CN108328836B - Water inlet control system based on high-salt-content wastewater reduction process - Google Patents

Abstract

The utility model provides a control system of intaking based on high salt waste water minimizing process, adjusts monitoring devices real-time supervision through intaking and adjusts parameter index through the parameter index of the high salt waste water that reduces and adjust the parameter index according to the index of intaking of back end process, and high salt waste water minimizing process includes at least: adjusting the wastewater to be in an alkaline environment based on a pretreatment process by adopting a dosing mode, wherein the dosing amount is adjusted according to the change condition of each ion concentration of the actual inlet water of the high-salinity wastewater; and sequentially carrying out reduction treatment on the pretreated high-salt-content wastewater by a medium-pressure membrane element with the flow channel width of 1.524-1.778 mm and a high-pressure membrane element with the flow channel width of 1.905-2.159 mm; the inlet water adjusting and monitoring device monitors the high-salt-content wastewater subjected to reduction treatment through a temperature detector, a chloride ion detector, a heavy metal ion detector and a micro particle detector to obtain parameter indexes. The water inlet control system can effectively prevent the membrane element from being polluted.

Description

Water inlet control system based on high-salt-content wastewater reduction process

The invention is filed for application No. 201510980936.X, filed for 12/23/2015, filed for the invention in the type of application, and filed for a divisional application of the method for reducing the high-salt wastewater.

Technical Field

The invention relates to the field of industrial wastewater treatment equipment, in particular to a water inlet control system based on a high-salt-content wastewater reduction process.

Background

In recent years, with the rapid development of industries such as petrochemical industry, electric power industry, metallurgy industry, coal chemical industry and the like, the amount of sewage with complex salt content, such as reverse osmosis concentrated water, industrial sewage, circulating sewage, part of process drainage and the like generated in the industrial production process, is increasing year by year, and how to treat and utilize the sewage with complex salt content finally receives wide attention. Along with the stricter of the country on the sewage discharge control of enterprises, especially in water resource deficient areas, how to reasonably treat and utilize the part of sewage with complex salt content to realize zero discharge of wastewater is of great significance for protecting the surrounding environment and natural water body which we rely on to live, further improving the comprehensive utilization efficiency of water resources and relieving the water resource shortage condition. At present, in the sewage treatment and reuse technology, a reverse osmosis membrane method has gradually become a very important treatment means in the fields of industrial circulating water treatment, wastewater reuse, reduction and the like.

The reverse osmosis technology for treating wastewater is developed relatively quickly at present, but the technology has increasingly prominent problems in treating wastewater with complex components, and the main problems are shown in two aspects:

firstly, the reverse osmosis membrane element has high desalination rate to containing salt waste water, and the desalination rate that reverse osmosis membrane element can reach is more than 98% under normal circumstances for salt and impurity more than 98% in the phase transition water do not take place and hold back in the dense water that the system produced. The reverse osmosis water production system generally has a water recovery rate of only about 75%, and the water production system still has about 25% of concentrated water which cannot be recovered and discharged. Because the concentrated water of the complex wastewater containing salt contains a large amount of calcium ions, magnesium ions, heavy metal ions, silicon ions and colloid substances, and some chemical wastewater contains a large amount of non-degradable organic matters and inorganic salts and complex components closely related to the production process, the direct discharge can cause water pollution to the discharged river. Although the reverse osmosis treatment realizes reduction treatment to a certain degree, concentrated salt substances still remain in discharged concentrated water, the conventional wastewater treatment method generally adopts simple treatment and then discharges the concentrated salt substances out or directly discharges the concentrated salt substances, the influence on the surrounding environment is gradually serious, and finally the treatment of the concentrated reverse osmosis water is a difficult problem.

And secondly, the salt-containing complex wastewater subjected to low-pressure, medium-pressure and high-pressure reverse osmosis concentration has the problems of organic matter pollution of a membrane element and easy scaling of inorganic salt calcium magnesium compounds tending to be saturated on the surface of the membrane when the wastewater is treated by a reverse osmosis treatment mode. Therefore, the problems of increased difficulty in salt separation, increased energy consumption for separation, poor economy, low reliability and the like are caused.

