CN110902964A

CN110902964A - Ramie wastewater treatment process and treatment system

Info

Publication number: CN110902964A
Application number: CN201911263563.9A
Authority: CN
Inventors: 黄文�; 胡海蓉
Original assignee: Chengdu Tairun Environmental Engineering Co Ltd
Current assignee: Chengdu Tairun Environmental Engineering Co Ltd
Priority date: 2019-12-11
Filing date: 2019-12-11
Publication date: 2020-03-24

Abstract

The invention belongs to the field of wastewater treatment, and particularly relates to a ramie wastewater treatment process and a ramie wastewater treatment system, wherein the system comprises a first mechanical grating, a first water collecting tank, a first adjusting tank, an acidification reaction tank, a first plate-and-frame filter press, an intermediate tank, a first hydrolysis acidification tank, an IC anaerobic reactor, a first biological contact oxidation tank, a first sedimentation tank, a first air flotation system, a second mechanical grating, a second water collecting tank, a second adjusting tank, a second hydrolysis acidification tank, a second biological contact oxidation tank, a second sedimentation tank, a second air flotation system, a sludge concentration tank and a second plate-and-frame filter press; the invention has the beneficial effects that: can effectively treat ramie waste water with different concentrations, thereby avoiding environmental pollution and achieving the purpose of saving water resources, and the final waste water treatment result reaches the A standard of Vietnamese ramie industry pollutant discharge Standard.

Description

Ramie wastewater treatment process and treatment system

Technical Field

The invention belongs to the field of wastewater treatment, and particularly relates to a ramie wastewater treatment process and a ramie wastewater treatment system.

Background

According to the production process of ramie, the produced wastewater is mainly used in degumming production workshops, and the main wastewater is divided into pickling wastewater, ramie boiling wastewater, ramie washing wastewater, bleaching wastewater, pickling wastewater, refining wastewater and oil supply wastewater. The high-concentration wastewater has the advantages of large concentration change, high organic matter content, high SS content, high lignin content, high pH value and high chromaticityHigh grade, the main pollutants are COD and BOD₅SS, chromaticity and the concentration of each pollutant of low-concentration wastewater are all not high,

the characteristics of the high-concentration wastewater are as follows:

1) high concentration and high composition of organic pollutants

The first boiling wastewater has the characteristics of high wastewater temperature, high chroma, high pH value, high COD and large amount of refractory organic matters, and belongs to high-difficulty wastewater. COD is as high as 12000-20000 mg/L, the wastewater is brown, the water temperature is higher than 100 ℃, the wastewater is alkaline, the pH is as high as 13-14, the biodegradability is general, and the biological oxygen consumption BOD₅The concentration ranges from 5000 mg/L to 7000mg/L, wherein the lignin content is as high as 6000mg/L, so that the water quality is quite complex, the pollutant types are many, and the concentration has short-term fluctuation.

2) High concentration of SS

The SS content of the wastewater reaches 2000mg/L, if high-concentration SS is not pretreated, the subsequent biochemical treatment load can be seriously increased, the treatment efficiency is reduced, and insoluble suspended matters are accumulated in a biochemical tank along with the passage of time, so that the effective retention time of the biochemical tank is shortened, and microbial populations are reduced.

3) The biodegradability is more general

According to BOD₅the/CODcr is about 0.3, and the biodegradability is general.

4) The chroma of the waste water is higher

The raw water chroma of the wastewater is generally about 3000 times.

At present, few reports about ramie waste water treatment are reported or the treated ramie waste water is difficult to reach the discharge standard.

Disclosure of Invention

The invention provides a ramie wastewater treatment process and a ramie wastewater treatment system for solving the technical problems.

The technical scheme for solving the technical problems is as follows: a ramie wastewater treatment process comprises the following steps:

A. removing large particles from high-concentration wastewater through a first mechanical grid, then feeding the high-concentration wastewater into a first regulating tank, feeding the effluent into an acidification reaction tank to regulate the pH value, and feeding the effluent into a first plate-and-frame filter press to perform slag-water separation;

B. the clear effluent of the first plate-and-frame filter press enters an intermediate tank to adjust the pH value, the effluent enters a first hydrolysis acidification tank to degrade organic matters, part of organic pollutants in the wastewater are removed from the effluent in an IC (integrated circuit) anaerobic reactor through the respiration of anaerobic microorganisms, and then the effluent enters a first biological contact oxidation tank to remove most of the organic pollutants and ammonia nitrogen pollutants in the wastewater through the aerobic respiration and nitrification of aerobic microorganisms;

C. the effluent of the first biological contact oxidation tank enters a first sedimentation tank for sedimentation, the effluent enters a first air flotation system for sedimentation, and a flocculating agent is added into the first air flotation system;

D. and (2) low-concentration wastewater enters a second regulating reservoir through a second mechanical grid, the effluent of the second regulating reservoir and the effluent of the air flotation system in the step C enter a second hydrolysis acidification tank to degrade organic matters, the effluent enters a second biological contact oxidation tank to remove most organic pollutants and ammonia nitrogen pollutants in the wastewater, the effluent enters a second sedimentation tank to be precipitated, the effluent enters a second air flotation system with a flocculating agent, the effluent enters a sludge concentration tank to be treated, and finally the effluent after flocculation precipitation enters a second plate and frame filter press to be treated.

Further preferably, in step A, the pH is controlled to 2 to 3.

Further preferably, in step B, the pH is controlled to 7 to 8.

As a further preferred aspect of the present invention, in step C and step D, the flocculant is PAC and PAM.

As a further preferable mode of the present invention, in the steps C and D, the first air flotation system includes a first pipeline mixer and a first high-efficiency shallow air flotation machine, the second air flotation system includes a second pipeline mixer and a second high-efficiency shallow air flotation machine, and the flocculating agent is added into the first pipeline mixer and the second pipeline mixer through a dosing pump.

The invention also provides a ramie wastewater treatment system, which comprises a first mechanical grating, a first water collecting tank, a first regulating tank, an acidification reaction tank, a first plate-and-frame filter press, an intermediate tank, a first hydrolysis acidification tank, an IC (integrated circuit) anaerobic reactor, a first biological contact oxidation tank, a first sedimentation tank, a first air flotation system, a second mechanical grating, a second water collecting tank, a second regulating tank, a second hydrolysis acidification tank, a second biological contact oxidation tank, a second sedimentation tank, a second air flotation system, a sludge concentration tank and a second plate-and-frame filter press;

the first mechanical grating is communicated with a first water collecting tank, the water outlet of the first water collecting tank is communicated with the water inlet of a first regulating tank through a pipeline, the water outlet of the first regulating tank is communicated with the water inlet of an acidification reaction tank through a pipeline, the water outlet of the acidification reaction tank is communicated with the water inlet of a first plate-and-frame filter press through a pipeline, the water outlet of the first plate-and-frame filter press is communicated with the water inlet of an intermediate tank through a pipeline, the water outlet of the intermediate tank is communicated with the water inlet of a first hydrolysis acidification tank through a pipeline, the water outlet of the first hydrolysis acidification tank is communicated with the water inlet of an IC (integrated circuit) anaerobic reactor through a pipeline, the water outlet of the IC anaerobic reactor is communicated with the water inlet of a first biological contact oxidation tank through a pipeline, and the water outlet of the first biological contact oxidation tank is communicated with the water inlet of a first sedimentation tank through, the water outlet of the first sedimentation tank is communicated with the water inlet of the first air flotation system through a pipeline, and the water outlet of the first air flotation system is communicated with the water inlet of the second hydrolysis acidification tank through a pipeline;

the second mechanical grating is communicated with the second water collecting tank, the water outlet of the second water collecting tank is communicated with the water inlet of the second adjusting tank through a pipeline, the water outlet of the second adjusting tank is communicated with the water inlet of the second hydrolysis acidification tank through a pipeline, the water outlet of the second hydrolysis acidification tank is communicated with the water inlet of the second biological contact oxidation tank through a pipeline, the water outlet of the second biological contact oxidation tank is communicated with the water inlet of the second sedimentation tank through a pipeline, the water outlet of the second sedimentation tank is communicated with the water inlet of the second air floatation system through a pipeline, the water outlet of the second air floatation system is communicated with the water inlet of the sludge concentration tank through a pipeline, and the water outlet of the sludge concentration tank is communicated with the water inlet of the second plate and frame filter press through a pipeline.

