CN115353262A - Esterification wastewater treatment process - Google Patents
Esterification wastewater treatment process Download PDFInfo
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- CN115353262A CN115353262A CN202211283094.9A CN202211283094A CN115353262A CN 115353262 A CN115353262 A CN 115353262A CN 202211283094 A CN202211283094 A CN 202211283094A CN 115353262 A CN115353262 A CN 115353262A
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- 238000000034 method Methods 0.000 title claims abstract description 40
- 230000032050 esterification Effects 0.000 title claims abstract description 34
- 238000005886 esterification reaction Methods 0.000 title claims abstract description 34
- 238000004065 wastewater treatment Methods 0.000 title claims abstract description 20
- 239000010802 sludge Substances 0.000 claims abstract description 133
- 238000002156 mixing Methods 0.000 claims abstract description 53
- 239000002351 wastewater Substances 0.000 claims abstract description 47
- 238000000108 ultra-filtration Methods 0.000 claims abstract description 31
- 238000005868 electrolysis reaction Methods 0.000 claims abstract description 24
- 230000003647 oxidation Effects 0.000 claims abstract description 22
- 238000007254 oxidation reaction Methods 0.000 claims abstract description 22
- 238000001556 precipitation Methods 0.000 claims abstract description 8
- 238000003756 stirring Methods 0.000 claims description 21
- 238000004062 sedimentation Methods 0.000 claims description 20
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 20
- IKHGUXGNUITLKF-UHFFFAOYSA-N Acetaldehyde Chemical compound CC=O IKHGUXGNUITLKF-UHFFFAOYSA-N 0.000 claims description 14
- 239000006228 supernatant Substances 0.000 claims description 9
- 239000005416 organic matter Substances 0.000 claims description 6
- 230000001105 regulatory effect Effects 0.000 claims description 6
- 239000012528 membrane Substances 0.000 claims description 5
- 230000035484 reaction time Effects 0.000 claims description 5
- 208000005156 Dehydration Diseases 0.000 claims description 4
- 230000018044 dehydration Effects 0.000 claims description 4
- 238000006297 dehydration reaction Methods 0.000 claims description 4
- 238000010979 pH adjustment Methods 0.000 claims description 3
- AXCZMVOFGPJBDE-UHFFFAOYSA-L calcium dihydroxide Chemical compound [OH-].[OH-].[Ca+2] AXCZMVOFGPJBDE-UHFFFAOYSA-L 0.000 claims description 2
- 229910001861 calcium hydroxide Inorganic materials 0.000 claims description 2
- 239000000920 calcium hydroxide Substances 0.000 claims description 2
- 230000003750 conditioning effect Effects 0.000 claims 1
- 230000029219 regulation of pH Effects 0.000 claims 1
- 239000000126 substance Substances 0.000 abstract description 8
- 239000003344 environmental pollutant Substances 0.000 abstract description 4
- 231100000719 pollutant Toxicity 0.000 abstract description 4
- 238000005265 energy consumption Methods 0.000 abstract description 2
- 235000015097 nutrients Nutrition 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 13
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 6
- 239000007788 liquid Substances 0.000 description 5
- 229920000728 polyester Polymers 0.000 description 5
- 238000007605 air drying Methods 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- XEEYBQQBJWHFJM-UHFFFAOYSA-N iron Substances [Fe] XEEYBQQBJWHFJM-UHFFFAOYSA-N 0.000 description 3
- 229910052742 iron Inorganic materials 0.000 description 3
- -1 iron ions Chemical class 0.000 description 3
- MHAJPDPJQMAIIY-UHFFFAOYSA-N Hydrogen peroxide Chemical compound OO MHAJPDPJQMAIIY-UHFFFAOYSA-N 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 2
- 238000003487 electrochemical reaction Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 125000001997 phenyl group Chemical group [H]C1=C([H])C([H])=C(*)C([H])=C1[H] 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- CWYNVVGOOAEACU-UHFFFAOYSA-N Fe2+ Chemical compound [Fe+2] CWYNVVGOOAEACU-UHFFFAOYSA-N 0.000 description 1
- 239000003513 alkali Substances 0.000 description 1
- 150000001491 aromatic compounds Chemical class 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000007717 exclusion Effects 0.000 description 1
- 229910001448 ferrous ion Inorganic materials 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 235000016709 nutrition Nutrition 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 231100000614 poison Toxicity 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000003440 toxic substance Substances 0.000 description 1
- 231100000419 toxicity Toxicity 0.000 description 1
- 230000001988 toxicity Effects 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F9/00—Multistage treatment of water, waste water or sewage
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/02—Treatment of water, waste water, or sewage by heating
- C02F1/04—Treatment of water, waste water, or sewage by heating by distillation or evaporation