For example, chinese patent CN 102923876a discloses a system for recovering heavy metals and recycling wastewater in heavy metal wastewater by a tubular microfiltration membrane method. This system carries out pH regulation, tubular micro-filtration preliminary treatment through carrying out waste water, carries out waste water recovery through reverse osmosis unit again. The filtering of waste water particle pollutants is realized, and the phenomenon of sludge particles leakage cannot occur; the micro-filtration membrane can bear the cleaning of acidic, alkaline, bleaching and oxidizing agents, and the cleaned micro-filtration membrane tube has a longer service life. The invention has simple flow, more convenient operation and easy realization of automatic control; the floor area is small, the investment of the infrastructure period can be saved, and the investment of the medicament can be saved. However, the system only carries out pretreatment and reverse osmosis treatment on the wastewater, the water resource recovery and utilization rate of the wastewater is low, the problem of large water resource waste exists, meanwhile, the ratio of the tail liquid to be treated to the wastewater is large, the energy consumption for treating the tail liquid is increased, the wastewater treatment cost is increased, and the environmental protection problem is solved.

Patent publication No. CN103508602A (reference 1) discloses a membrane and evaporative crystallization integrated high salinity industrial wastewater zero discharge process. The method specifically points out that the traditional processes such as a chemical precipitation method, a redox method, a membrane separation method, an ion exchange method and the like cannot meet the requirement of zero emission after wastewater treatment, and based on the technical background, the technical means that the solid impurities in the wastewater are concentrated to a very high concentration by comprehensively applying physical, chemical and biochemical processes such as membrane separation, evaporative crystallization and/or drying, most of the water is returned for recycling, and the remaining small amount of water accompanied with solid waste is treated and recycled through the ways such as evaporation/crystallization, evaporation/drying, solid fertilizer absorption and the like, so that the water is not discharged out of the system is provided. The method does not relate to the technical means of monitoring and adjusting the parameter indexes of the wastewater in real time so as to solve the problems of membrane pollution, low water yield and the like in the actual wastewater treatment process. Furthermore, the technical means of the reverse osmosis membrane element with the dosage dynamically adjusted according to the actual concentration of the inlet water ions and the super-large flow channel width are not involved.

The patent with publication number CN102030397A (reference 2) discloses an on-line detection method and device for building reclaimed water, and specifically points out that the building reclaimed water detection device is arranged at a reclaimed water supply pipe leading to a reclaimed water user to detect residual chlorine content and turbidity of reclaimed water entering the water supply pipe. Meanwhile, under the condition of combining the comparison document 1 and the comparison document 2, a person skilled in the art can only obtain the water quality of the recycled purified water obtained after the water inlet detection device is arranged at the water inlet pipeline of the recycled water of a user to detect the water quality of the recycled purified water obtained after treatment, and cannot obtain the technical means of applying the detection device to monitoring the parameter index of the wastewater and dynamically adjusting the parameter index of the wastewater to improve membrane pollution and improve the water yield.

Patent publication No. CN103319042A (reference 3) discloses an integrated device and process for recycling high-salt complex wastewater and zero emission. It specifically discloses a wastewater pretreatment process for homogenizing and homogenizing high-salt complex wastewater and then adjusting the wastewater to be alkaline by adding sodium hydroxide, sodium carbonate and the like. The method does not relate to the technical means of dynamically adjusting the dosing quantity according to the actual inlet water ion concentration of inlet water and monitoring and dynamically adjusting the parameter indexes of the wastewater in real time.

