CN113292210B

CN113292210B - Ultramicro filter membrane manufacturing wastewater treatment process

Info

Publication number: CN113292210B
Application number: CN202110847190.0A
Authority: CN
Inventors: 陈福泰; 刘兴甜; 杨艳
Original assignee: Beijing Qingda Guohua Film Technology Co ltd; Go Higher Environment Group Co ltd
Current assignee: Beijing Qingda Guohua Film Technology Co ltd; Go Higher Environment Group Co ltd
Priority date: 2021-07-27
Filing date: 2021-07-27
Publication date: 2021-11-26
Anticipated expiration: 2041-07-27
Also published as: CN113292210A

Abstract

The application relates to the field of membrane preparation wastewater treatment, and particularly discloses an ultramicro filter membrane preparation wastewater treatment process, which comprises the following steps: filtering; concentrating, namely putting the filtered filtrate into an environment with the vacuum degree of-95.5 to-90 kPa and the temperature of 35 to 48 ℃ for evaporation and concentration, condensing the evaporated material to obtain evaporated condensate and residual concentrated solution, and stopping concentrating when the weight of the obtained condensate reaches 90 to 95 percent of the weight of the filtrate; condensate treatment, namely sequentially carrying out micro-electrolysis treatment and biochemical treatment on the condensate; or the condensate is directly reused in the film-making production. The method has the advantages of conveniently treating the membrane-making wastewater and recycling valuable components of the membrane-making wastewater.

Description

Ultramicro filter membrane manufacturing wastewater treatment process

Technical Field

The application relates to the field of membrane preparation wastewater treatment, in particular to an ultramicro filter membrane preparation wastewater treatment process.

Background

Membrane separation technology is an emerging technology for separating, concentrating and purifying substances. The membrane separation technology can realize separation under the condition of maintaining the environment of an original biological system, can efficiently concentrate and enrich products, effectively remove impurities, has convenient operation, compact structure, low energy consumption, simplified process and no secondary pollution, does not need to add chemicals, and gradually becomes a basic unit operation process in food industry, medicine and sewage treatment.

The ultra-micro filtration separation membrane of the membrane separation system is usually prepared by a non-solvent induced phase separation method, wherein a large amount of pollutants including solvent pollutants, organic additive pollutants, inorganic additive pollutants, partial polymers and the like exist in membrane preparation wastewater.

Generally, at least 5-10 t of film-making wastewater is generated per 1000 square meters of film. The membrane-making wastewater contains a solvent with higher concentration, the COD of the wastewater is generally more than 2 ten thousand ppm, the biodegradability is poor, and the wastewater cannot be treated to the discharge standard by the traditional biological treatment technology; in order to solve the above problems, a treatment process for treating membrane-making wastewater and recovering valuable components therein is urgently needed.

Disclosure of Invention

In order to conveniently treat the membrane-making wastewater and recycle valuable components thereof, the application provides an ultramicro-filtration membrane-making wastewater treatment process.

The application provides an ultramicro filter membrane preparation wastewater treatment process which adopts the following technical scheme:

an ultramicro filter membrane manufacturing wastewater treatment process comprises the following steps:

filtering;

concentrating, namely putting the filtered filtrate into an environment with the vacuum degree of-95.5 to-90 kPa and the temperature of 35 to 48 ℃ for evaporation and concentration, condensing the evaporated material to obtain evaporated condensate and residual concentrated solution, and stopping concentrating when the weight of the obtained condensate reaches 90 to 95 percent of the weight of the filtrate;

condensate treatment, namely sequentially carrying out micro-electrolysis treatment and biochemical treatment on the condensate; or the condensate is directly reused in the film-making production.

In one embodiment the vacuum of the environment in the concentration step may be-92 kPa and the temperature may be 45 ℃.

By adopting the technical scheme, the filtered filtrate is poured into the concentration tank, and is decompressed and heated, so that the moisture in the filtrate can be evaporated, and the aim of concentrating the solvent pollutants in the wastewater is fulfilled; the second aspect reduces the condition that the solvent in the filtrate is mixed in the condensate along with the evaporation of the water vapor, and reduces the content of organic matters in the condensate; in the third aspect, the organic matter in the wastewater is not easy to polymerize at a lower temperature, thereby facilitating the separation and reuse of the solvent.