- C02F1/048—Purification of waste water by evaporation
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
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- C02F1/28—Treatment of water, waste water, or sewage by sorption
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/30—Treatment of water, waste water, or sewage by irradiation
- C02F1/302—Treatment of water, waste water, or sewage by irradiation with microwaves
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
- C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
- C02F1/46104—Devices therefor; Their operating or servicing
- C02F1/46176—Galvanic cells
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- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
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- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F2001/007—Processes including a sedimentation step
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- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/30—Organic compounds
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- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/36—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from the manufacture of organic compounds
- C02F2103/38—Polymers
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- C02F3/02—Aerobic processes
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Abstract
The invention discloses an esterification wastewater treatment process, which belongs to the field of wastewater treatment and comprises the following steps: the method comprises the steps of air stripping, sludge mixing, precipitation, ultrafiltration, micro-electrolysis, microwave treatment, anaerobic treatment, contact oxidation and MBR treatment, the sludge mixing tank is utilized to carry out sectional treatment on pollutants in the esterification wastewater, the precipitation part is subjected to microwave treatment to destroy the stability of refractory organic matters, the sludge is cracked while the biodegradability of the wastewater is improved, the micro-wastewater provides necessary nutrient substances, the other part of wastewater is subjected to ultrafiltration and micro-electrolysis treatment to directly improve the biodegradability of the wastewater, and finally the anaerobic treatment, contact oxidation and MBR treatment are carried out, so that the aim of esterification wastewater with low energy consumption and high efficiency biochemical treatment is fulfilled.
Description
Technical Field
The invention relates to the field of wastewater treatment, in particular to an esterification wastewater treatment process.
Background
The esterification wastewater is various wastewater generated in the polyester production process, has complex components, low pH and high COD, but has poor biodegradability due to a large amount of aromatic compounds and oligomers contained in the wastewater. The traditional treatment method of the esterification wastewater is to burn organic matters after steam stripping, so as to recover heat and save part of fuel. However, such waste water contains acetaldehyde and ethylene glycol, which causes waste due to burning, and also generates highly toxic substances due to incomplete combustion in the burning process, so if the biodegradability of the esterification waste water can be improved, the realization of the biochemical treatment of the waste water is the key point for solving the problem of difficult treatment of the esterification waste water.
However, the esterification wastewater has low content of N and P, so that the normal nutritional requirement of biochemical treatment is difficult to maintain, meanwhile, the biodegradability of COD is further reduced due to the recovery of acetaldehyde and ethylene glycol, and the toxicity of the wastewater is high due to the existence of a benzene ring structure in the wastewater, so that the possibility of biochemical treatment is further reduced.
Chinese patent No. CN111039511B discloses a modular integrated process for treating chemical recovery wastewater, which utilizes a pretreatment module, a biochemical module and an advanced treatment module to treat esterification wastewater, however, the process utilizes fenton reaction and electrochemical reaction to degrade refractory organics, thereby improving the biodegradability of wastewater, but a large amount of hydrogen peroxide, ferrous ions and the like need to be added, so that not only is the treatment cost greatly improved, but also iron ions can be introduced into wastewater, and simultaneously, a large amount of energy is consumed during electrochemical reaction. The final treatment cost is very high, and the wide-range popularization is difficult.
Therefore, the problem to be solved at present is to provide an esterification wastewater treatment process which can realize low energy consumption and high-efficiency biochemical treatment.
