CN215480368U - Biphenyl alcohol waste water treatment system - Google Patents

Biphenyl alcohol waste water treatment system Download PDF

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CN215480368U
CN215480368U CN202022963747.0U CN202022963747U CN215480368U CN 215480368 U CN215480368 U CN 215480368U CN 202022963747 U CN202022963747 U CN 202022963747U CN 215480368 U CN215480368 U CN 215480368U
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process system
tank
fenton
sludge
baf
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梁志霞
张晓晨
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Beijing Fangyuan Environmental Engineering Co ltd
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Beijing Fangyuan Environmental Engineering Co ltd
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Abstract

The utility model relates to a biphenyl alcohol production wastewater treatment system, which comprises an adjusting tank (1), an iron-carbon micro-electrolysis process system (2), a front Fenton process system (3), an air flotation process system (4), a biochemical process system (5), a rear Fenton process system (6), a BAF process system (7), a deep denitrification process system (8), an MBR membrane process system (9) and a sludge treatment system (12), wherein wastewater sequentially passes through the components and then is discharged, and sludge generated by operation enters the sludge treatment system (12); the method is suitable for treating the waste water generated in the production of the biphenylalcohol through physicochemical treatment, biochemical treatment and advanced oxidation treatment of the sewage.

Description

Biphenyl alcohol waste water treatment system
Technical Field
The utility model relates to a biphenyl alcohol production wastewater treatment system, relates to physicochemical treatment, biochemical treatment and advanced oxidation of sewage, is suitable for biphenyl alcohol production wastewater treatment, and belongs to the field of environmental protection.
Background
Biphenyl alcohol, also known as 2-methyl-3-hydroxymethyl biphenyl, is an important basic chemical raw material and is an intermediate of the insecticide bifenthrin. The production of the biphenyl alcohol takes 6-dichlorotoluene as a raw material, bromoethane as an initiator, and the raw material reacts with magnesium in a THF solvent to generate a Grignard reagent, and then the Grignard reagent and bromobenzene are coupled by a catalyst, the Grignard reagent and the bromobenzene, and the coupling material is prepared by hydrolysis and rectification; the coupling material is subjected to formatting reaction, addition reaction and reduction reaction to prepare the biphenyl alcohol product.
High-concentration wastewater can be generated in the production process of the biphenylalcohol, wastewater pollutants mainly comprise pH, COD, ammonia nitrogen, SS, methylbenzene, chloride, tetrahydrofuran, biphenyls, chlorobenzenes and salt, and the pollutants can cause great harm to the environment. Aiming at the problem that the wastewater is difficult to effectively treat by adopting a single physical, chemical or biological method, and the effluent requirement can be met only by combining multiple processes.
Disclosure of Invention
The utility model aims to provide a diphenoxyl production wastewater treatment system with a good treatment effect.
The scheme provided by the utility model is as follows: a waste water treatment system for biphenyl alcohol production comprises an adjusting tank (1), an iron-carbon micro-electrolysis process system (2), a front Fenton process system (3), an air floatation process system (4), a biochemical process system (5), a rear Fenton process system (6), a BAF process system (7), a deep denitrification process system (8), an MBR membrane process system (9) and a sludge treatment system (12), waste water sequentially passes through the adjusting tank (1), the iron-carbon micro-electrolysis process system (2), the front Fenton process system (3), the air floatation process system (4), the biochemical process system (5), the rear Fenton process system (6), the BAF process system (7), the deep denitrification process system (8) and the MBR membrane process system (9), and water is discharged, and sludge generated by operation enters the sludge treatment system (12).
The waste water produced in the production of the biphenylalcohol is firstly balanced in water quality and water quantity through a regulating reservoir (1) and adjusted to have the PH value of 2-3, and is sent to an iron-carbon micro-electrolysis process system (2) through a regulating reservoir lifting pump (11), wherein the iron-carbon micro-electrolysis process system (2) is provided with an iron-carbon filler (21) and an aeration device. The aeration gas-water ratio is 100-200%. The iron-carbon filler (21) is a filler which has large specific surface area, good adsorption performance, high mechanical strength, long service life, stable physical and chemical properties, difficult passivation and hardening and can be activated and recycled, and a closed loop is formed in acidic sewage by utilizing the electrode potential difference between the fillers, so that countless micro primary batteries are formed and further electrochemical reaction occurs. The aeration device provides sufficient dissolved oxygen for the sewage. Under the combined action of the organic compound and the inorganic compound, a plurality of organic compounds and inorganic compounds in the sewage undergo oxidation-reduction reaction, degraded macromolecular substances are micromolecules, the chemical structure of toxic organic compounds is destroyed, the toxicity of the sewage is reduced, and the biodegradability of the wastewater is improved.