Preferably, the first air flotation system comprises a first pipeline mixer, a first high-efficiency shallow air flotation machine and two first dosing pumps, a water outlet of the first sedimentation tank is communicated with a water inlet of the first pipeline mixer through a pipeline, a water outlet of the first pipeline mixer is communicated with a water inlet of the first high-efficiency shallow air flotation machine through a pipeline, a water outlet of the first high-efficiency shallow air flotation machine is communicated with a water inlet of the second hydrolysis acidification tank through a pipeline, and the two first dosing pumps are respectively communicated with two dosing ports on the first pipeline mixer through dosing pipelines.

Preferably, the second air flotation system comprises a second pipeline mixer, a second high-efficiency shallow air flotation machine and two second dosing pumps, a water outlet of the second sedimentation tank is communicated with a water inlet of the second pipeline mixer through a pipeline, a water outlet of the second pipeline mixer is communicated with a water inlet of the second high-efficiency shallow air flotation machine through a pipeline, a water outlet of the second high-efficiency shallow air flotation machine is communicated with a water inlet of the sludge concentration tank through a pipeline, and the two second dosing pumps are respectively communicated with two dosing ports on the second pipeline mixer through dosing pipelines.

Preferably, the sludge treatment system further comprises a third pipeline mixer, wherein a water outlet of the sludge concentration tank is communicated with a water inlet of the third pipeline mixer through a pipeline, and a water outlet of the third pipeline mixer is communicated with a water inlet of the second plate-and-frame filter press through a pipeline.

The invention has the beneficial effects that: can effectively treat ramie waste water with different concentrations, thereby avoiding environmental pollution and achieving the purpose of saving water resources, and the final waste water treatment result reaches the A standard of Vietnamese ramie industry pollutant discharge Standard.

Drawings

FIG. 1 is a flow chart of a processing system of the present invention.

In the drawings, the reference numerals denote the following components:

1. the system comprises a first mechanical grating, 2, a first adjusting tank, 3, an acidification reaction tank, 4, a first plate-and-frame filter press, 5, an intermediate tank, 6, a first hydrolysis acidification tank, 7, an IC anaerobic reactor, 8, a first biological contact oxidation tank, 9, a first sedimentation tank, 10, a second mechanical grating, 11, a second adjusting tank, 12, a second hydrolysis acidification tank, 13, a second biological contact oxidation tank, 14, a second sedimentation tank, 15, a sludge concentration tank, 16, a second plate-and-frame filter press, 17, a first pipeline mixer, 18, a first efficient shallow air flotation machine, 19, a second pipeline mixer, 20, a second efficient shallow air flotation machine, 21, a first water collecting tank, 22, a second water collecting tank, 23, a first dosing pump, 24, a second dosing pump, 25 and a third pipeline mixer.

Detailed Description

The principles and features of this invention are described below in conjunction with examples which are set forth to illustrate, but are not to be construed to limit the scope of the invention.

Examples

The invention provides a ramie wastewater treatment process, which comprises the following steps:

A. high-concentration wastewater is discharged into a sewage pipeline from a production workshop in a self-flowing mode, then the high-concentration wastewater is subjected to large particulate matter removal through a first mechanical grid 1 to avoid causing pipeline blockage of a subsequent working section, the collected slag is transported out together with a mud cake treated by a subsequent sludge treatment system, the effluent enters a first regulating tank 2 to be mechanically stirred to be homogenized and equalized, so that load impact of the subsequent working section is avoided, the effluent of the first regulating tank 2 is pumped into an acid precipitation reaction tank 3 through a pump, the pH value of the effluent is regulated to be 2-3 through adding sulfuric acid into the tank, the effluent is pumped into a first plate-and-frame filter press 4 to be subjected to slag-water separation after being fully reacted under the action of mechanical stirring, the removal rate of lignin in the process can reach more than 85%, SS in the wastewater is removed at the same time, and the dewatered slag is transported out;

B. the clear water of the first plate-and-frame filter press 4 enters an intermediate tank 5, alkali is added into the tank and the pH value is adjusted to 7-8 under the action of mechanical stirring, the stable operation of the subsequent biochemical treatment is ensured, the effluent of the intermediate tank 5 is pumped into a first hydrolysis acidification tank 6, the microbial film is suspended in the tank, the wastewater biochemical property is improved and part of organic matters are degraded through the action of acid-producing bacteria microorganisms, so that good water inlet conditions are provided for a subsequent IC anaerobic reactor 7, the tank is provided with a water collecting tank at the back, which provides the power for the subsequent IC anaerobic reactor 7, and a steam heating pipeline is arranged in the tank, so as to ensure the water temperature of the system during the operation in winter, remove part of organic pollutants in the wastewater in the IC anaerobic reactor 7 through the respiration of anaerobic microorganisms and generate methane, then the effluent enters a first biological contact oxidation tank 8, and most organic pollutants and ammonia nitrogen pollutants in the wastewater are removed through aerobic respiration and nitrification of aerobic microorganisms;

C. the effluent of the first biological contact oxidation tank 8 enters a first sedimentation tank 9 for sedimentation, mud and water are separated through the action of gravity, part of sludge flows back to an aerobic tank to ensure the number of microorganisms in the aerobic system, clear liquid is pumped into a first air floatation system to separate out sediment, the rest sludge is discharged into a sludge concentration tank 15, PAC and PAM are added into the first air floatation system to separate out sediment of part of soluble substances in the wastewater, the organic pollutants in the wastewater are further reduced, and slag enters the sludge concentration tank 15;

D. the low-concentration wastewater is discharged into a sewage pipeline from a production workshop in a self-flowing mode, the clear liquid after large granular substances are removed by a second mechanical grid 10 during collection enters a second regulating tank 11, the clear liquid is homogenized and equalized by mechanical stirring to avoid causing load impact of a subsequent workshop section, the effluent of the second regulating tank 11 and the effluent of the air floatation system in the step C enter a second hydrolysis acidification tank 12 to degrade organic matters, the organic pollutants in the wastewater are further reduced by the action of microorganisms, then the effluent automatically flows into a second biological contact oxidation tank 13 to remove most organic pollutants and ammonia nitrogen pollutants in the wastewater by the aerobic respiration action and nitrification action of aerobic microorganisms, then the effluent enters a second sedimentation tank 14 to be precipitated, mud and water are separated by the action of gravity, and part of sludge flows back to the second biological contact oxidation tank 13 to ensure the quantity of the microorganisms of the aerobic system, and discharging the clear liquid which reaches the standard, discharging the residual sludge into a sludge concentration tank 15, feeding the effluent of the second sedimentation tank 14 into a second air floatation system added with PAC and PAM, feeding the effluent into the sludge concentration tank 15 for treatment, and finally feeding the clear liquid subjected to flocculation and precipitation of the effluent into a second plate-and-frame filter press 16 for treatment.