The quality of the condensate obtained after low-temperature and low-pressure concentration is obviously improved, but the COD value in the condensate is still higher, generally about 1500-3500 ppm, the B/C value is often less than 0.03, the condensate cannot be directly subjected to biochemical treatment at the moment, and the condensate needs to be further treated by micro-electrolysis. After micro-electrolysis treatment, the COD value of the condensate is further reduced, and the B/C value is increased to about 0.35, so that biochemical treatment can be carried out, and the emission standard is reached.

Preferably, the micro-electrolysis process comprises:

adjusting the pH value of the condensate to 2-3, adding the condensate into an iron-carbon micro-electrolysis filler, aerating for 10-60 min, and controlling the gas-water ratio to be 2-5: 1, obtaining an electrolytic processing liquid.

As a preferred embodiment, the gas-water ratio can also be 2.5-3.5: 1.

preferably, the iron-carbon micro-electrolysis filler comprises, by weight, 60-75 parts of iron powder, 8-15 parts of carbon powder, 3-10 parts of copper powder and 10-20 parts of an additive.

In a preferred embodiment, the iron-carbon micro-electrolysis filler comprises 70 parts of iron powder, 12 parts of carbon powder, 5 parts of copper powder and 10 parts of additives by weight.

By adopting the technical scheme, after the condensing agent is introduced into the iron-carbon micro-electrolysis filler, the iron powder is used as the anode and the carbon powder is used as the cathode in an acidic environment, so that a potential difference is generated, organic components in the condensate are decomposed, the content of the organic components in the condensate is reduced, and subsequent biochemical treatment is conveniently carried out.

The inventor finds that the electrolytic efficiency is accelerated by selecting and proportioning the components, the copper powder can serve as a cathode after being added, so that the decomposition of the iron powder is further accelerated, the situation that the iron powder generates inertia after being oxidized for a long time is reduced due to the addition of the copper powder, and the production efficiency is improved.

Preferably, the additive comprises silicon carbide, aluminum oxide, bismuth oxide and titanium dioxide, and the corresponding weight ratio is 1-3: 3:3: 3.

By adopting the technical scheme, the addition of the additive further improves the electrolysis efficiency and reduces the organic content in the condensate.

Preferably, a Fenton oxidation treatment is further included between the step micro-electrolysis treatment and the step biochemical treatment,

adjusting the pH value of the electrolytic treatment solution to 3-4, adding a hydrogen peroxide aqueous solution, aerating for 10-30 min, and controlling the gas-water ratio to be 2-4: 1, obtaining an oxidation treatment liquid.

Preferably, the concentration of the aqueous hydrogen peroxide solution is 30v%, and the amount of the hydrogen peroxide is 0.5-1 wt% of the electrolytic treatment solution.

By adopting the technical scheme, hydrogen peroxide reacts with Fe under acidic condition²⁺And hydroxyl free radicals with oxidizing capability are generated through reaction, and organic matters in the electrolytic treatment liquid are further treated, so that the oxidation treatment liquid subjected to Fenton oxidation treatment can enter a biochemical sludge tank and then is more easily decomposed by microorganisms in activated sludge, and the quality of wastewater treatment is improved.

Preferably, the biochemical treatment comprises the steps of adjusting the pH value of the condensate supernatant subjected to micro-electrolysis treatment or the condensate supernatant subjected to Fenton oxidation treatment to 8-9, then, allowing the condensate supernatant to enter a biochemical sludge tank for biochemical degradation, filtering the degraded condensate by an MBR membrane, and pumping out to obtain reuse water.

Particularly, a precipitation process is arranged between the micro-electrolysis treatment or the Fenton oxidation treatment and the biochemical treatment, liquid after the micro-electrolysis treatment or the Fenton oxidation enters the precipitation tank for precipitation, and the pH value in the precipitation tank is controlled to be 8-9. The liquid is kept stand in a sedimentation tank, so that ferric hydroxide generated by micro-electrolysis reaction and Fenton oxidation reaction is precipitated, impurities in the oxidation treatment liquid are further removed through coagulation during precipitation, and the supernatant after precipitation enters a biochemical sludge tank for biochemical treatment.

The microorganisms in the biochemical sludge tank carry out biochemical degradation on the wastewater, so that the content of organic matters in the wastewater is further reduced, and the wastewater after biochemical degradation is filtered by an MBR membrane and then pumped out, so that the discharge standard is reached. The operation of biochemical treatment is simple, the amount of treated wastewater is large, the cost is low, the treated wastewater can be discharged, and the environmental pollution is reduced.