The effluent of the iron-carbon micro-electrolysis process system (2) enters a front Fenton process system (3) and sequentially passes through a front Fenton tank (31), a front neutralization tank (32) and a front sedimentation tank (33) of the front Fenton process system (3). The front Fenton tank (31) is provided with a hydrogen peroxide dosing device (101) and a ferrous sulfate dosing device (102) to dose medicaments into the tank, the front neutralization tank (32) is provided with a sodium hydroxide dosing device (105) to dose alkali liquor, the PH of the sewage is adjusted to 6.5-9.5, and the sewage enters the air floatation process system (4).
The effluent of the air floatation process system (4) enters a biochemical process system (5) and sequentially passes through a UASB buffer tank (51), a UASB anaerobic tank (52), an anaerobic sedimentation tank (53), a primary anoxic tank (54), a primary aerobic tank (55), a secondary anoxic tank (56), a secondary aerobic tank (57) and a high-density sedimentation tank (58) of the biochemical process system (5). The UASB buffer pool (51) is provided with a heat exchange coil pipe (511) and a UASB water inlet pump (512). Adjusting the nutrient proportion and the PH of the wastewater in an UASB buffer tank (51), keeping the pH in a reasonable range, heating the wastewater to 35-45 ℃, and then feeding the wastewater into an UASB anaerobic tank (52), wherein a water distribution device (521), a steam-water separator (523) and a methane treatment device (534) are arranged at the top of the tank. The pool is internally provided with a three-phase separator (522) and a sludge discharge device (525). The wastewater passes through complete anaerobism in the UASB anaerobic tank (52), is assisted to be in a proper temperature range and pH control range, various pollutants in the wastewater are further degraded by microorganisms in anaerobic sludge, organic pollutants in the wastewater are greatly removed, and generated biogas, sludge and effluent are separated through a three-phase separator (522). The marsh gas enters a steam-water separator (523) and a marsh gas treatment device (534), sludge is left in the tank, and effluent enters an anaerobic tank (53). The effluent carries a part of sludge, and the sludge is precipitated in the anaerobic tank (53) and then flows back to the UASB anaerobic tank (52). The effluent of the anaerobic sedimentation tank (53) is distributed into a primary anoxic tank (54) and a secondary anoxic tank (56) in a proportion range of 3-5: 1. The residence time ratio of the first-stage anoxic tank (54) to the first-stage aerobic tank (55) is 1: 2-3, and the residence time ratio of the first-stage anoxic tank (54) to the second-stage anoxic tank (56) is 1: 3. The reflux ratio of the nitrifying liquid is 150-250%. The sludge in the high-density sedimentation tank (58) flows back to the first-level anoxic tank (54), and the sludge reflux ratio is 50-100%.
The effluent of the biochemical process system (5) still contains a certain amount of refractory pollutants, and the effluent of the biochemical process system (5) enters a post-Fenton process system (6). The post-Fenton process system (6) comprises an acid adjusting tank (61), a post-Fenton tank (62), post-neutralization tanks (63) (63) and a post-sedimentation tank (64). The sewage enters a post-Fenton pool (62) after the PH value of the sewage is adjusted to 3-4 in an acid adjusting pool (61), and the reaction effluent enters a post-sedimentation pool (64) after the PH value of the reaction effluent is adjusted to 7-9 in a neutralization pool.
And the effluent of the post-Fenton process system (6) enters a BAF process system (7). The BAF process system (7) comprises a BAF buffer pool (71) and a BAF biological filter pool (72). BAF filler (721) is arranged in the BAF biological filter (72), and pollutants in the sewage are removed by utilizing the microbial oxidative decomposition effect in a biological membrane attached to the BAF filler (721), the adsorption and retention effects of the BAF filler (721) and the microbial membrane, the food chain graded predation effect formed along the water flow direction and the denitrification effect of a microenvironment in the microbial membrane.