In the steps C and D, the first air flotation system comprises a first pipeline mixer 17 and a first high-efficiency shallow layer air flotation machine 18, the second air flotation system comprises a second pipeline mixer 19 and a second high-efficiency shallow layer air flotation machine 20, and the flocculating agent is added into the first pipeline mixer 17 and the second pipeline mixer 19 respectively through a dosing pump.

As shown in fig. 1, a ramie waste water treatment system includes a first mechanical grating 1, a first water collecting tank 21, a first adjusting tank 2, an acid precipitation reaction tank 3, a first plate-and-frame filter press 4, an intermediate tank 5, a first hydrolysis acidification tank 6, an IC anaerobic reactor 7, a first biological contact oxidation tank 8, a first sedimentation tank 9, a first air flotation system, a second mechanical grating 10, a second water collecting tank 22, a second adjusting tank 11, a second hydrolysis acidification tank 12, a second biological contact oxidation tank 13, a second sedimentation tank 14, a second air flotation system, a sludge concentration tank 15 and a second plate-and-frame filter press 16;

the first mechanical grating 1 is communicated with a first water collecting tank 21, a water outlet of the first water collecting tank 21 is communicated with a water inlet of a first adjusting tank 2 through a pipeline, a water outlet of the first adjusting tank 2 is communicated with a water inlet of an acid precipitation reaction tank 3 through a pipeline, a water outlet of the acid precipitation reaction tank 3 is communicated with a water inlet of a first plate and frame filter press 4 through a pipeline, a water outlet of the first plate and frame filter press 4 is communicated with a water inlet of an intermediate tank 5 through a pipeline, a water outlet of the intermediate tank 5 is communicated with a water inlet of a first hydrolysis acidification tank 6 through a pipeline, a water outlet of the first hydrolysis acidification tank 6 is communicated with a water inlet of an IC anaerobic reactor 7 through a pipeline, a water outlet of the IC anaerobic reactor 7 is communicated with a water inlet of a first biological contact oxidation tank 8 through a pipeline, the water outlet of the first biological contact oxidation tank 8 is communicated with the water inlet of the first sedimentation tank 9 through a pipeline, the water outlet of the first sedimentation tank 9 is communicated with the water inlet of the first air flotation system through a pipeline, and the water outlet of the first air flotation system is communicated with the water inlet of the second hydrolysis acidification tank 12 through a pipeline;

the second mechanical grid 10 is communicated with the second water collecting tank 22, the water outlet of the second water collecting tank 22 is communicated with the water inlet of the second adjusting tank 11 through a pipeline, the water outlet of the second regulating tank 11 is communicated with the water inlet of the second hydrolysis acidification tank 12 through a pipeline, the water outlet of the second hydrolytic acidification tank 12 is communicated with the water inlet of the second biological contact oxidation tank 13 through a pipeline, the water outlet of the second biological contact oxidation tank 13 is communicated with the water inlet of the second sedimentation tank 14 through a pipeline, the water outlet of the second sedimentation tank 14 is communicated with the water inlet of the second air floatation system through a pipeline, the water outlet of the second air floatation system is communicated with the water inlet of the sludge concentration tank 15 through a pipeline, and the water outlet of the sludge concentration tank 15 is communicated with the water inlet of the second plate-and-frame filter press 16 through a pipeline.

The first air flotation system comprises a first pipeline mixer 17, a first efficient shallow air flotation machine 18 and two first dosing pumps 23, a water outlet of the first sedimentation tank 9 is communicated with a water inlet of the first pipeline mixer 17 through a pipeline, a water outlet of the first pipeline mixer 17 is communicated with a water inlet of the first efficient shallow air flotation machine 18 through a pipeline, a water outlet of the first efficient shallow air flotation machine 18 is communicated with a water inlet of the second hydrolysis acidification tank 12 through a pipeline, and the first dosing pumps 23 are respectively communicated with two dosing ports on the first pipeline mixer 17 through dosing pipelines.

The second air flotation system comprises a second pipeline mixer 19, a second efficient shallow air flotation machine 20 and two second dosing pumps 24, the water outlet of the second sedimentation tank 14 is communicated with the water inlet of the second pipeline mixer 19 through a pipeline, the water outlet of the second pipeline mixer 19 is communicated with the water inlet of the second efficient shallow air flotation machine 20 through a pipeline, the water outlet of the second efficient shallow air flotation machine 20 is communicated with the water inlet of the sludge concentration tank 15 through a pipeline, and the two second dosing pumps 24 are respectively communicated with two dosing ports on the second pipeline mixer 19 through dosing pipelines.

The sludge treatment device is characterized by further comprising a third pipeline mixer 25, wherein a water outlet of the sludge concentration tank 15 is communicated with a water inlet of the third pipeline mixer 25 through a pipeline, and a water outlet of the third pipeline mixer 25 is communicated with a water inlet of the second plate-and-frame filter press 16 through a pipeline.

1.1 selection of treatment Process for high-concentration wastewater

When the treatment process is selected, the problems of high CODcr concentration and BOD in the high-concentration wastewater are mainly solved₅High concentration, high SS, high lignin and high chroma. Aiming at the characteristic wastewater, the design adopts a treatment process of physicochemical pretreatment and biochemical treatment. The physicochemical treatment mainly reduces SS, lignin and chroma in the wastewater, and the biochemical treatment mainly reduces high-concentration COD, BOD and ammonia nitrogen, and ensures that pollutants such as the COD of the wastewater can be stably discharged up to the standard.

1.1.1 physicochemical treatment

1. Lignin removal process

At present, methods for removing lignin in wastewater mainly comprise an acid precipitation method, a membrane separation method, an evaporation concentration method and a microorganism acid precipitation method.

The microbe acid separating method is mainly characterized by that after the culture of strain is adopted, it is fed into the waste water, and the pH value of the waste water is reduced to 2-3, then the lignin is separated out, and then degraded or modified by other strains.

The evaporative concentration method is mainly high in investment and operation cost, so that enterprises are difficult to bear.

The membrane separation method is mainly characterized in that the wastewater pollutant concentration is high, the membrane is easily polluted, the removal rate is reduced, and the service life of the membrane is greatly reduced.

According to the technical and economic comparison and in combination with the more and more successful cases of the current practical engineering application, the acid precipitation method is selected as the process for removing the lignin in the project, namely the pH value of the wastewater is adjusted to be about 2-3, the lignin in the wastewater is precipitated under the acidic condition to form a suspended state in the wastewater, and the lignin degradation rate of the wastewater can reach more than 90% and the effect is stable after the lignin is filtered by a special plate-and-frame filter press.

2. SS removal method

At present, the main methods for removing SS in wastewater comprise: coagulating sedimentation (gravity sedimentation), air-float method, mechanical filtration method, etc.

The suspended matters in the project are mainly small-particle matters in the wastewater and high in content, and if mechanical filtration is directly adopted, the method can only remove non-soluble solids with the diameter more than 0.1 mu m and can not remove matters with the diameter less than 0.1 mu m; the air floatation method has a good effect on wastewater with the SS content lower than 1000mg/L, but the wastewater with the SS content too high can cause air floatation water turbidity, so the inventor proposes to adopt the process of the air floatation method as the front end materialization treatment of the wastewater.