Disclosure of Invention

Aiming at the defects of the prior art, the invention provides a reduction treatment method of high-salt-content wastewater, which comprises the steps of pretreating the high-salt-content wastewater, then carrying out preliminary reduction treatment and deep concentration treatment, wherein a water inlet control system of the deep concentration treatment is characterized in that residual chlorine, heavy metal ions and colloid in a high-pressure reverse osmosis concentrated solution generated by the preliminary reduction treatment are adsorbed by an activated carbon filter and a resin tank, then tiny suspended matters and colloid are filtered by a third security filter, the filtered wastewater is sent to a water inlet adjusting and monitoring device, and based on a water inlet index of a first-level electric driven ionic membrane unit in the deep concentration treatment process and the filtered wastewater information monitored by a water inlet adjusting and monitoring device, at least one treatment device of a water temperature regulator, the activated carbon filter, the resin tank and the third security filter is used for carrying out at least one-time cyclic treatment on the filtered wastewater under the control of the water inlet adjusting and monitoring device And until the filtered wastewater reaches the water inlet index of the first-level electrically-driven ionic membrane unit.

According to a preferred embodiment, the intake water regulation monitoring device comprises: the system comprises a temperature detector for monitoring the temperature of the wastewater, a chloride ion detector for monitoring the concentration of chloride ions in the wastewater, a heavy metal ion detector for monitoring the concentration of heavy metal ions, and a micro particle detector for monitoring the content of colloids and micro suspended matters; the system comprises a water temperature regulator for regulating the temperature of the wastewater, a first drain valve for controlling the wastewater to flow into a first-stage electrically-driven ionic membrane unit, a second drain valve for controlling the wastewater to flow into an activated carbon filter, a third drain valve for controlling the wastewater to flow into a resin tank, and a fourth drain valve for controlling the wastewater to flow into a third security filter; a distributed A/D acquisition module for receiving monitoring data), a singlechip for data processing, a PC terminal for controlling the singlechip and a distributed digital input and output module for feeding back control information.

According to a preferred embodiment, the water inlet adjusting and monitoring device transmits information detected by the temperature detector, the chloride ion detector, the heavy metal ion detector and the micro particle detector to the single chip microcomputer through a distributed A/D acquisition module, the single chip microcomputer carries out data processing on the monitoring information based on the water inlet requirement of the first-stage electrically driven ionic membrane unit input by the PC terminal, and the processing result is fed back to the water temperature regulator, the first drain valve, the second drain valve, the third drain valve and the fourth drain valve through a distributed digital input and output module.

According to a preferred embodiment, the water inlet index of the primary electrically-driven ionic membrane unit is as follows: the water inlet temperature is 5-40 ℃; the content of residual chlorine is not more than 0.05 mg/L; the content of heavy metal ions is not more than 0.1 mg/L; the sewage quality index SDI is not more than 3.0.

According to a preferred embodiment, the preliminary reduction process comprises the following steps: the pretreated wastewater is filtered by a first cartridge filter and then is sent into the medium-pressure reverse osmosis device; treating the wastewater by the medium-pressure reverse osmosis device to obtain medium-pressure reverse osmosis produced water and medium-pressure reverse osmosis concentrated solution, wherein the medium-pressure reverse osmosis produced water is sent to a secondary reverse osmosis device, and the medium-pressure reverse osmosis concentrated solution is filtered by a second cartridge filter and then sent to the high-pressure reverse osmosis device; and the filtered medium-pressure reverse osmosis concentrated solution is treated by the high-pressure reverse osmosis device to obtain high-pressure reverse osmosis produced water and high-pressure reverse osmosis concentrated solution, wherein the high-pressure reverse osmosis produced water is sent to a secondary reverse osmosis device, and the high-pressure reverse osmosis concentrated solution is subjected to deep concentration treatment.

According to a preferred embodiment, the deep concentration process comprises the following steps: the high-pressure reverse osmosis concentrated solution is treated by a water inlet control system and then is sent to a first-stage electric driven ion membrane unit for deep concentration treatment; the water is treated by the first-stage electrically-driven ionic membrane unit to obtain first-stage electrically-driven strong brine and first-stage electrically-driven water production, wherein the first-stage electrically-driven water production enters a second-stage reverse osmosis device, and the first-stage electrically-driven strong brine is pumped into the second-stage electrically-driven ionic membrane unit by a third booster water pump; and treating by the second-stage electrically-driven ionic membrane unit to obtain second-stage electrically-driven strong brine and second-stage electrically-driven water production, wherein the second-stage electrically-driven water production is sent to the medium-pressure water pool, and the second-stage electrically-driven strong brine is sent to a second strong brine tank.