Preferably, the concentrated solution is subjected to rectification treatment.

Preferably, after the rectification is completed, the residue at the bottom of the tower is incinerated.

Because only one solvent is usually considered to be added in the production, the content of the solvent in the treated wastewater is single, and workers can select different temperature stages according to the use of the solvent to evaporate the corresponding solvent.

If the temperature of the tower bottom is 145-152 ℃, recovering the dimethylformamide, and if the temperature of the tower bottom exceeds 152 ℃, stopping recovering;

if the temperature of the tower bottom is 165-167 ℃, recovering the dimethylacetamide, and if the temperature of the tower bottom exceeds 167 ℃, stopping recovering;

when the temperature of the tower bottom is 200-202 ℃, recovering the N-methyl pyrrolidone mixture, and when the temperature of the tower bottom exceeds 202 ℃, stopping recovering;

by adopting the technical scheme, the concentrated solution can be rectified to recover the solvent, and the recovered solvent can be reused for production, thereby reducing the production cost and lightening the environmental pollution. The residue at the bottom of the tower is mainly a small amount of organic impurities (mainly additives and polymers of a film-making formula) which are difficult to separate, and can be directly incinerated, so that the pollution of the organic impurities to the environment is reduced.

Preferably, the precision of the filter used for filtering is 0.1-30 μm.

By adopting the technical scheme, the method has the advantages that,

1. the method adopts a reduced pressure concentration method, water is evaporated at low temperature under the negative pressure environment, the membrane-making wastewater is concentrated, and the temperature during evaporation is lower, so that the overflow of an organic solvent in the membrane-making wastewater is reduced, the reaction of active ingredients in the membrane-making wastewater is reduced, the concentrated solution after concentration has economic value, can be directly sold to a unit with a receiving quality, the organic solvent can also be recovered through rectification, the condensate can be directly recycled to the production of the same membrane, and can be further treated to reach the discharge or recycling standard. Through the above treatment modes, effective ingredients in the membrane preparation wastewater can be fully utilized, the wastewater is treated, the environment is protected, and the membrane preparation wastewater treatment difficulty and the membrane preparation wastewater treatment energy consumption are reduced.

2. The preferred specific vacuum degree and the temperature ratio of adopting in this application for the impurity content is few in the condensate water that extracts, thereby is convenient for the little electrolytic treatment in later stage, fenton oxidation treatment, biochemical treatment, has improved the treatment effeciency and the treatment quality of membrane preparation waste water.

3. The iron-carbon micro-electrolysis filler with a specific proportion is preferably adopted, so that the purification capacity of the iron-carbon micro-electrolysis treatment process is improved, and the quality of the reuse water is further improved.

Drawings

Fig. 1 is a flow chart of a method provided herein.

Detailed Description

The present application will be described in further detail with reference to fig. 1 and the examples.

Preparation example of iron-carbon micro-electrolytic Filler

Preparation method of iron-carbon micro-electrolysis filler

Feeding iron powder, carbon powder, copper powder, silicon carbide, aluminum oxide, bismuth oxide and titanium dioxide in proportion, adding deionized water accounting for 5 percent of the total weight of the iron powder, the carbon powder, the copper powder, the silicon carbide, the aluminum oxide, the bismuth oxide and the titanium dioxide, fully stirring and mixing, and calcining the mixed material at 850 ℃ for 90 min.

Preparation examples 1 to 3 the following components were used:

components

Iron powder

Carbon powder

Copper powder

Silicon carbide

Alumina oxide

Bismuth oxide

Titanium dioxide

Preparation example 1

70g

12g

3g

1g

3g

Preparation example 2

70g

12g

5g

1g

3g

Preparation example 3

70g

12g

10g

1g

3g

Comparative preparation example 1

The difference from preparation example 2 is that no copper powder was added in this comparative preparation example.

Comparative preparation example 2

The difference from preparation example 2 is that equal weight of manganese powder was used instead of copper powder in this comparative preparation example.

The treatment of a film-forming waste water was carried out by using dimethylacetamide as an organic solvent, and the film-forming waste water had COD26140ppm and BOD100ppm and was a pale yellow translucent aqueous solution.

Examples

Example 1

filtering; and (3) introducing the membrane-making wastewater into a filter for filtering, wherein the precision of the filter is 30 mu m.