1.1.2 Biochemical treatment

1. Hydrolytic acidification treatment

The principle and the characteristics of the hydrolysis acidification reactor are as follows:

the mechanism-hydrolytic acidification is a sewage biochemical treatment technology which is widely adopted in recent years, and mainly utilizes the preceding stage reaction mechanism of anaerobic biochemical treatment, and microorganisms participating in the reaction mainly take facultative bacteria as main components. In the hydrolysis stage, the solid matter is degraded into soluble matter, the macromolecular matter is degraded into small molecular matter, and in the acidogenic stage, the carbohydrate is degraded into fatty acid, mainly acetic acid, butyric acid and propionic acid. Hydrolysis and acidogenesis proceed very quickly and it is difficult to separate them. The microorganisms participating in the reaction at this stage are mainly hydrolysis and acid-producing bacteria. During the acid decline phase, the organic acids and dissolved nitrogen compounds decompose into ammonia, amines, carbonates and small amounts of CO₃.N₂、CH₄And H₂. In this stage, the ammonia nitrogen concentration is increased due to the activity of ammonia-producing bacteria, the oxidation-reduction potential is reduced, the pH is raised, and the change of the pH creates a proper active condition for the growth and the propagation of methanobacteria. The methane bacteria then convert the organic acid into biogas. By hydrolytic acidification treatment, the organic pollutants in a macromolecular state are decomposed into micromolecular substances with strong biochemical property, and the biochemical property and the solubility of the sewage are improved. The hydrolytic acidification treatment process absorbs the characteristic that organic matters are adsorbed by microorganisms in a short process, and achieves the purposes of saving energy and reducing the operation cost.

The research work of the hydrolysis acidification process is to gradually develop the hydrolysis acidification biological treatment process from the test of the sewage anaerobic treatment through repeated practice and theoretical analysis, and the hydraulic retention time is greatly shortened because the methanation stage is omitted, and compared with an anaerobic tank, the hydrolysis acidification process has the following advantages:

(1) a closed pool, a stirrer and a three-phase separator are not needed;

(2) the hydrolyzed product is micromolecular organic matter, so that the biodegradability is improved, the reaction time is shortened, and the energy consumption for treatment is reduced;

(3) the effluent has no bad smell of anaerobic fermentation, and the treatment environment is improved;

(4) the hydrolysis tank has small volume, and the capital investment is saved;

(5) the hydrolysis tank has the function of a digestion tank, and the residual sludge is less;

(6) generally, the SS treatment rate is 80 percent, and the COD removal rate is 20 to 30 percent, which is beneficial to subsequent treatment.

2. Anaerobic biochemical treatment

Mechanism-because the COD value of the waste water after mixing is very high, the waste water needs to be treated anaerobically to ensure the effect of the waste water in the next step. Anaerobic treatment is a harmless treatment method which mainly uses anaerobic microorganisms to degrade and stabilize organic matters under the anaerobic condition. During anaerobic biological treatment, complex organic compounds are degraded and converted into simple and stable compounds, while releasing energy (mostly in CH)₄In the form of (d). A small amount of organic matter is converted intoSynthesized as a new cellular component, the sludge growth rate is small. Compared with the current commonly used anaerobic reactors, such as the application situations and the application ranges of an Upflow Anaerobic Sludge Blanket (UASB), an anaerobic biological filter (AF), an anaerobic contact oxidation method, an IC reactor and the like, the characteristics of the waste water are combined, the IC reactor is selected as the anaerobic treatment process of the project, the waste water enters a second-stage UASB anaerobic reactor after degrading most pollutants in a first-stage IC anaerobic reactor, the residual protein substances are thoroughly degraded, and the waste water after subsequent aerobic treatment is ensured to reach the standard.

IC anaerobic reactor

The mechanism-IC reactor is similar to that formed by connecting 2 layers of UASB reactors in series. According to the functional division, the reactor is divided into 5 areas from bottom to top: a mixing zone, a 1 st anaerobic zone, a 2 nd anaerobic zone, a settling zone and a gas-liquid separation zone.

A mixing area: the water entering the bottom of the reactor, the granular sludge and the mud-water mixture returned from the gas-liquid separation zone are effectively mixed in the zone.

1, anaerobic zone: the mud-water mixture formed in the mixing area enters the area, and most organic matters are converted into methane under the action of high-concentration sludge. The rising flow of the mixed liquid and the violent disturbance of the methane enable the sludge in the reaction area to be in an expanded and fluidized state, the contact of the surface of the sludge and the water is enhanced, and the sludge keeps high activity. Along with the increase of the output of the biogas, a part of the mud-water mixture is lifted to the gas-liquid separation area at the top by the biogas.

A gas-liquid separation zone: the methane in the lifted mixture is separated from mud and water and is led out of the treatment system, and the mud and water mixture returns to the mixing area at the lowest end along the return pipe and is fully mixed with the sludge and the inlet water at the bottom of the reactor, so that the internal circulation of the mixed liquid is realized.

A 2 nd anaerobic zone: and (3) the waste water treated in the anaerobic zone (1) is partially lifted by the methane, and the rest of the waste water enters the anaerobic zone (2) through a three-phase separator. The sludge concentration in the area is low, and most organic matters in the wastewater are degraded in the No. 1 anaerobic zone, so the methane generation amount is low. The marsh gas is introduced into the gas-liquid separation zone through the marsh gas pipe, the disturbance to the anaerobic zone 2 is small, and favorable conditions are provided for the retention of the sludge.

A precipitation zone: and (3) performing solid-liquid separation on the sludge-water mixture in the anaerobic zone 2 in the settling zone, discharging supernatant liquid through a water outlet pipe, and returning the settled granular sludge to a sludge bed in the anaerobic zone 2.

It can be seen from the working principle of the IC reactor that the reactor is realized by a 2-layer three-phase separator to obtain high sludge concentration; the mud and water are fully contacted through the violent disturbance of a large amount of methane and internal circulation, and a good mass transfer effect is obtained.

Features-the main advantages of the IC reactor are as follows:

(1) high volume load: the IC reactor has high sludge concentration, large microbial biomass, internal circulation and good mass transfer effect, and the organic load of the inlet water can exceed 3 times of that of a common anaerobic reactor.

(2) Saving investment and floor area: the volume load rate of the IC reactor is about 3 times higher than that of the common UASB reactor, and the volume of the IC reactor is about 1/4-1/3 of the common reactor, so that the capital investment of the reactor is greatly reduced; furthermore, the height-diameter ratio of the IC reactor is very large (generally 4-8), so that the occupied area is small.

(3) Strong impact load resistance: when low-concentration wastewater (COD is 2000-3000 mg/L), the circulating flow in the reactor can reach 2-3 times of the water inflow; when high-concentration waste water (COD is 10000-12000 mg/L), the internal circulation flow can reach 10-20 times of water inflow. A large amount of circulating water and inlet water are fully mixed, so that harmful substances in raw water are fully diluted, and the influence of poisons on the anaerobic digestion process is greatly reduced.

(4) The low temperature resistance is strong: the effect of temperature on anaerobic digestion is primarily on the rate of digestion. The effect of temperature on anaerobic digestion becomes no longer significant and severe in IC reactors due to the large number of microorganisms. Generally, anaerobic digestion in the IC reactor can be carried out under normal temperature (20-25 ℃), so that the difficulty of digestion heat preservation is reduced, and energy is saved.

(5) Ability to buffer pH: the internal circulation flow is equivalent to the effluent backflow of the No. 1 anaerobic zone, the pH value can be buffered by utilizing the alkalinity of COD conversion, the pH value in the reactor is kept in an optimal state, and the alkali feeding amount of the inlet water can be reduced.