Disclosure of Invention
The embodiment of the invention provides an esterification wastewater treatment process, which comprises the following steps:
(1) Gas stripping: introducing esterification wastewater and steam into a stripping tower for treatment, wherein the heat transfer medium of the stripping tower is steam, introducing organic matter gas and steam collected at the tower top into an acetaldehyde rectifying tower, and collecting wastewater at the tower bottom of the stripping tower;
(2) Sludge mixing: conveying the waste water collected at the bottom of the gas stripping tower to a sludge mixing tank, and adding excess sludge into the sludge mixing tank, wherein a plurality of stirring devices are arranged in the sludge mixing tank, the stirring speed of each stirring device is 300-800r/min, the mixing time is 20-30min, and the adding amount of the excess sludge is 20-40g/L based on the dry weight of the sludge;
(3) And (3) precipitation: conveying the mixed liquid in the sludge mixing tank to a sedimentation tank for sedimentation treatment, wherein the sedimentation time is 1-3h;
(4) And (3) ultrafiltration: conveying the supernatant in the sedimentation tank to an ultrafiltration device for ultrafiltration treatment, wherein the ultrafiltration device adopts PAN and PVDP membranes, and the working pressure is 0.2-0.4MPa;
(5) Micro-electrolysis: conveying the water outlet of the ultrafiltration device to a micro-electrolysis process for treatment;
(6) Microwave treatment: conveying the sludge mixed liquor settled in the settling tank to a microwave treatment process for microwave treatment, wherein the power of the microwave treatment is 700-1000W, and the reaction time is 7-10 min;
(7) Anaerobic treatment: conveying the sludge mixed liquor after the microwave treatment and the micro-electrolysis effluent to an anaerobic tank for anaerobic treatment;
(8) Contact oxidation: conveying the anaerobic effluent to a contact oxidation tank for treatment;
(9) MBR: and (4) conveying the effluent of the contact oxidation to an MBR tank for treatment.
Further, sludge generated in the anaerobic tank, the contact oxidation tank and the MBR tank is conveyed to a plate-and-frame filter for dehydration treatment to obtain dehydrated sludge, and the water content of the dehydrated sludge is 75-80%.
Further, the residual sludge added in the sludge mixing tank is dewatered sludge.
Further, air-drying the dewatered sludge to obtain air-dried sludge, wherein the water content of the air-dried sludge is 40-50%.
Further, the air-dried sludge is added into the sludge mixing tank, and the dry weight ratio of the added amount of the air-dried sludge to the dehydrated sludge is (1).
Further, concentrated water generated by the ultrafiltration device is conveyed to the microwave treatment process.
Further, the dewatered sludge is firstly added into the sludge mixing tank, then stirred and mixed for 10-15min, and then air-dried sludge is added into the sludge mixing tank for stirring and mixing.
Further, the sludge mixed liquor after the microwave treatment and the micro-electrolysis effluent are conveyed to an adjusting tank for pH adjustment before entering an anaerobic tank, and the pH is adjusted to 6-8.
Further, calcium hydroxide is added into the adjusting tank to adjust the pH value.
Further, the supernatant of the adjusting tank is conveyed to the anaerobic tank.
Compared with the prior art, according to the scheme of the embodiment of the invention, a sludge mixing process is arranged, in the sludge mixing process, sludge can adsorb organic pollutants in wastewater, dewatered sludge and dried sludge are added step by step under the stirring effect, and macromolecular pollutants in the wastewater are adsorbed on the surface of the sludge through the adsorption effect and the sedimentation effect;
conveying the sludge mixed liquor after precipitation separation to a microwave treatment process, wherein under the action of microwaves, benzene ring structures on the surface of the sludge are opened, and microbial cells of the sludge are cracked under the action of microwaves, so that the content of nutrient substances in the wastewater is increased, and the biodegradability of the wastewater is further improved;
after the supernatant of the sedimentation tank is subjected to ultrafiltration treatment, the ultrafiltration effluent is subjected to micro-electrolysis treatment to further reduce the concentration of pollutants in the wastewater, a small amount of iron ions are generated in the micro-electrolysis process, the micro-electrolysis effluent and the sludge mixed liquid after microwave treatment enter a regulating tank and are subjected to alkali addition regulation, a sedimentation reaction occurs in the regulating tank, and part of pollutants can be separated into the wastewater by settled floc; meanwhile, the effluent of the regulating tank meets the treatment conditions of the anaerobic tank, so that the anaerobic treatment, the contact oxidation and the normal MBR treatment can be realized;
the sludge mixed liquid after microwave treatment is mixed with micro-electrolysis effluent, and the pH value of the sludge mixed liquid is adjusted, so that iron ions entering wastewater in the micro-electrolysis process can be removed, large particle substances in sludge are reduced, and the content of solid substances in the wastewater is reduced.