Concentrating, evaporating and concentrating the filtered filtrate in an environment with vacuum degree of-92 kPa and temperature of 48 ℃, condensing and collecting the evaporated product to obtain evaporated condensate and residual concentrated solution, and stopping concentrating when the weight of the obtained condensate reaches 95% of the weight of the filtrate;

and the condensate treatment comprises micro-electrolysis treatment and biochemical treatment which are sequentially carried out on the condensate.

Micro-electrolysis treatment:

adjusting the pH value of the condensate to 2, adding the condensate into the iron-carbon micro-electrolysis filler, wherein the weight ratio of the condensate to the iron-carbon micro-electrolysis filler is 2:1, introducing air at a constant speed, and aerating for 60min at a gas-water ratio of 3: 1; obtaining an electrolytic treatment liquid, and selecting the filler obtained in the preparation example 1 as the iron-carbon micro-electrolytic filler.

And (3) precipitation treatment:

and (3) allowing the electrolysis treatment solution after micro-electrolysis treatment to enter a sedimentation tank for sedimentation, and controlling the pH value in the sedimentation tank to be 9. The electrolytic treatment liquid is kept standing and layered in the sedimentation tank.

Biochemical treatment:

and regulating the pH value of supernatant after precipitation and stratification to 8.5, then feeding the supernatant into a biochemical sludge tank for biochemical degradation, filtering the supernatant through an MBR membrane after degradation, and pumping out the supernatant to obtain reuse water, wherein the filtering precision of the MBR membrane is 0.1 mu m.

Rectification treatment of the concentrated solution:

since the organic solvent in the film-making wastewater is unique and definite (dimethylacetamide).

Heating the concentrated solution during rectification; when the temperature of the tower bottom is 164-166 ℃, recovering distillate (the main component is dimethylacetamide), and stopping rectification when the temperature of the tower bottom exceeds 166 ℃;

after the rectification is finished, burning the residue at the bottom of the tower.

Example 2

The difference from example 1 is that the iron-carbon microelectrolytic filler used in this example was the filler obtained from preparation 2.

Example 3

The difference from example 1 is that the iron-carbon microelectrolytic filler used in this example was the filler obtained in preparation example 3.

Example 4

The difference from example 2 is that in the concentration process of this example, the concentration is carried out by evaporation under the environment of-92 kPa and 45 ℃.

Example 5

The difference from example 2 is that in the concentration process of this example, the concentration is carried out by evaporation under an environment of-95 kPa and 45 ℃.

Example 6

The difference from the example 2 is that in the concentration process of the example, the concentration is carried out by evaporation under the environment that the environmental vacuum degree is-92 kPa and the temperature is 40 ℃.

Example 7

The difference from example 4 is that in the concentration process of this example, the concentration is carried out by evaporation under the environment of-92 kPa and 35 ℃.

Example 8

The difference from example 5 is that this example is in the concentration process. Evaporating and concentrating at 45 deg.C under-90 kPa.

Example 9

Concentrating, evaporating and concentrating the filtered filtrate in an environment with vacuum degree of-92 kPa and temperature of 45 ℃, condensing and collecting the evaporated product to obtain evaporated condensate and residual concentrated solution, and stopping concentrating when the weight of the obtained condensate reaches 95% of the weight of the filtrate;

and the condensate treatment comprises micro-electrolysis treatment, Fenton oxidation treatment and biochemical treatment which are sequentially carried out on the condensate.

Micro-electrolysis treatment:

adjusting the pH value of the condensate to 2, adding the condensate into the iron-carbon micro-electrolysis filler, wherein the weight ratio of the condensate to the iron-carbon micro-electrolysis filler is 2:1, and aerating for 60min, wherein the gas-water ratio during aeration is 3: 1; obtaining an electrolytic treatment liquid, and selecting the filler obtained in the preparation example 2 as the iron-carbon micro-electrolysis filler.

Fenton oxidation treatment:

adjusting the pH value of the electrolytic treatment solution to 3-4, adding aqueous hydrogen peroxide, and aerating for 30min at a gas-water ratio of 3:1 to obtain an oxidation treatment solution.

The concentration of the aqueous hydrogen peroxide solution was 30% by volume, and the amount of hydrogen peroxide was 1% by weight based on the electrolytic treatment solution.

And (3) precipitation treatment:

and introducing the oxidation treatment liquid into a sedimentation tank, adjusting the pH value to 9, and standing, settling and layering.