(6) Internal automatic circulation without external power: the reflux of the common anaerobic reactor is realized by external pressurization, and the IC reactor realizes the internal circulation of mixed liquid by taking the methane generated by the IC reactor as lifting power, so that a pump is not required to be arranged for forced circulation, and the power consumption is saved.

(7) The effluent stability is good: the adverse effects of K s high level in the anaerobic process can be compensated by using two stages of UASB cascaded anaerobic treatment.

(8) The starting period is short: the sludge activity in the IC reactor is high, the biological proliferation is fast, and favorable conditions are provided for fast starting of the reactor. The starting period of the IC reactor is generally 1-2 months, while the starting period of the UASB is 4-6 months.

(9) The biogas has high utilization value: the purity of the biogas generated by the reactor is high, CH₄60% -70% of CO₂30-40 percent of the total organic matter and 1-5 percent of other organic matter, and can be used as fuel.

To IC anaerobic system, I want to adopt enamel tower structure, for traditional steel concrete cell body structure, enamel steel sheet tower structure has following advantage:

1) the complete equipment is made, the construction period is short, and the complete production and installation can be realized within 1-2 months generally;

2) the corrosion resistance of the enameled pressed steel is stronger than that of a steel concrete structure, and the defects of high difficulty and high requirement on corrosion resistance of the steel concrete can be overcome;

3) under the condition of a certain volume, the tower type equipment can save the floor area by increasing the height;

4) the tower structure is convenient to overhaul and maintain;

5) more successful experiences are accumulated in the complete reactor engineering, the traditional three-phase separator is optimally designed, and the method can be applied to the engineering to ensure the treatment effect.

3. Aerobic biochemical treatment

Because the ammonia nitrogen and the total nitrogen in the wastewater are not high, I prefer to adopt a contact oxidation process.

The biological contact oxidation process has the characteristics that:

the biological contact oxidation method is a biomembrane process between activated sludge process and biological filter, the biological contact oxidation pond is equipped with filler, part of microorganism is fixed and grown on the surface of filler in the form of biomembrane, and part is grown in water in the form of flocculent suspension, so that it has the characteristics of both activated sludge process and biological filter.

The aeration device of the biological contact oxidation system is arranged at the bottom of the filler, and a blast aeration system is adopted, so that the effective volume can be increased, the turbulence between filler layers is intense, the biological membrane is updated quickly, the activity is high, and the blockage is not easy to occur.

The biological contact oxidation method has the process characteristics that:

1) because the specific surface area of the filler is large, the oxygenation condition in the tank is good, and the biomass per unit volume in the biological contact oxidation tank is higher than that in the activated sludge aeration tank and the biological filter tank, the biological contact oxidation tank has higher volume load;

2) because a certain part of microorganisms are attached to and grow on the surface of the filler, the problem of sludge expansion does not exist, and the operation and management are simple and convenient;

3) because the biological contact oxidation pond has a large amount of biological solids and the water flow belongs to a complete mixing type, the biological contact oxidation pond has stronger adaptability to sudden change of water quality and water quantity.

4) The operation is simple, the operation is convenient, the maintenance and the management are easy, the sludge expansion phenomenon is not generated, and the filter flies are not generated.

5) The biological contact oxidation treatment technology has various purification functions, and has certain effects on nitrogen removal and phosphorus removal besides effectively removing organic pollutants.

The sewage treatment project is an infrastructure project with complex technology, large investment and strong policy. Although no obvious economic benefit exists, the environmental benefit and the long-term social benefit are immeasurable. Based on the characteristics, even developed countries pay attention to the development and construction of sewage treatment engineering projects, the problem of how to reduce capital investment and operation cost must be considered, and the research simplifies the sewage treatment process flow, occupies less land, saves electricity consumption, is convenient for management, improves the treatment effect and the like, and has new breakthrough. Compared with the traditional two-stage biochemical treatment and the existing oxidation ditch and SBR processes, the biological contact oxidation process has the advantages of simple process flow, strong applicability and stable and excellent effluent quality. Has obvious advantages in the aspects of construction investment, floor area, operation cost and the like.

Therefore, for high-concentration wastewater, the first aeration treatment process adopts a contact oxidation process, and effluent enters a low-concentration wastewater treatment system after passing through an air flotation machine.

1.2 selection of Low concentration wastewater treatment Process

The B/C value of the low-concentration wastewater is 0.34, so that the low-concentration wastewater can be directly biochemically treated, and the concentration of each pollutant in the wastewater is not high, so that the wastewater can enter a biochemical treatment system without pretreatment.

The practical engineering experience of China shows that the wastewater can reach the discharge standard by adopting hydrolytic acidification and contact oxidation.

1.3 high concentration wastewater System design

1.3.1 first mechanical grid 1

The functions are as follows: get rid of the large granule material in the waste water, avoid causing the jam of follow-up elevator pump and pipeline, guarantee the steady continuous operation of system.

Design parameters

Designing the size: 3.0 × 0.5 × 1.0m, structure: steel concrete;

configuring equipment: a rotary mechanical grating machine, GSHZ400, N is 0.55KW, H is 2350m, the grid spacing is 1mm, a rake tooth ABS and a main body frame material SUS 304;

1.3.2 first regulating reservoir 2

The functions are as follows: high-concentration wastewater in a workshop is drained and the water quality and the water quantity are regulated, the high-concentration wastewater belongs to high-pollution wastewater, and the designed retention capacity of a regulating tank cannot be lower than 24 hours.

Designing parameters: designing the size: 14.0 × 10.0 × 6.0m, water inflow: 700m³Effective volume: 770m³Residence time: 26.4h, structure: and (5) steel concrete.

The corollary equipment:

1.1 set of perforation aeration stirring equipment, which is made of stainless steel;

2. a lift pump, a self-priming stainless steel pump, 65ZW30-18P, Q is 30m3/H, N is 4KW, H is 18m, the self-priming height is 5.5 m, 2 pumps are used, and 1 is prepared;

3. sensor liquid level controller, 1 set.

4. Flow meter, 0-30m³And h, 1 set.

1.3.3 acid out reaction tank 3

The functions are as follows: adding sulfuric acid, separating lignin in the wastewater under an acidic condition, and performing solid-liquid separation by a subsequent plate-and-frame filter press.

Designing parameters: designing the size: 7.0 × 2.0 × 6.0m, effective volume: 73m³The residence time is as follows: 2.5h, structure: and (4) corrosion prevention of the reinforced concrete and the glass fiber reinforced plastics.

Configuring equipment:

2. a lift pump, a self-priming stainless steel pump, 80ZW 50-60P, Q is 50m3/H, N is 22KW, H is 60m, 2 pumps are used, 1 is spare;

3.1 set of acid adding equipment, V is 5m³The chemical adding pump Q is 0-160L/h, N is 0.35KW, P is 0.6MPa, PVDF pump head.

4.1, pH on-line monitor, 1 set;

5. sensor liquid level controller, 1 set.

6. Flow meter, 0-30m³And h, 1 set.

1.3.4 first plate and frame Filter Press 4

The functions are as follows: the lignin separated out in the acidification reaction tank 3 is subjected to solid-liquid separation through mechanical separation, and most of lignin and organic pollutants are removed.

Configuring equipment:

1. the first plate-and-frame filter press 4XMZ120-1000-30U, N is 4kw, and the filtering area is 120m²The program-controlled automatic plate-pulling box-type filter press is provided with a plate-turning mud guide hopper and 2 plates, and the operation is switched.