Effluent of the BAF process system (7) enters a deep denitrification process system (8), and the deep denitrification process system (8) comprises a deep denitrification tank (81) and a deep dephosphorization tank (82).
Effluent of the deep denitrification process system (8) enters an MBR (membrane bioreactor) membrane process system (9), and the MBR membrane process system (9) comprises an MBR membrane tank (91) and a clean water tank (92). The MBR membrane tank (91) is provided with an MBR curtain type membrane (911) for filtering impurities in water and improving the quality of the outlet water.
A certain amount of sludge is generated in the sewage treatment process, the sludge is periodically discharged into a sludge tank for concentration and volume reduction, then the sludge is treated by a sludge treatment system (12), the sludge is concentrated and then discharged into a filter press (125) by a filter press mud pump (123), mud cakes after mud-water separation enter a sludge dryer (126) for drying and volume reduction, and then the sludge cakes are treated outside. The filtrate returns to the biochemical process system (5) to continue to receive circulating and re-processing. The filter pressing sludge inlet pump (123) adopts a pneumatic diaphragm pump and is provided with an air compressor (124).
The process system has reasonable integral process design and good effluent quality, and can effectively reduce the pollution of the waste water from the production of the biphenylalcohol to the environment.
Drawings
FIG. 1 is a process flow diagram of the present invention;
fig. 2 is a structural arrangement diagram of an example of the present invention.
In fig. 2: 1. a regulating tank, 2, an iron-carbon micro-electrolysis process system, 3, a front Fenton process system, 4, an air flotation process system, 5, a biochemical process system, 6, a rear Fenton process system, 7, a BAF process system, 8, a deep denitrification process system, 9, an MBR membrane process system, 12, a sludge disposal system, 11, a regulating tank lift pump, 21, iron-carbon filler, 31, a front Fenton tank, 32, a front neutralization tank, 33, a front sedimentation tank, 331, a sludge discharge pump, 41, an air flotation buffer tank, 411, an air flotation lift pump, 42, a dissolved air flotation device, 421 air flotation discharge pump, 51, an UASB buffer tank, 511 coil heat exchange, 512, an UASB water inlet pump, 52, an UASB anaerobic tank, 521, a water distribution device, 522, a three-phase separator, 523, a steam-water separator, 524, a methane treatment device, 53, a sludge discharge device, 53, a 531, a sludge return pump, 54, a primary anoxic tank, 541, a submersible mixer, 55. a primary aerobic tank 551, a liftable aerator 56, a secondary anoxic tank 57, a secondary aerobic tank 58, a high-density sedimentation tank 61, an acid regulating tank 62, a post-Fenton tank 63, a post-neutralization tank 64, a post-sedimentation tank 71.BAF buffer tank 711, a BAF water inlet pump 712, a BAF backwashing pump 72, a BAF biological filter tank 721, BAF filler 81, a deep denitrification tank 82, a deep dephosphorization tank 91, an MBR membrane tank 911, an MBR curtain membrane 92, a clear water tank 921, an effluent pump 101, a hydrogen peroxide dosing device 102, a ferrous sulfate dosing device 103, a PAM dosing device 104, a PAC dosing device 105, a sodium hydroxide dosing device 106, a dilute dosing sulfuric acid device 107, a denitrifier dosing device 108, a dephosphorizing agent dosing device 111, a micro electrolysis Fenton air supply fan 111, a biochemical reaction air supply fan 112, a 113, a deep treatment air supply fan 121, a chemical sludge tank, 122. a biochemical sludge pool, 123, a filter-pressing sludge inlet pump, 124, an air compressor, 125, a filter press, 126 and a sludge dryer.
Detailed Description
The present invention is described in detail by way of an example.
The major business of Cangzhou biological science and technology limited company is chemical product production, retail sale and the like, a production base of 1200 tons of terpineol is newly built, and the quality of the production wastewater CODGr、NH3The indexes of-N are 18000mg/L and 150mg/L respectively, and the indexes of CODCr and NH3-N after treatment reach 105mg/L and 18mg/L respectively.