According to a preferred embodiment, the produced water fed into the secondary reverse osmosis device is treated to obtain secondary reverse osmosis produced water and secondary reverse osmosis concentrated brine, wherein the secondary reverse osmosis produced water is fed into the fresh water tank, and the secondary reverse osmosis concentrated brine is fed into the first intermediate water tank.

According to a preferred embodiment, the medium-pressure reverse osmosis device adopts a medium-pressure membrane element with the flow channel width of 1.524-1.778 mm, and the high-pressure reverse osmosis device adopts a high-pressure membrane element with the flow channel width of 1.905-2.159 mm.

According to a preferred embodiment, the activated carbon filter is used for adsorbing chlorine which is not removed in the primary reduction process, and simultaneously adsorbing small molecular organic matters, colloids and heavy metal ions; the resin tank is provided with ion exchange resin and is used for adsorbing heavy metal ions in the solution treated by the activated carbon filter; the third cartridge filter is used for filtering micro suspended matters and colloids in the solution.

According to a preferred embodiment, the wastewater pretreatment, preliminary reduction treatment and advanced concentration treatment comprise the following steps: homogenizing and homogenizing the high-salinity wastewater, adding more than one coagulant or softener of lime or sodium hydroxide, sodium carbonate, polyaluminium chloride and polyacrylamide for precipitation, adjusting the wastewater to be in an alkaline environment, discharging the precipitate into a sludge pool, and feeding the precipitated wastewater into a tubular micro-filter for filtering;

carrying out mud-water separation on the sediment in the sludge pool through a sludge dewatering device to obtain mud cakes and salt-containing wastewater, carrying out dry sludge treatment on the mud cakes, and sending the salt-containing wastewater into a regulating reservoir to be mixed with a wastewater stock solution;

sending the supernatant filtered by the tubular micro-filter into a filter element filter, and discharging the chemical precipitate filtered by the tubular micro-filter into a high-density tank; the produced water filtered by the filter element filter is sent to a first intermediate water tank for reduction treatment;

the pretreated wastewater in the first intermediate water tank is sent to the medium-pressure reverse osmosis device after wastewater suspended matters and colloids are filtered by a first cartridge filter;

treating the wastewater by the medium-pressure reverse osmosis device to obtain medium-pressure reverse osmosis produced water and medium-pressure reverse osmosis concentrated solution, wherein the medium-pressure reverse osmosis produced water is sent to a secondary reverse osmosis device, and the medium-pressure reverse osmosis concentrated solution is filtered by a second cartridge filter and then sent to the high-pressure reverse osmosis device;

the filtered medium-pressure reverse osmosis concentrated solution is treated by the high-pressure reverse osmosis device to obtain high-pressure reverse osmosis produced water and a high-pressure reverse osmosis concentrated solution, wherein the high-pressure reverse osmosis produced water is sent to a secondary reverse osmosis device, and the high-pressure reverse osmosis concentrated solution is sent to a deep concentration water inlet control system;

the deep concentration water inlet control system is characterized in that residual chlorine, heavy metal ions and colloid in the high-pressure reverse osmosis concentrated solution generated by preliminary reduction treatment are adsorbed by an activated carbon filter and a resin tank, tiny suspended matters and colloid are filtered by a third security filter, and the filtered wastewater is sent to a water inlet adjustment monitoring device;

based on the information of the filtered wastewater monitored by a first-stage electrically-driven ionic membrane unit water inlet index and a water inlet adjusting and monitoring device in the deep concentration treatment process, realizing at least one-time treatment of the filtered wastewater by at least one treatment device selected from a water temperature regulator, an activated carbon filter, a resin tank and a third security filter until the filtered wastewater reaches the first-stage electrically-driven ionic membrane unit water inlet index;