Drawings
FIG. 1 is a schematic diagram of an esterification wastewater treatment process according to an embodiment of the present invention;
FIG. 2 is a schematic view of an esterification wastewater treatment process according to an embodiment of the present invention.
Detailed Description
The following detailed description of the present invention is provided in conjunction with the accompanying drawings, but it should be understood that the scope of the present invention is not limited to the specific embodiments.
Throughout the specification and claims, unless explicitly stated otherwise, the term "comprise" or variations such as "comprises" or "comprising", etc., will be understood to imply the inclusion of a stated element or component but not the exclusion of any other element or component.
Example 1
Esterification wastewater generated by a certain polyester chemical industry enterprise: pH2-3, COD29000-32000mg/L, see figure 1;
(1) Gas stripping: the esterification wastewater and steam enter a stripping tower for treatment, the heat transfer medium of the stripping tower is steam, the organic matter gas and the steam collected at the tower top enter an acetaldehyde rectification tower, and the wastewater is collected at the tower bottom of the stripping tower, wherein the COD is 5800mg/L and the BOD is BOD 5 /COD<0.1;
(2) Sludge mixing: conveying the waste water collected at the bottom of the gas stripping tower to a sludge mixing tank, and adding excess sludge into the sludge mixing tank, wherein a plurality of stirring devices are arranged in the sludge mixing tank, the stirring speed of each stirring device is 300-800r/min, the mixing time is 20-30min, and the adding amount of the excess sludge is 20-40g/L based on the dry weight of the sludge;
(3) And (3) precipitation: conveying the mixed liquid in the sludge mixing tank to a sedimentation tank for sedimentation treatment, wherein the sedimentation time is 1-3h;
(4) And (3) ultrafiltration: conveying the supernatant in the sedimentation tank to an ultrafiltration device for ultrafiltration treatment, wherein the ultrafiltration device adopts PAN and PVDP membranes, and the working pressure is 0.2-0.4MPa;
(5) Micro-electrolysis: conveying the water outlet of the ultrafiltration device to a micro-electrolysis process for treatment;
(6) Microwave treatment: conveying the sludge mixed liquor settled in the settling pond to a microwave treatment process for microwave treatment, wherein the power of the microwave treatment is 700-1000W, and the reaction time is 7-10 min;
(7) Anaerobic treatment: conveying the sludge mixed liquor after the microwave treatment and the micro-electrolysis effluent to an anaerobic tank for anaerobic treatment;
(8) Contact oxidation: conveying the anaerobic effluent to a contact oxidation tank for treatment;
(9) MBR: conveying the effluent of the contact oxidation to an MBR tank for treatment;
and (3) water outlet condition: pH6.0-7.5, COD93mg/L.
Example 2
Esterification wastewater generated by a certain polyester chemical industry enterprise: pH2-3, COD29000-32000mg/L;
(1) Gas stripping: the esterification wastewater and steam enter a stripping tower for treatment, the heat transfer medium of the stripping tower is steam, the organic matter gas and the steam collected at the tower top enter an acetaldehyde rectification tower, and the wastewater is collected at the tower bottom of the stripping tower, wherein the COD is 5800mg/L and the BOD is BOD 5 /COD<0.1;
(2) Sludge mixing: conveying the waste water collected at the bottom of the gas stripping tower to a sludge mixing pool, and simultaneously adding excess sludge into the sludge mixing pool, wherein a plurality of stirring devices are arranged in the sludge mixing pool, the stirring speed of each stirring device is 300-800r/min, the mixing time is 20-30min, and the adding amount of the excess sludge is 20-40g/L based on the dry weight of the sludge; conveying sludge generated in the anaerobic tank, the contact oxidation tank and the MBR tank to a plate-and-frame filter for dehydration treatment to obtain dehydrated sludge, wherein the water content of the dehydrated sludge is 75-80%; the excess sludge added into the sludge mixing tank is dewatered sludge; air-drying the dewatered sludge to obtain air-dried sludge, wherein the water content of the air-dried sludge is 40-50%, the air-dried sludge is also added into the sludge mixing tank, and the dry-weight ratio of the added amount of the air-dried sludge to the dewatered sludge is 1-5; adding the dehydrated sludge into the sludge mixing tank, stirring and mixing for 10-15min, and then adding air-dried sludge for stirring and mixing;