The process production wastewater of each production workshop is firstly sent into an iron-carbon micro-electrolysis process system (2) after the pH value is regulated to 2-3 by a construction unit, and the iron-carbon micro-electrolysis process system (2) is provided with an iron-carbon filler (21) and an aeration device. The aeration gas-water ratio is 180 percent. The iron-carbon filler (21) is a filler which has large specific surface area, good adsorption performance, high mechanical strength, long service life, stable physical and chemical properties, difficult passivation and hardening and can be activated and recycled, and a closed loop is formed in acidic sewage by utilizing the electrode potential difference between the fillers, so that countless micro primary batteries are formed and further electrochemical reaction occurs. Aeration provides sufficient dissolved oxygen for the sewage. Under the combined action of the organic compound and the inorganic compound, a plurality of organic compounds and inorganic compounds in the sewage undergo redox reaction, degraded macromolecular substances are micromolecules, the chemical structure of toxic organic compounds is destroyed, the toxicity of the sewage is reduced, and the biodegradability of the wastewater is improved.
The effluent of the iron-carbon micro-electrolysis process system (2) enters a front Fenton process system (3) and sequentially passes through a front Fenton tank (31), a front neutralization tank (32) and a front sedimentation tank (33) of the front Fenton process system (3). The front Fenton tank (31) is provided with a hydrogen peroxide dosing device (101), a ferrous sulfate dosing device (102) adds a medicament into the tank, the front neutralization tank (32) is provided with a sodium hydroxide dosing device (105) to add alkali liquor, the PH of the sewage is adjusted to 6.5-9.5, the sewage enters the front sedimentation tank (33), the front sedimentation tank (33) is provided with a PAM dosing device (103) and a PAC dosing device (104) to add the medicament into a water inlet end, and the water discharged from the front sedimentation tank (33) enters the air flotation process system (4). The sludge in the front sedimentation tank (33) is discharged into the chemical sludge tank (121) through a sludge discharge pump (331).
The air floatation process system (4) is provided with an air floatation buffer tank (41) and an air dissolving air floatation device (42), and factory domestic sewage enters the air floatation buffer tank (41) to be uniformly mixed with production wastewater and then enters the air dissolving air floatation device (42) to remove most suspended matters. The dissolved air flotation device (42) is provided with a PAM dosing device (103) and a PAC dosing device (104) to feed medicaments to the water inlet end, so that the treatment efficiency is improved.
The effluent of the air floatation process system (4) is lifted to a biochemical process system (5) through an air floatation lifting pump (421), and sequentially passes through a UASB buffer tank (51), a UASB anaerobic tank (52), an anaerobic sedimentation tank (53), a primary anoxic tank (54), a primary aerobic tank (55), a secondary anoxic tank (56), a secondary aerobic tank (57) and a high-density sedimentation tank (58) of the biochemical process system (5). The UASB buffer pool (51) is provided with a heat exchange coil pipe (511) and a UASB water inlet pump (512). The wastewater is adjusted in the UASB buffer pool (51) to the nutrition proportion of the wastewater, the PH is kept in a reasonable range, and the wastewater is heated to 40 ℃ and then is lifted to a water distribution device (521) at the top of the UASB anaerobic pool (52) by a UASB water inlet pump (512). The three-phase separator (522) and the sludge discharge device (523) are arranged in the tank, wastewater passes through complete anaerobism in the UASB anaerobic tank (52), various pollutants in the wastewater are further degraded by microorganisms in anaerobic sludge in an appropriate temperature range and pH control range in an auxiliary manner, organic pollutants in the wastewater are greatly removed, and generated biogas, sludge and effluent are separated through the three-phase separator (522). The marsh gas enters a steam-water separator (523) and a marsh gas treatment device (534), sludge is left in the tank, and effluent enters an anaerobic tank (53). The effluent carries a part of sludge, and the sludge is precipitated in the anaerobic tank (53) and then flows back to the UASB anaerobic tank (52). The effluent of the anaerobic sedimentation tank (53) is distributed into a first-stage anoxic tank (54) and a second-stage anoxic tank (56) in a proportion range of 4: 1. The residence time of the anoxic tank and the aerobic tank is in a ratio range of 1:2.5, and the residence time of the primary anoxic tank (54) and the secondary anoxic tank (56) is in a ratio of 1: 3. The reflux ratio of the nitrifying liquid is 200 percent. The sludge in the high-density sedimentation tank (58) flows back to the first-level anoxic tank (54), and the sludge reflux ratio is 100 percent. Sludge discharged by the air floatation process system (4) and the biochemical process system (5) enters a biochemical sludge tank (122).