the high-pressure reverse osmosis concentrated solution is treated by a deep concentration water inlet control system and then is sent to a first-stage electric driven ion membrane unit for deep concentration treatment; the water is treated by the first-stage electrically-driven ionic membrane unit to obtain first-stage electrically-driven strong brine and first-stage electrically-driven water production, wherein the first-stage electrically-driven water production enters a second-stage reverse osmosis device, and the first-stage electrically-driven strong brine is pumped into the second-stage electrically-driven ionic membrane unit by a third booster water pump;

after being treated by the secondary electric drive ionic membrane unit, secondary electric drive strong brine and secondary electric drive produced water are obtained, the secondary electric drive produced water is sent to a medium-pressure water pool, and the secondary electric drive strong brine is sent to a second strong brine tank;

the produced water sent into the secondary reverse osmosis device is treated to obtain secondary reverse osmosis produced water and secondary reverse osmosis strong brine, wherein the secondary reverse osmosis produced water is sent into a fresh water tank, and the secondary reverse osmosis strong brine is sent to a first intermediate water tank;

the high-salt wastewater (after the pretreatment, the preliminary reduction treatment and the deep concentration treatment, more than 95% of the wastewater solution can be recovered to a fresh water tank, and the produced water collected by the fresh water tank is sent to a reuse water tank to realize the reuse of the wastewater.

The invention has the following advantages:

(1) in the preliminary wastewater reduction process, the wastewater is in an alkaline condition, and the problems of silicon scaling and organic pollution on the surface of the membrane can be inhibited under the alkaline condition.

(2) The high-pressure membrane element has the characteristic of an oversized flow passage, and the reverse osmosis system is less prone to ion scaling and organic matter pollution due to the special flow passage and structural design.

(3) The water inlet adjusting device can effectively adjust the temperature of the wastewater, realize that the primary electrically-driven ionic membrane unit works at the optimal temperature and improve the water yield.

(4) The water inlet adjusting device can effectively avoid the problems of calcium and magnesium ion pollution of the electrically driven ionic membrane and scaling of heavy metal ions on the surface of the membrane.

(5) The wastewater reduction treatment method can recover over 95 percent of high-quality desalted water to be reused in a production device, and creates favorable conditions for subsequent large-scale reduction treatment of water quantity.

Drawings

FIG. 1 is a flow chart of the treatment of high salinity wastewater in accordance with the present invention;

FIG. 2 is a flow chart of a preferred mode of treating the high salinity wastewater according to the present invention; and

FIG. 3 is a schematic diagram of a module of the water inlet adjusting device of the present invention.

List of reference numerals

101: high-salt-content wastewater 102: the adjusting tank 103: lift pump

104: the high-density pond 105: first booster pump 106: tubular micro-filter

107: cartridge filter 108: first intermediate pool 109: second booster pump

110: first security filter 111: medium-pressure reverse osmosis device 112: medium-pressure water pool

113: third booster pump 114: second canister filter 115: high-pressure reverse osmosis device

116: second intermediate water pool 117: first booster water pump 118: activated carbon filter

119: the resin tank 120: the intermediate water tank 121: second booster water pump

122: third cartridge filter 123: primary electrically-driven ionic membrane unit 124: first strong brine tank

125: third booster water pump 126: secondary electrically driven ionic membrane unit 127: second strong brine tank

128: secondary reverse osmosis device 129: fresh water tank 130: recycling water tank

131: salt evaporative crystallization apparatus 132: crystalline salt 133: sludge tank

134: sludge dewatering device 135: the mud cake 136: medicine adding device

200: water inflow adjustment monitoring device 201: temperature probe 202: chloride ion detector

203: heavy metal ion detector 204: the fine particle detector 205: water temperature regulator

206: first drain valve 207: the second drain valve 208: third drain valve

209: the fourth drain valve 210: distributed a/D acquisition module 211: distributed digital input/output module

212: the single chip microcomputer 213: PC terminal

Detailed Description

The following detailed description is made with reference to the accompanying drawings and examples.