(3) And (3) precipitation: conveying the mixed liquor in the sludge mixing tank to a sedimentation tank for sedimentation for 1-3h;
(4) And (3) ultrafiltration: conveying the supernatant in the sedimentation tank to an ultrafiltration device for ultrafiltration treatment, wherein the ultrafiltration device adopts PAN and PVDP membranes, and the working pressure is 0.2-0.4MPa;
(5) Micro-electrolysis: conveying the water outlet of the ultrafiltration device to a micro-electrolysis process for treatment;
(6) Microwave treatment: conveying the sludge mixed liquor settled in the settling tank to a microwave treatment process for microwave treatment, wherein the power of the microwave treatment is 700-1000W, and the reaction time is 7-10 min;
(7) Anaerobic treatment: conveying the sludge mixed liquor after the microwave treatment and the micro-electrolysis effluent to an anaerobic tank for anaerobic treatment;
(8) Contact oxidation: conveying the anaerobic effluent to a contact oxidation tank for treatment;
(9) MBR: conveying the effluent of the contact oxidation to an MBR tank for treatment;
and (3) water outlet condition: pH6.3-7.3, COD68mg/L.
Example 3
Esterification wastewater generated by a certain polyester chemical industry enterprise: pH2-3, COD29000-32000mg/L, see figure 2;
(1) Gas stripping: the esterification wastewater and steam enter a stripping tower for treatment, the heat transfer medium of the stripping tower is steam, the organic matter gas and the steam collected at the top of the stripping tower enter an acetaldehyde rectifying tower, and the organic matter gas and the steam enter a rectification towerWaste water is collected at the bottom of the stripping tower, COD is 5800mg/L, BOD 5 /COD<0.1;
(2) Sludge mixing: conveying the waste water collected at the bottom of the gas stripping tower to a sludge mixing tank, and adding excess sludge into the sludge mixing tank, wherein a plurality of stirring devices are arranged in the sludge mixing tank, the stirring speed of each stirring device is 300-800r/min, the mixing time is 20-30min, and the adding amount of the excess sludge is 20-40g/L based on the dry weight of the sludge; conveying sludge generated in the anaerobic tank, the contact oxidation tank and the MBR tank to a plate-and-frame filter for dehydration treatment to obtain dehydrated sludge, wherein the water content of the dehydrated sludge is 75-80%; the excess sludge added into the sludge mixing tank is dewatered sludge; air-drying the dewatered sludge to obtain air-dried sludge, wherein the water content of the air-dried sludge is 40-50%, the air-dried sludge is also added into the sludge mixing tank, and the dry-weight ratio of the added amount of the air-dried sludge to the dewatered sludge is 1-5; adding the dehydrated sludge into the sludge mixing tank, stirring and mixing for 10-15min, and then adding air-dried sludge for stirring and mixing;
(3) And (3) precipitation: conveying the mixed liquor in the sludge mixing tank to a sedimentation tank for sedimentation for 1-3h;
(4) And (3) ultrafiltration: conveying the supernatant in the sedimentation tank to an ultrafiltration device for ultrafiltration treatment, wherein the ultrafiltration device adopts PAN and PVDP membranes, and the working pressure is 0.2-0.4MPa;
(5) Micro-electrolysis: conveying a water outlet of the ultrafiltration device to a micro-electrolysis process for treatment;
(6) Microwave treatment: conveying the sludge mixed liquor settled in the settling pond to a microwave treatment process for microwave treatment, wherein the power of the microwave treatment is 700-1000W, and the reaction time is 7-10 min;
(7) Anaerobic treatment: conveying the sludge mixed liquor subjected to microwave treatment and the micro-electrolysis effluent to an adjusting tank for pH adjustment before entering an anaerobic tank, adjusting the pH to 6-8, and conveying the supernatant of the adjusting tank to the anaerobic tank;
(8) Contact oxidation: conveying the anaerobic effluent to a contact oxidation tank for treatment;
(9) MBR: conveying the effluent of the contact oxidation to an MBR tank for treatment;
and (4) water outlet condition: pH6.7-7.3, COD52mg/L.