The effluent of the biochemical process system (5) still contains a certain amount of refractory pollutants, and the effluent of the biochemical process system (5) enters a post-Fenton process system (6). The post-Fenton process system (6) comprises an acid adjusting tank (61), a post-Fenton tank (62), a post-neutralization tank (63) and a post-sedimentation tank (64). The acid adjusting tank (61) is provided with a dilute sulfuric acid dosing device (106) for dosing acid liquor, sewage enters the rear Fenton tank (62) after the pH value of the sewage is adjusted to 3-4 in the acid adjusting tank (61), the rear Fenton tank (62) is provided with a hydrogen peroxide dosing device (101) and a ferrous sulfate dosing device (102) for dosing agents into the tank, and effluent enters the rear sedimentation tank (64) after the pH value of the effluent is adjusted to 7-9 in the rear neutralization tank (63). The post-neutralization tank (63) is provided with a sodium hydroxide dosing device (105) for dosing alkali liquor. The rear sedimentation tank (64) is provided with a PAM dosing device (103) and a PAC dosing device (104) for dosing the medicament to the water inlet end, and the outlet water of the rear sedimentation tank (64) enters the BAF process system (7). And the sludge in the post-sedimentation tank (64) is discharged into the chemical sludge tank (121) through a sludge discharge pump (331).
The BAF process system (7) comprises a BAF buffer pool (71) and a BAF biological filter pool (72). BAF filler (721) is arranged in the BAF biological filter (72), and pollutants in the sewage are removed by utilizing the microbial oxidative decomposition effect in a biological membrane attached to the BAF filler (721), the adsorption and retention effects of the BAF filler (721) and the microbial membrane, the food chain graded predation effect formed along the water flow direction and the denitrification effect of a microenvironment in the microbial membrane. BAF backwashing drains to a primary aerobic tank (55).
Effluent of the BAF process system (7) enters a deep denitrification process system (8), and the deep denitrification process system (8) comprises a deep denitrification tank (81) and a deep dephosphorization tank (82). The deep denitrification tank (81) and the deep dephosphorization tank (82) are respectively provided with a denitrifying agent dosing device (107) and a dephosphorizing agent dosing device (108) for dosing agents into the tanks.
Effluent of the deep denitrification process system (8) enters an MBR (membrane bioreactor) membrane process system (9), and the MBR membrane process system (9) comprises an MBR membrane tank (91) and a clean water tank (92). The MBR membrane tank (91) is provided with an MBR curtain type membrane (911) for filtering impurities in water and improving the quality of the outlet water. A BAF backwashing pump (721) is arranged in the clean water tank (92) to provide clean water for BAF backwashing, and an external drainage pump (921) is additionally arranged to externally drain the clean water reaching the standard to a plant pipe network.
Sludge in the biochemical sludge pool (122) and the chemical sludge pool (121) is concentrated and then is discharged into a filter press (125) through a filter press mud pump (123), and mud cakes after mud-water separation enter a sludge dryer (126) to be dried and volume-reduced and then are treated outside. The filtrate returns to the biochemical process system (5) to continue to receive circulating and re-processing. The filter pressing sludge inlet pump (123) adopts a pneumatic diaphragm pump and is provided with an air compressor (124). The filter press (125) adopts a high-pressure diaphragm filter press, and the water content of the treated mud cake can reach 65 percent.
The process system has reasonable integral process design and good effluent quality, and reduces the pollution of the waste water from the production of the biphenylalcohol to the environment.
The above examples are intended to illustrate the utility model in detail, and it should be understood that the practice of the utility model is not limited to these illustrations. For those skilled in the art to which the utility model pertains, several simple deductions or substitutions can be made without departing from the spirit of the utility model, and all shall be considered as belonging to the protection scope of the utility model.