FIG. 1 shows a wastewater treatment scheme of the present invention. As shown in figure 1, the high-salinity wastewater treatment of the invention comprises a wastewater pretreatment stage, a wastewater preliminary reduction treatment stage, a wastewater deep concentration stage and a wastewater evaporative crystallization stage.

Referring to fig. 1, the wastewater pretreatment stage device of the present invention comprises a regulating tank 102, a lift pump 103, a dense tank 104, a first booster pump 105, a tubular micro filter 106, a filter element filter 107, a first intermediate water tank 108, a sludge tank 133, a sludge dewatering device 134, and a dosing device 136. The regulating reservoir 102 is connected with a lift pump 103 and is used for carrying out homogeneous and uniform treatment on the high-salinity wastewater 101. The lift pump 103 sends the wastewater with high salt content after the homogenization and uniform treatment to the high-density tank 104. The dosing device 136 is connected to the high density tank 104 and is used to add coagulant and softener to the wastewater in the high density tank 104 while adjusting the wastewater to an alkaline environment, which has a tendency to inhibit silicon scaling and organic contamination on the membrane surface. The high-density tank 104 is also connected to a first booster pump 105 and a sludge tank 133. The high density tank 104 is used for realizing coagulation and softening processes of the wastewater and completing turbidity reduction and precipitation processes of the wastewater. The precipitated chemical sludge is discharged into a sludge tank 133, and the rest of the wastewater liquid is sent to a tubular micro-filter 106 through a first booster pump 105. The sludge tank 133 is connected to a sludge dewatering device 134. The sludge tank 133 performs sludge conditioning treatment on the chemical sludge discharged therein, and then sends the chemical sludge to the sludge dewatering device 134 for treatment. The sludge dewatering device 134 is connected to the conditioning tank 102. The sludge dewatering device 134 performs sludge-water separation processing on the sludge fed thereto. Wastewater separated by the sludge dewatering device 134 is sent to the regulating reservoir 102 to be mixed with the original wastewater for further treatment. The sludge cake 135 produced by the sludge dewatering device 134 is finally subjected to a dry sludge treatment. The tubular micro-filter 106 is connected to a cartridge filter 107 and the high density reservoir 104. The tubular micro-filter 106 is used for filtering the coagulation colloid substance in the wastewater and sending the filtered wastewater to the high-density tank 104, and the filtered wastewater is sent to the filter element filter 107. The cartridge filter 107 is connected to the first intermediate sump 108, and the cartridge filter 107 filters the wastewater supplied thereto and supplies the filtered wastewater to the first intermediate sump 108.

Referring again to fig. 1, the wastewater preliminary reduction treatment stage apparatus of the present invention includes a second booster pump 109, a first safety filter 110, a medium pressure partial osmosis device 111, a medium pressure water tank 112, a third booster pump 113, a second safety filter 114, a high pressure partial osmosis device 115, a second intermediate water tank 116, a secondary reverse osmosis device 128, a fresh water tank 129, and a reuse water tank 130. The second booster pump 109 is connected to a first safety filter 110. The second booster pump 109 is used to transfer the wastewater of the first intermediate water sump 108 to the first safety filter 110. The first safety filter 110 is connected to a medium pressure reverse osmosis unit 111. The first safety filter 110 is used for filtering micro suspended matters in the wastewater, and the filtered wastewater is sent to the medium-pressure reverse osmosis device 111. The medium pressure reverse osmosis unit 111 is connected to the medium pressure water tank 112 and the secondary reverse osmosis unit 128. The medium-pressure reverse osmosis device 111 adopts a medium-pressure membrane element with the width of a flow channel of 1.524-1.778 mm. The medium-pressure reverse osmosis device 111 is used for pressurizing the wastewater and performing reverse osmosis treatment. The treated medium pressure reverse osmosis produced water enters a secondary reverse osmosis device 128, and the treated medium pressure reverse osmosis concentrated solution is sent to the medium pressure water tank 112. The medium pressure water tank 112 is connected to a third booster pump 113. The third booster pump 113 is connected to a second canister filter 114. The third booster pump 113 is used to send the medium-pressure reverse osmosis concentrated solution in the medium-pressure water tank 112 to the second cartridge filter 114. The second canister filter 114 is connected to a high pressure reverse osmosis unit 115. The second cartridge filter 114 is used to filter the fine suspended matters in the wastewater and send the filtered wastewater to the high pressure reverse osmosis device 115. The high pressure reverse osmosis unit 115 is connected to the second intermediate water tank 116 and the secondary reverse osmosis unit 128. The high-pressure reverse osmosis device 115 adopts a high-pressure membrane element with the width of a flow channel of 1.905-2.159 mm. The high pressure reverse osmosis device 115 pressurizes the wastewater fed thereto and completes the high pressure reverse osmosis treatment of the wastewater, the treated high pressure reverse osmosis produced water is fed to the secondary reverse osmosis device 128, and the treated high pressure reverse osmosis concentrated solution is fed to the second intermediate water tank 116. The secondary reverse osmosis device 128 is connected to a fresh water tank 129. The secondary reverse osmosis device 128 is used for carrying out secondary reverse osmosis treatment on the produced water entering the secondary reverse osmosis device, the treated secondary reverse osmosis produced water is sent to the reuse water tank 130 through the fresh water tank 129 to realize water resource reuse, and the treated secondary reverse osmosis concentrated brine is sent to the first intermediate water tank 108 to be mixed with the original wastewater.