Biochemical treatment:

and adjusting the pH value of the supernatant after the precipitation to 8.5, then feeding the supernatant into a biochemical sludge tank for biochemical degradation, filtering the supernatant by an MBR membrane after the degradation, and then pumping out the supernatant to obtain reuse water, wherein the filtering precision of the MBR membrane is 0.1 mu m.

Rectification treatment of the concentrated solution:

Heating the concentrated solution during rectification;

Comparative example 1

The difference from example 2 is that this comparative example uses the iron-carbon microelectrolytic filler obtained in comparative preparation example 1.

Comparative example 2

The difference from example 2 is that this comparative example uses the iron-carbon microelectrolytic filler obtained in comparative preparation example 2.

In a comparative example 3,

the difference from example 2 is that the concentration step of this comparative example was carried out at ambient temperature of 100 c under normal pressure.

Comparative example 4

The difference from example 2 is that the concentration step of this comparative example was carried out under an ambient vacuum of-84 kPa and at an ambient temperature of 57 deg.C

Performance test

Detection method/test method

Respectively detecting the water quality of the condensed liquid and the water used for reuse after biochemical treatment, wherein the detection of the water quality of the condensed liquid comprises Chemical Oxygen Demand (COD), Biochemical Oxygen Demand (BOD), chroma and turbidity; the quality detection of the reuse water Comprises Oxygen Demand (COD), Biochemical Oxygen Demand (BOD), total nitrogen and turbidity.

The detection method is from the corresponding detection method disclosed in Water and wastewater monitoring and analyzing method (fourth edition), Chinese environmental science publishers.

TABLE 1 Water quality testing of condensed liquids after concentration

Group of	COD(ppm)	BOD(ppm)	Color intensity	Turbidity (FTU)
					Example 1	1926	51.1	6	0.13
Example 2	1927	51.1	6	0.13
					Example 3	1927	51.0	6	0.13
Example 4	1792	50.2	5	0.10
					Example 5	2049	53.6	5	0.15
Example 6	1802	50.3	5	0.10
					Example 7	1804	52.4	5	0.11
Example 8	1876	50.4	5	0.12
					Example 9	1794	50.2	5	0.11
Comparative example 1	1927	51.1	5	0.11
					Comparative example 2	1927	51.1	5	0.11
Comparative example 3	8764	175.7	42	2.41
					Comparative example 4	5004	111.2	31	1.67

TABLE 2 quality testing of reuse water

Group of	COD(ppm)	BOD(ppm)	Total nitrogen (mg/L)	Turbidity (FTU)
					Example 1	55.9	23.0	4	0.12
Example 2	44.3	18.5	3	0.11
					Example 3	52.0	21.4	4	0.12
Example 4	41.2	17.3	3	0.1
					Example 5	47.1	18.6	3	0.18
Example 6	41.5	17.1	3	0.12
					Example 7	41.8	16.8	3	0.16
Example 8	43.1	18.4	3	0.14
					Example 9	16.5	8.4	3	0.14
Comparative example 1	67.4	23.4	14	0.25
					Comparative example 2	65.5	22.9	12	0.2
Comparative example 3	201.6	54.2	25	0.26
					Comparative example 4	115.1	33.8	18	0.22

It can be seen from the combination of examples 1, 2 and 3 and comparative examples 1 and 2 and the combination of table 2 that the microelectrolysis efficiency is improved and the water quality is improved by selecting a specific iron-carbon microelectrolysis filler proportion, and the difference of the iron-carbon microelectrolysis fillers with different proportions mainly lies in the addition of copper powder and the selection of the addition amount of the copper powder. The inventor of the application finds that the conductive capacity of the iron-carbon micro-electrolysis filler is improved after the copper powder is added, so that the electrolysis efficiency is accelerated, the copper powder is added to serve as the cathode of an electrolytic cell, the electrolysis efficiency is improved, the promotion of inertia of iron powder after being oxidized for a long time is reduced, so that the micro-electrolysis filler can still keep higher electrolysis efficiency after being used for a long time, and the water quality of condensate after micro-electrolysis treatment is improved.