Example 4
On the basis of example 3, domestic sewage is added into a regulating tank, and the volume ratio of the domestic sewage to the polyester production wastewater is 1.
And (3) water outlet condition: pH6.7-7.3, COD27mg/L.
The foregoing description of specific exemplary embodiments of the invention has been presented for the purposes of illustration and description. It is not intended to limit the invention to the precise form disclosed, and obviously many modifications and variations are possible in light of the above teaching. The exemplary embodiments were chosen and described in order to explain certain principles of the invention and its practical application to enable one skilled in the art to make and use various exemplary embodiments of the invention and various alternatives and modifications as are suited to the particular use contemplated. It is intended that the scope of the invention be defined by the claims and their equivalents.
Claims (10)
1. An esterification wastewater treatment process is characterized by comprising the following steps:
(1) Gas stripping: introducing esterification wastewater and steam into a stripping tower for treatment, wherein the heat transfer medium of the stripping tower is steam, introducing organic matter gas and steam collected at the tower top into an acetaldehyde rectifying tower, and collecting wastewater at the tower bottom of the stripping tower;
(2) Sludge mixing: conveying the waste water collected at the bottom of the gas stripping tower to a sludge mixing tank, and adding excess sludge into the sludge mixing tank, wherein a plurality of stirring devices are arranged in the sludge mixing tank, the stirring speed of each stirring device is 300-800r/min, the mixing time is 20-30min, and the adding amount of the excess sludge is 20-40g/L based on the dry weight of the sludge;
(3) And (3) precipitation: conveying the mixed liquor in the sludge mixing tank to a sedimentation tank for sedimentation for 1-3h;
(4) And (3) ultrafiltration: conveying the supernatant in the sedimentation tank to an ultrafiltration device for ultrafiltration treatment, wherein the ultrafiltration device adopts PAN and PVDP membranes, and the working pressure is 0.2-0.4MPa;
(5) Micro-electrolysis: conveying the water outlet of the ultrafiltration device to a micro-electrolysis process for treatment;
(6) Microwave treatment: conveying the sludge mixed liquor settled in the settling pond to a microwave treatment process for microwave treatment, wherein the power of the microwave treatment is 700-1000W, and the reaction time is 7-10 min;
(7) Anaerobic treatment: conveying the sludge mixed liquor after the microwave treatment and the micro-electrolysis effluent to an anaerobic tank for anaerobic treatment;
(8) Contact oxidation: conveying the anaerobic effluent to a contact oxidation tank for treatment;
(9) MBR: and (4) conveying the effluent of the contact oxidation to an MBR tank for treatment.
2. The esterification wastewater treatment process according to claim 1, wherein the sludge generated in the anaerobic tank, the contact oxidation tank and the MBR tank is conveyed to a plate-and-frame filter for dehydration treatment to obtain dehydrated sludge, and the water content of the dehydrated sludge is 75-80%.
3. The esterification wastewater treatment process according to claim 2, wherein the excess sludge added to the sludge mixing tank is the dewatered sludge.
4. The esterification wastewater treatment process according to claim 2, wherein the dewatered sludge is air-dried to obtain air-dried sludge having a water content of 40 to 50%.
5. The esterification wastewater treatment process according to claim 4, wherein the air-dried sludge is further added into the sludge mixing tank, and the dry weight ratio of the added amount of the air-dried sludge to the dehydrated sludge is 1.
6. The esterification waste water treatment process according to claim 1, wherein the concentrated water produced by the ultrafiltration apparatus is fed to the microwave treatment process.
7. The esterification wastewater treatment process according to claim 4 or 5, wherein the dewatered sludge is added to the sludge mixing tank, stirred and mixed for 10-15min, and then air-dried sludge is added to the sludge mixing tank, and stirred and mixed.
8. The esterification wastewater treatment process according to claim 1, wherein the sludge mixed liquor after the microwave treatment and the micro-electrolysis effluent are conveyed to a regulating tank for pH regulation before entering an anaerobic tank, and the pH is regulated to 6 to 8.
9. The esterification wastewater treatment process according to claim 8, wherein the pH adjustment is performed by adding calcium hydroxide to the adjustment tank.
10. The esterification wastewater treatment process of claim 8, wherein the conditioning tank supernatant is delivered to the anaerobic tank.
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