2. PAC/PAM medicine adding device 1 set, metering pump Q0-240L/h, N0.55 KW, P0.6 MPa, PVDF pump head 2 sets.

1.3.5 intermediate tank 5

The functions are as follows: and storing the clear liquid of the plate-and-frame filter press, so that alkali can be conveniently added to adjust the pH value to 7-8 under the mechanical stirring action, and the subsequent biochemical water inlet condition is ensured.

Designing parameters: designing the size: 7.0 × 2.0 × 6.0m, effective volume: 77m³The residence time is as follows: 2.64h, structure: and (5) steel concrete.

Configuring equipment:

1. a self-priming pump 65ZW30-18, Q is 30m3/H, N is 4KW, H is 18m, the self-priming height is 5.5 m, 2 pumps are used, and 1 is prepared;

2. sensor liquid level controller, 1 set;

3.1 flowmeter, namely 1;

4. the alkali adding device V is 5m3, the carbon steel is used for corrosion prevention, the medicine adding pump Q is 0-160L/h, N is 0.35KW, P is 0.6MPa, and the PVDF pump head is used.

1.3.6 first hydrolysis acidification tank 6

The functions are as follows: the anaerobic and facultative composite microbes are utilized to decompose macromolecular substances into micromolecular substances, so that the biodegradability of the wastewater is improved.

Designing parameters:

designing the size of the hydrolysis acidification tank: l multiplied by B multiplied by H is 16.0m multiplied by 14.0m multiplied by 6.0m, the reinforced concrete is divided into two grids and runs in series.

Total effective volume: 1232m³(ii) a Residence time: 42.24 h; volume load: 2.95kgCOD/m³D distribution pool size: l × B × H is 14.0 × 2.0m × 6.0m, and is made of steel concrete; effective volume: 140m³(ii) a Residence time: 4.7 h;

configuring equipment:

the first hydrolysis acidification pool 6:

1.4 submersible mixers, QJB4/12-620/3-480S, N is 4.0 kw;

2. a guide plate 2 sets;

3. combined filler,. phi.150X 3000, 672m³And comprises a bracket.

4. The dredge pump 65WQ25-15-2.2, Q is 25m³H15 m, N2.2 kw,2 stands.

A water distribution pool:

5. a self-priming pump 80ZW40-25, Q is 40m3/H, N is 7.5KW, H is 25m, the self-priming height is 5.5 m, 2 pumps are used for 1;

6. 1 set of flow meter;

7. 1, pH on-line monitor, 1 set;

8. heating pipeline, 1 set.

1.3.7IC anaerobic reactor 7

The functions are as follows: the IC anaerobic reactor 7 has the functions of removing organic pollutants in the wastewater, converting organic compounds into methane and carbon dioxide, reducing the concentration of the wastewater and facilitating subsequent biochemical treatment.

Designing parameters:

water inflow: 700m³D; COD volumetric load: 2.55kgCOD/m³D; the structure is as follows: enamelled steel sheet

Number of reactors: 1, seat; the reactor size:

effective volume: 963.78m³(ii) a Residence time: 33 h.

The corollary equipment:

1. an IC reactor tank body, an enamel steel plate,

1 table (including internal supporting ring plate, stainless steel).

2. Water distribution system, the material: 1 set of stainless steel 304;

3. three-phase separator, the material: 2 sets of carbon steel corrosion prevention;

4.1 set of water seal device, phi 1200mm X1800 mm, stainless steel material;

5. 1, a mud-water separator, which is made of stainless steel;

6. a gas-water separator made of stainless steel, 1 unit;

7. sampling mud discharging system, material: stainless steel pipe, 1 set

8. The device comprises a matched instrument, 1 flowmeter and 1 pH meter;

1.3.8 first biological contact Oxidation tank 8

The functions are as follows: the first biological contact oxidation pond 8 utilizes microorganisms to oxidize and decompose organic matters in the sewage so as to achieve the purpose of removing pollutants;

designing parameters: sludge loading: 0.25 kgCOD/(kgMLSS. d); sludge concentration: 3000 mg/L; the structure of the tank body is as follows: steel concrete; designing the size: 16.0 multiplied by 14.0 multiplied by 6.0m, effective water depth 5.0m, 2 grids, and series operation. Effective volume: 1120m³. Residence time: and 38.4 h.

The corollary equipment:

1. roots blower: SSR150-150A, 2 stands, 1 stands with 1 stand, Q is 24.4m³Configuring a frequency converter for/min, 53.9kPa and 37kw for P;

2. a microporous aeration disc: 640 sets of silica gel is imported.

3. Aeration pipelines in the tank are 1 batch of ABS material.

4. Microorganism filler phi 150 x 2500mm, 560m³。

5. Dissolved oxygen detector, 2 sets.

1.3.9 first sedimentation tank 9

The functions are as follows: the solid-liquid separation in the waste water is realized through the gravity action, most suspended substances in the waste water are removed, the SS content of the effluent is ensured, and the quantity of microorganisms in the front end contacting the oxidation pond is ensured through a sludge reflux pump.

Design parameters

Designing the size: 6.0 multiplied by 6.5m, a vertical sedimentation tank is adopted; surface loading: 0.84m³/m²H settling time: 2 h; the structure is as follows: and (5) steel concrete.

Configuring equipment:

1. a central guide cylinder: 1, performing a chemical reaction on the raw materials,

preserving Q235;

2. sludge discharge pump and sludge external reflux pump: 65WQ25-15-2.2, Q25 m³H15 m, N2.2 kw,2 stands, 1 was prepared with 1.

1.3.10 air flotation system

The functions are as follows: solid-liquid separation is carried out in the wastewater through the gas dissolving effect, suspended substances in the wastewater are further removed, and the chromaticity of the wastewater is further reduced by adding PAC/PAM.

Design parameters

Designing the size: phi 4.0X 0.75 m. Designing the treatment capacity: 30-35m³H is used as the reference value. The structure is as follows: and the Q235 is corrosion-resistant. Residence time: 15 min;

configuring equipment:

super-efficient shallow air-float 1 set (comprising main machine system, dissolved air system, medicine-adding system and main machine electric control system)

1.4 Low (comprehensive) concentration wastewater System design

1.4.1 second mechanical grid 10

Designing parameters: designing the size: 8.00X 1.00X 1.50 m; the structure is as follows: steel concrete

Configuring equipment:

a rotary mechanical grating machine, HG600, 1.50KW N, 4000m H, 3mm of grating spacing, ABS, and SUS304 as a main body frame;

1.4.2 second equalizing basin 11

The functions are as follows: all low-concentration wastewater drained from the storage workshop is degraded under the action of mechanical stirring. Designing parameters: designing the size: 14.0 × 12.0 × 6.0 m; water inflow: 3700m³D; effective volume: 924m³(ii) a Residence time: 6.0 h; the structure is as follows: and (5) steel concrete.

The corollary equipment:

2. a lift pump, a self-suction pump, 100ZW100-15, Q100 m3/H, N7.5 KW, H15 m, a self-suction height of 5.5 m, 3 stands for 2, 1 stands for 2;

3. sensor liquid level controller, 1 set.

4. Flow meter, 0-150m³And h, 2 sets.

1.4.3 second hydrolytic acidification tank 12

Designing parameters: the design size of the second hydrolysis acidification tank 12 is as follows: l xB xH 25.0 × 14.0 × 6.0m, steel concrete 3 lattices, series operation, and pre-mixed reaction area. Total effective volume of the second hydrolysis acidification tank 12: 1820m³(ii) a Residence time: 10.0 h; volume load: 0.89kgCOD/m³D; the size of the mixing pool is as follows: l × B × H is 3.0 × 14.0 × 6.0m, and is made of steel concrete; effective volume: 210m³(ii) a Residence time: 1.2 h; configuring equipment:

the second hydrolysis acidification tank 12:

1. the submersible mixer is QJB4/12-620/3-480S, N is 4.0kw, 6 stands;

2. a guide plate 3 sets;

3. combined fillers,. phi.150X 2500, 875m³And comprises a bracket.