Claims (10)

1. The utility model provides a biphenyl alcohol waste water treatment system which characterized in that: the system comprises an adjusting tank (1), an iron-carbon micro-electrolysis process system (2), a front Fenton process system (3), an air floatation process system (4), a biochemical process system (5), a rear Fenton process system (6), a BAF process system (7), a deep denitrification process system (8), an MBR membrane process system (9) and a sludge disposal system (12), wherein wastewater sequentially passes through the adjusting tank (1), the iron-carbon micro-electrolysis process system (2), the front Fenton process system (3), the air floatation process system (4), the biochemical process system (5), the rear Fenton process system (6), the BAF process system (7), the deep denitrification process system (8) and the MBR membrane process system (9) to be discharged, and sludge generated by operation enters the sludge disposal system (12).
2. The diphenoxyl production wastewater treatment system according to claim 1, characterized in that: the iron-carbon micro-electrolysis process system (2) is internally provided with a micro-electrolysis filler and an aeration device.
3. The diphenoxyl production wastewater treatment system according to claim 1, characterized in that: the iron-carbon micro-electrolysis process system (2) goes out water and gets into preceding fenton process system (3), and preceding fenton process system (3) are including preceding fenton pond (31), preceding neutralization pond (32) and preceding sedimentation tank (33), preceding fenton pond (31) set up hydrogen peroxide charge device (101) and ferrous sulfate charge device (102), preceding neutralization pond (32) set up sodium hydroxide charge device (105).
4. The diphenoxyl production wastewater treatment system according to claim 1, characterized in that: and the effluent of the front Fenton process system (3) enters the air floatation process system (4).
5. The diphenoxyl production wastewater treatment system according to claim 1, characterized in that: the effluent of the air floatation process system (4) enters a biochemical process system (5) and sequentially passes through a UASB buffer tank (51), a UASB anaerobic tank (52), an anaerobic sedimentation tank (53), a primary anoxic tank (54), a primary aerobic tank (55), a secondary anoxic tank (56), a secondary aerobic tank (57) and a high-density sedimentation tank (58) of the biochemical process system (5); the UASB buffer tank (51) is provided with a heat exchange coil (511) and an UASB water inlet pump (512), and the top of the UASB anaerobic tank (52) is provided with a water distribution device (521), a steam-water separator (523) and a methane treatment device (534); the three-phase separator (522) is arranged in the tank, the garbage sludge discharging device (525) is arranged in the tank, the wastewater is distributed to enter the first-stage anoxic tank (54) and the second-stage anoxic tank (56), and the sludge in the high-density sedimentation tank (58) flows back to the first-stage anoxic tank (54).
6. The diphenoxyl production wastewater treatment system according to claim 1, characterized in that: biochemical processes system (5) goes out water and gets into back fenton process system (6), back fenton process system (6) are including transferring sour pond (61), back fenton pond (62), back neutralization pond (63) and back sedimentation tank (64), it sets up dilute sulfuric acid charge device (106) to transfer sour pond (61), back fenton pond (62) set up hydrogen peroxide charge device (101), ferrous sulfate charge device (102), back neutralization pond (63) set up sodium hydroxide charge device (105), back sedimentation tank (64) are equipped with PAM charge device (103) and PAC charge device (104), and the play water gets into BAF process system (7).
7. The diphenoxyl production wastewater treatment system according to claim 1, characterized in that: the BAF process system (7) comprises a BAF buffer water tank (71) and a BAF biological filter (72), wherein a BAF filler (721) is arranged in the BAF biological filter (72).
8. The diphenoxyl production wastewater treatment system according to claim 1, characterized in that: effluent of the BAF process system (7) enters a deep denitrification process system (8), and the deep denitrification process system (8) comprises a deep denitrification tank (81) and a deep dephosphorization tank (82).
9. The diphenoxyl production wastewater treatment system according to claim 1, characterized in that: effluent of the deep denitrification process system (8) enters an MBR (membrane bioreactor) membrane process system (9), the MBR membrane process system (9) comprises an MBR membrane tank (91) and a clean water tank (92), and the MBR membrane tank (91) is provided with an MBR curtain type membrane (911).
10. The diphenoxyl production wastewater treatment system according to claim 1, characterized in that: the sludge treatment system (12) comprises a filter-pressing sludge inlet pump (123), a filter press (125) and a sludge dryer (126), wherein the filter-pressing sludge inlet pump (123) adopts a pneumatic diaphragm pump and is provided with an air compressor (124).
CN202022963747.0U 2020-12-11 2020-12-11 Biphenyl alcohol waste water treatment system Active CN215480368U (en)

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