unit, the anaerobic unit comprises an anaerobic fluidized bed reactor and an anaerobic continuous stirring reactor, and the aerobic unit comprises a biological contact oxidation reactor and an anoxic-aerobic aeration biological filter reactor; the three-stage advanced treatment module is provided with a micro-sand sedimentation tank, an active sand filter, a dynamic membrane filtration system and an ultraviolet disinfection reactor; the inlet of the fine mesh sieve of the primary pretreatment module is connected with a non-fermentation bean product production wastewater inlet, and the outlet of the fine mesh sieve of the primary pretreatment module is connected with the inlet of the air floatation oil separation sedimentation regulating water tank; the outlet of the air floatation oil separation sedimentation adjusting water tank is connected with the inlet of the secondary biochemical module;
an anaerobic unit inlet of the second-stage biochemical module is connected with an outlet of the first-stage pretreatment module air floatation oil separation sedimentation regulating water tank; the inlet of the anaerobic fluidized bed is connected with the inlet of the anaerobic unit, the outlet of the anaerobic fluidized bed is connected with the outlet of the anaerobic unit, the inlet of the anaerobic continuous stirring reactor is connected with the inlet of the anaerobic unit, and the outlet of the anaerobic continuous stirring reactor is connected with the outlet of the anaerobic unit; the outlet of the anaerobic unit is connected with the inlet of the aerobic unit; the outlet of the aerobic unit is connected with the inlet of the three-stage advanced treatment module, the inlet of the biological contact oxidation reactor is connected with the inlet of the aerobic unit, the outlet of the biological contact oxidation reactor is connected with the outlet of the aerobic unit, the inlet of the anoxic-aerobic biological aerated filter is connected with the inlet of the aerobic unit, and the outlet of the anoxic-aerobic biological aerated filter is connected with the outlet of the aerobic unit;
the inlet of the micro-sand sedimentation tank of the three-level advanced treatment module is connected with the outlet of the secondary biochemical treatment module, and the outlet of the micro-sand sedimentation tank is connected with the inlet of the active sand filter; the outlet of the active sand filter is connected to the inlet of the dynamic membrane filtration system; the outlet of the dynamic membrane filtration system is connected with the inlet of the ultraviolet disinfection reactor; the outlet of the ultraviolet disinfection reactor is connected to the main outlet of the water treatment system;
the anaerobic fluidized bed reactor, the anaerobic continuous stirring reactor, the biological contact oxidation reactor, the anoxic-aerobic biological aerated filter and the dynamic membrane filtration system are provided with a monitoring device and an electric valve in front of the inlet, and different units can be automatically selected to operate according to the water quality condition.
2. The modular integrated process for treating the non-fermented bean product production wastewater is characterized by comprising the following steps of:
(1) starting and operating a primary pretreatment module, introducing non-fermentation bean product production wastewater into a total sewage treatment system, and removing larger substances in the wastewater through a fine mesh sieve;
(2) starting an air floatation oil separation precipitation adjusting water tank, removing oil and suspended matters in water and adjusting water quality and water quantity;
(3) on-line monitoring and analyzing COD value of wastewater in air floatation oil removal precipitation regulation pool, and combining actual water quantity QFruit of Chinese wolfberryAnd the design water quantity QIs provided withSelecting different operation units according to the relation;
(4) when Q isFruit of Chinese wolfberry≥1/2QIs provided withAnd when the COD is more than or equal to 2000mg/L, the step (5) is operated, otherwise, the step (6) is operated;
(5) starting the anaerobic continuous stirring reactor to remove pollutants in water, and operating the step (7);
(6) starting the anaerobic fluidized bed reactor to remove pollutants in water;
(7) monitoring and analyzing the COD value, BOD value and ammonia nitrogen value of the effluent of the anaerobic unit on line, entering the step (8) when the COD is more than 500mg/L, or the BOD is more than 300mg/L, or the ammonia nitrogen is more than 40mg/L, and entering the step (10) if not;
(8) starting the anoxic-aerobic biological aerated filter to remove pollutants in water;
(9) monitoring and analyzing the COD value, BOD value and ammonia nitrogen value of the effluent of the anaerobic fluidized bed reactor on line, entering the step (10) when the COD is more than 100mg/L, or the BOD is more than 30mg/L, or the ammonia nitrogen is more than 15mg/L, and entering the step (11) if not;
(10) starting a biological contact oxidation reactor to remove pollutants in water;
(11) starting a micro-sand sedimentation tank, and carrying out sedimentation and sludge discharge on the wastewater;
(12) starting the active sand filter to filter the wastewater;
(13) according to the requirement of the effluent quality, when the SS of the effluent quality is less than 15mg/L, the step (14) is carried out, otherwise, the step (15) is carried out;
(14) starting a dynamic membrane filtration system to filter the wastewater;
(15) starting the ultraviolet disinfection reactor to disinfect the wastewater.
3. The modular integrated process for treating wastewater from non-fermented bean product production according to claim 2, wherein: the design grid size of the fine grid sieve adopts 10 mm; in the air flotation oil separation sedimentation regulating water tank, the designed retention time of a reaction zone of an air flotation zone is 5min, the designed flow velocity of a contact chamber of the air flotation zone is 0.05m/s, the designed retention time of the contact chamber is 2min, and the surface load of a separation chamber of the air flotation zone is 6-8 m3/(m2H); in the oil separation area, a 2-stage oil separation lower baffle, a 1-stage oil separation upper baffle and 1 floater oil skimmer are designed, and the floater oil skimmer is arranged in front of the oil separation upper baffle; the settling zone comprises 2-4 sediment hoppers and 1 set of a slag discharge system; the designed retention time of the regulating pool is 12-24 h.
4. The modular integrated process for treating wastewater from non-fermented bean product production according to claim 2, wherein: the design load of the anaerobic fluidized bed reactor is 5-8 kgCOD/(m)3D), designing the maximum ascending flow velocity to be 8-10 m/h; the anaerobic continuous stirred reactor is designed to have a residence time of 20 d; the BOD load of the biological contact oxidation reactor is 1.5 kg/(m)3D); in the anoxic-aerobic biological aerated filter reactor, the retention time of an anoxic zone is 3h, the reflux ratio of nitrifying liquid is 200%, and the BOD load is 1.8-2.0 kgBOD/(m)3·d)。
5. The modular integrated process for treating wastewater from non-fermented bean product production according to claim 2, wherein: the design surface load of the micro-sand sedimentation tank is 10-14 m3/(m2H); the average filtering speed of the active sand filter is designed to be 6 m/h; the dynamic membrane filtration system is designed to have a filtration speed of 12-15 m/h; the film forming material comprises a nylon screen, a terylene non-woven fabric and diatomite, wherein the nylon screen is 1cm x 1cm in size, the designed mesh size is 10 meshes, the terylene non-woven fabric is 1cm x 1cm in size, and the unit area mass is 250-300 g/m2The designed permeability of the diatomite is 0.15-0.25 Darcy, and the mass ratio of the nylon screen mesh, the polyester non-woven fabric and the diatomite is 10:1: 5.
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| CN111252990A (en) * | 2020-03-23 | 2020-06-09 | 导洁(北京)环境科技有限公司 | Low-cost and easy-to-operate desulfurization wastewater zero-discharge method |
| CN113788577B (en) * | 2021-09-13 | 2023-04-18 | 昆明理工大学 | Integrated treatment device for underground water |
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