It can be seen from the embodiment 2 and the comparative examples 3 and 4 that the treatment difficulty of the membrane-making wastewater can be obviously simplified and the quality of the treated condensed water and the reuse water can be improved by adopting a low-pressure and low-temperature concentration mode. The possibility of producing such effect is that under the low pressure microthermal environment, the boiling point disparity of organic solvent and water is great to easily separate water and organic solvent through the evaporation, secondly, some polymer membrane making materials that contain in the waste water are difficult for reacting at low temperature, have reduced the thick gellan gum of concentrate, the unable condition of effectively separating solvent and polymer membrane making material. Meanwhile, evaporation is carried out under the condition of low temperature, thereby being beneficial to reducing energy consumption and saving energy.

As can be seen from the examples 2, 4, 5, 6 and 7, when the vacuum degree is-92 kPa, the condensate obtained by concentration at the ambient temperature of 45 ℃ has better water quality, and the condensate carries less organic solvent, thereby facilitating the biochemical treatment at the later stage. As can be seen from examples 4, 5 and 8, the condensed water obtained by concentration had the best quality when the degree of vacuum was-92 kPa in an atmosphere maintained at 45 ℃ during concentration.

It can be seen from examples 4 and 9 that the addition of the fenton oxidation treatment further improves the quality of the treated reuse water, and the electrolytic treatment solution is subjected to the fenton oxidation treatment to further oxidize the internal organic substances, thereby improving the quality of the obtained reuse water.

In the light of the above example 10,

an ultramicro filter membrane wastewater treatment process comprises the following steps

the obtained condensate is reused in the production of the same filter membrane, the prepared membrane is tested under 0.1MPa, the pure water flux is 3460L/(m 2 h), the retention rate for yeast extract powder is 95.7%, the pure water flux of the membrane prepared by using pure water is 3448L/(m 2 h), the retention rate for yeast extract powder is 95.8%, and by comparison, the performance of the membrane produced by using the condensate is consistent with that of the membrane produced by using pure water. The concentrated solution obtained by production has economic value due to higher concentration, and can be directly sold to enterprises with recovery qualification to obtain economic effect.

The present embodiment is only for explaining the present application, and it is not limited to the present application, and those skilled in the art can make modifications of the present embodiment without inventive contribution as needed after reading the present specification, but all of them are protected by patent law within the scope of the claims of the present application.

Claims

1. A process for treating wastewater generated by membrane preparation with an ultra-micro filter membrane is characterized by comprising the following steps:

filtering;

condensate treatment, namely sequentially carrying out micro-electrolysis treatment and biochemical treatment on the condensate; or the condensate is directly reused in the film preparation production;

the micro-electrolysis process includes: adjusting the pH value of the condensate to 2-3, adding the condensate into an iron-carbon micro-electrolysis filler, aerating for 10-60 min, and controlling the gas-water ratio to be 2-5: 1, obtaining an electrolytic treatment solution;

the iron-carbon micro-electrolysis filler comprises, by weight, 60-75 parts of iron powder, 8-15 parts of carbon powder, 3-10 parts of copper powder and 10-20 parts of an additive;

the additive comprises silicon carbide, aluminum oxide, bismuth oxide and titanium dioxide, and the corresponding weight ratio is 1-3: 3:3: 3.

2. The process for treating wastewater generated by membrane production with an ultrafiltration membrane according to claim 1, further comprising Fenton oxidation between the step of microelectrolysis and the step of biochemical treatment,

3. The process for treating wastewater from membrane production with an ultrafiltration membrane according to claim 2, wherein the concentration of the aqueous hydrogen peroxide solution is 30v% and the amount of hydrogen peroxide is 0.5 to 1wt% based on the electrolytic treatment solution.

4. The process for treating wastewater generated by membrane production with an ultra-microfiltration membrane according to claim 1 or 2, wherein the biochemical treatment comprises feeding the supernatant of the condensate subjected to the micro-electrolysis treatment or the supernatant of the condensate subjected to the Fenton oxidation treatment into a biochemical sludge tank, degrading the supernatant, filtering the degraded supernatant with an MBR membrane, and pumping out the degraded supernatant to obtain reuse water.

5. The process for treating wastewater generated during membrane production with an ultrafiltration membrane according to claim 1, wherein the concentrated solution is subjected to rectification.

6. The process for treating wastewater from membrane production with ultra-microfiltration membrane according to claim 5, wherein the bottoms of the column are incinerated after completion of the rectification.

7. The process for treating wastewater from membrane production with ultra-microfiltration membrane according to claim 1, wherein the precision of the filter used for filtration is 0.1 to 30 μm.