4. Dredge pump 80WQ40-15-4, Q40 m³H15 m, N4 kw,3 stands.

A mixing pool:

5. 1 set of perforation aeration stirring equipment, which is made of stainless steel;

1.4.4 second biological contact oxidation tank 13

The functions are as follows: the second biological contact oxidation pond 13 uses microorganisms to oxidize and decompose organic matters in the sewage, thereby achieving the purpose of removing pollutants;

designing parameters: sludge loading: 0.15 kgCOD/(kgMLSS. d); sludge concentration: 3000 mg/L; the structure of the tank body is as follows: steel concrete; designing the size: 35.0 multiplied by 16.0 multiplied by 6.0m, divided into 6 grids and operated in series; effective volume: 2800m³. Residence time: 15.27 h.

The corollary equipment:

1. roots blower: SSR175-200A, 3 stands, 2 stands with 1 stand, Q is 30.35m³Configuring a frequency converter for/min, 53.9kPa and P equal to 45 kw;

2. a microporous aeration disc: 1600 sets of silica gel inlet.

3. Aeration pipelines in the tank are 1 batch of ABS material.

4. Phi 150X 2500mm, 1400m of microbial packing³。

5. Dissolved oxygen detector, 6 sets.

1.4.5 second settling tank 14

Design parameters and design dimensions: 7.0 × 7.0 × 7.5m, 4 seats, adopting a vertical flow sedimentation tank; surface loading: 0.95m³/m²H; precipitation time: 2 h; the structure is as follows: and (5) steel concrete.

Configuring equipment:

1. a central guide cylinder: 4, the number of the table is 4,

preserving Q235;

2. sludge discharge pump and sludge external reflux pump: 80WQ40-15-4, Q ═ 48m³H13.3 m, N4 kw, 4 stands.

1.4.6 sludge thickening tank 15

The functions are as follows: the residual sludge and the air floatation scum generated by the storage system are further concentrated so as to facilitate the subsequent plate-and-frame filter press to press the sludge.

Design parameters and design dimensions: 6.0X 6.5 m. The structure is as follows: steel concrete; effective volume: 72m³；

Configuring equipment:

sludge feeding pump 65HFM-I-H-30-60, Q is 30m³H, N22 KW, H60 m, 2 stands, 1 stands by 1

1.4.7 second plate and frame Filter 16

The functions are as follows: and (4) carrying out solid-liquid separation on the residual sludge amount of the system, transporting the mud cakes outwards, and returning clear liquid to the low-concentration regulating reservoir.

Configuring equipment:

1. the second plate-and-frame filter press 16 XMZ100 is 100-1000-30U, N is 4kw, and the filtering area is 100m²The program-controlled automatic plate-pulling box-type filter press is provided with a plate-turning mud guide hopper.

2. The dosing device comprises 2 sets of dosing devices (PAC and PAM), a metering pump Q is 0-240L/h, N is 0.55KW, P is 0.6MPa, and PVDF pump heads are 2 sets.

1.5 Integrated houses

The sewage station comprehensive machine room comprises a laboratory room, an on-duty room, a fan room, an electric control room, a sludge dewatering room and a storage room;

designing the size: laboratory 4.0 × 6.0 × 4.0 m; office 4.0 × 6.0 × 4.0 m; the fan room is 12.0 multiplied by 6.0 multiplied by 4.0 m; the electric control room is 6.0 multiplied by 4.0 m; sludge dewatering room 13.0 × 6.0 × 8.0m (two layers); the storage room is 4.0 multiplied by 6.0 multiplied by 4.0 m.

The structure is as follows: mixing the steel concrete and the brick; quantity: 1 time of each; configuring equipment: axial flow fans, 15;

1.6 on-line monitoring room

On-line monitoring of the chamber plane size: lxb ═ 4.0 × 4.0 m; drainage well plane dimensions: lxb ═ 6.0 × 0.5 m: the structure is as follows: mixing the steel concrete and the brick; quantity: 1, seat; configuring equipment: COD on-line monitor, flow tank, etc.

1.7 sludge amount calculation

High concentration treatment part with water inlet amount of 700m³D, the SS content is 2000mg/L, the removal rate can meet the discharge requirement only when the removal rate reaches more than 98.5 percent, and the slag with the water content of 70 percent is produced by 4.6 tons every day; the lignin content in the high-concentration wastewater is 4000mg/L, and the removal rate of the high-concentration wastewater treated by the system is more than 90%, so that 8.4 tons of slag with 70% of water content are produced every day; the sludge yield and the water content of an anaerobic system in a high-concentration wastewater biochemical system are respectively 0.6 ton/d and 0.12 ton of residual sludge with 70 percent of water content, an aerobic system is designed according to the system, the BOD value of inlet water is 250mg/L, and the outlet water is 50mg/L, so that the slag with 70 percent of water content produced every day is 0.12 ton.

Design inflow 3700m of low-concentration wastewater³D, the SS content is 400mg/L, the removal rate can meet the discharge requirement only when the removal rate reaches more than 92.5 percent, and the slag with the water content of 70 percent is produced by 4.56 tons every day; the sludge yield and the water content of the hydrolysis system in the low-concentration wastewater biochemical system are respectively 0.5 ton/d and 0.54 ton of residual sludge with 70 percent of water content, the BOD value of inlet water of the aerobic system is 80mg/L and the BOD value of outlet water of the aerobic system is 20mg/L according to the system design, and the slag with 70 percent of water content is produced every day.

The amount of slag generated each day is as follows: 4.6+8.4+4.56 tonne; the amount of excess sludge produced per day was: 0.6+0.12+0.5+0.54 to 1.76 tons.

The main produced slag is caused by SS substances in raw water and lignin substances in high-concentration wastewater.

1.8 other device configuration description

1.8.1 dosing device

1) The treatment system dosing device at least comprises a nutrition dosing device (the nutrient substance is corn starch), a coagulant aid dosing device, a flocculating agent dosing device and an acid and alkali dosing device;

2) the volume of each type of medicine metering box at least meets the medicine dosage of 24 hours;

3) the inlet of the metering pump is provided with a filter screen, the outlet of the metering pump is provided with a pressure gauge, a safety valve, a check valve and the like which are resistant to solution corrosion, the stroke is 0-l 00 percent and can be adjusted, and the output force is 1.25 times of the maximum dosage. The metering precision at the maximum stroke (relative stroke is 100%) point is not lower than 0.5%;

4) the metering box is made of PE material or carbon steel material, and is provided with an electric stirrer when necessary;

5) each dosing device is respectively designed into a unit form, and a metering tank, a metering pump, a pipeline, a valve, an accessory and the like of each medicine are assembled on a chassis;

6) the pipeline and equipment principle of the dosing device adopts stainless steel or UPVC material;

7) a medicine mixer is arranged at each dosing point.

The scheme of the application is mainly divided into two main types of waste water, and the water quantity and the water quality conditions are shown in the following table 1:

TABLE 1

Table 2 shows the wastewater quality, which is specifically shown below:

TABLE 2

Table 3 is a statistical table of the effect of wastewater treatment

TABLE 3

The final effluent result of the wastewater reaches the standard A of Vietnam Ramie industry pollutant discharge standard, and the specific requirements are as shown in the following table 4:

TABLE 4

The above description is only for the purpose of illustrating the preferred embodiments of the present invention and is not to be construed as limiting the invention, and any modifications, equivalents, improvements and the like that fall within the spirit and principle of the present invention are intended to be included therein.

Claims

1. A ramie wastewater treatment process is characterized by comprising the following steps:

A. removing large particles from high-concentration wastewater through a first mechanical grid (1), then feeding the high-concentration wastewater into a first regulating tank (2), feeding the effluent into an acidification reaction tank (3) to regulate the pH value, and feeding the effluent into a first plate-and-frame filter press (4) to perform slag-water separation;

B. clear water discharged from a first plate-and-frame filter press (4) enters an intermediate tank (5) to adjust the pH value, discharged water enters a first hydrolysis acidification tank (6) to degrade organic matters, discharged water removes part of organic pollutants in wastewater through the respiration of anaerobic microorganisms in an IC anaerobic reactor (7), and then discharged water enters a first biological contact oxidation tank (8) to remove most of organic pollutants and ammonia nitrogen pollutants in the wastewater through the aerobic respiration and nitrification of aerobic microorganisms;

C. the effluent of the first biological contact oxidation tank (8) enters a first sedimentation tank (9) for sedimentation, the effluent enters a first air flotation system for precipitation, and a flocculating agent is added into the first air flotation system;

D. and (3) low-concentration wastewater enters a second regulating tank (11) through a second mechanical grid (10), the effluent of the second regulating tank (11) and the effluent of the air floatation system in the step C enter a second hydrolysis acidification tank (12) to degrade organic matters, the effluent enters a second biological contact oxidation tank (13) to remove most of organic pollutants and ammonia nitrogen pollutants in the wastewater, the effluent enters a second sedimentation tank (14) for sedimentation, the effluent enters a second air floatation system with a flocculating agent, the effluent enters a sludge concentration tank (15) for treatment, and finally the clear solution after flocculation and sedimentation of the effluent enters a second filter press frame (16) for treatment.

2. The ramie wastewater treatment process of claim 1, wherein in step A, the pH is controlled to 2-3.

3. The ramie wastewater treatment process of claim 1, wherein in step B, the pH is controlled to be 7-8.

4. The ramie wastewater treatment process of claim 1, wherein in steps C and D, the flocculant is PAC and PAM.

5. The ramie wastewater treatment process according to claim 1, wherein in the steps C and D, the first air flotation system comprises a first pipeline mixer (17) and a first high-efficiency shallow air flotation machine (18), the second air flotation system comprises a second pipeline mixer (19) and a second high-efficiency shallow air flotation machine (20), and the flocculating agent is added into the first pipeline mixer (17) and the second pipeline mixer (19) through a dosing pump respectively.

6. A ramie wastewater treatment system is characterized by comprising a first mechanical grating (1), a first water collecting tank (21), a first adjusting tank (2), an acidification reaction tank (3), a first plate-and-frame filter press (4), an intermediate tank (5), a first hydrolysis acidification tank (6), an IC anaerobic reactor (7), a first biological contact oxidation tank (8), a first sedimentation tank (9), a first air flotation system, a second mechanical grating (10), a second water collecting tank (22), a second adjusting tank (11), a second hydrolysis acidification tank (12), a second biological contact oxidation tank (13), a second sedimentation tank (14), a second air flotation system, a sludge concentration tank (15) and a second plate-and-frame filter press (16);

the first mechanical grating (1) is communicated with a first water collecting tank (21), a water outlet of the first water collecting tank (21) is communicated with a water inlet of a first adjusting tank (2) through a pipeline, a water outlet of the first adjusting tank (2) is communicated with a water inlet of an acidification reaction tank (3) through a pipeline, a water outlet of the acidification reaction tank (3) is communicated with a water inlet of a first plate and frame filter press (4) through a pipeline, a water outlet of the first plate and frame filter press (4) is communicated with a water inlet of an intermediate tank (5) through a pipeline, a water outlet of the intermediate tank (5) is communicated with a water inlet of a first hydrolysis and acidification tank (6) through a pipeline, a water outlet of the first hydrolysis and acidification tank (6) is communicated with a water inlet of an IC anaerobic reactor (7) through a pipeline, and a water outlet of the IC anaerobic reactor (7) is connected with a water inlet of a first biological contact oxidation tank (8) through a pipeline The water outlet of the first biological contact oxidation pond (8) is communicated with the water inlet of the first sedimentation pond (9) through a pipeline, the water outlet of the first sedimentation pond (9) is communicated with the water inlet of the first air flotation system through a pipeline, and the water outlet of the first air flotation system is communicated with the water inlet of the second hydrolysis acidification pond (12) through a pipeline;

the second mechanical grating (10) is communicated with the second water collecting tank (22), the water outlet of the second water collecting tank (22) is communicated with the water inlet of the second adjusting tank (11) through a pipeline, the water outlet of the second adjusting tank (11) is communicated with the water inlet of the second hydrolysis acidification tank (12) through a pipeline, the water outlet of the second hydrolysis acidification tank (12) is communicated with the water inlet of the second biological contact oxidation tank (13) through a pipeline, the water outlet of the second biological contact oxidation tank (13) is communicated with the water inlet of the second sedimentation tank (14) through a pipeline, the water outlet of the second sedimentation tank (14) is communicated with the water inlet of the second air flotation system through a pipeline, the water outlet of the second air flotation system is communicated with the water inlet of the sludge concentration tank (15) through a pipeline, and the water outlet of the sludge concentration tank (15) is communicated with the water inlet of the second plate and frame filter press (16) through a pipeline Are communicated with each other.

7. The ramie wastewater treatment system according to claim 6, wherein the first flotation system comprises a first pipeline mixer (17), a first high-efficiency shallow flotation machine (18) and two first dosing pumps (23), the water outlet of the first sedimentation tank (9) is communicated with the water inlet of the first pipeline mixer (17) through a pipeline, the water outlet of the first pipeline mixer (17) is communicated with the water inlet of the first high-efficiency shallow flotation machine (18) through a pipeline, the water outlet of the first high-efficiency shallow flotation machine (18) is communicated with the water inlet of the second hydrolysis acidification tank (12) through a pipeline, and the two first dosing pumps (23) are respectively communicated with the two dosing ports on the first pipeline mixer (17) through dosing pipelines.

8. The ramie wastewater treatment system according to claim 6, wherein the second air flotation system comprises a second pipeline mixer (19), a second high-efficiency shallow air flotation machine (20) and two second dosing pumps (24), the water outlet of the second sedimentation tank (14) is communicated with the water inlet of the second pipeline mixer (19) through a pipeline, the water outlet of the second pipeline mixer (19) is communicated with the water inlet of the second high-efficiency shallow air flotation machine (20) through a pipeline, the water outlet of the second high-efficiency shallow air flotation machine (20) is communicated with the water inlet of the sludge concentration tank (15) through a pipeline, and the two second dosing pumps (24) are respectively communicated with the two dosing ports on the second pipeline mixer (19) through dosing pipelines.

9. The ramie wastewater treatment system according to claim 8, further comprising a third pipeline mixer (25), wherein the water outlet of the sludge concentration tank (15) is communicated with the water inlet of the third pipeline mixer (25) through a pipeline, and the water outlet of the third pipeline mixer (25) is communicated with the water inlet of the second plate-and-frame filter press (16) through a pipeline.