Referring again to fig. 1, the advanced wastewater concentration treatment stage apparatus of the present invention includes a first booster water pump 117, an activated carbon filter 118, a resin tank 119, an intermediate water tank 120, a second booster water pump 121, a third cartridge filter 122, a primary electrically driven ion membrane unit 123, a first concentrated brine tank 124, a third booster water pump 125, a secondary electrically driven ion membrane unit 126, a second concentrated brine tank 127, a secondary reverse osmosis apparatus 128, a fresh water tank 129, and a reuse water tank 130. First booster pump 117 is connected to carbon filter 118. A first booster pump 117 is used to deliver the high pressure reverse osmosis concentrate solution from the second intermediate water sump 116 to an activated carbon filter 118. The activated carbon filter 118 is connected to a resin tank 119. The activated carbon filter 118 is used for adsorbing residual chlorine in the preliminary reduction process, preventing the ion exchange resin from being polluted by free residual oxygen poisoning, adsorbing micromolecular organic matters, colloids and heavy metal ions, and sending the adsorbed concentrated solution to the resin tank 119. The resin tank 119 is connected to the intermediate water tank 120. The resin tank 119 is used to adsorb heavy metal ions in the solution treated by the activated carbon filter 118, and send the treated solution to the intermediate water tank 120. The intermediate water tank 120 is connected to a second booster water pump 121. Second booster pump 121 is connected to third cartridge filter 122. A second booster pump 121 is used to deliver the solution from the intermediate tank 120 to a third cartridge filter 122. The third cartridge filter 122 is connected to a primary electrically driven ion membrane unit 123. The third cartridge filter 122 is used to filter out the fine suspended matters in the solution, and send the filtered wastewater to the first-stage electrically driven ionic membrane unit 123. The primary electrically driven ionic membrane unit 123 is connected to a first concentrated brine tank 124 and a secondary reverse osmosis device 128. The first-stage electrically-driven ionic membrane unit 123 is used for performing cyclic desalination and concentration treatment on the wastewater, feeding the treated first-stage electrically-driven produced water into the second-stage reverse osmosis device 128, and feeding the treated first-stage electrically-driven concentrated brine into the first concentrated brine tank 124. The secondary reverse osmosis device 128 is connected to a fresh water tank 129. The secondary reverse osmosis device 128 is used for carrying out secondary reverse osmosis treatment on the produced water entering the secondary reverse osmosis device, the treated secondary reverse osmosis produced water is sent to the reuse water tank 130 through the fresh water tank 129 to realize water resource reuse, and the treated secondary reverse osmosis concentrated brine is sent to the first intermediate water tank 108 to be mixed with the original wastewater. The first rich brine tank 124 is connected to a third booster water pump 125. The third booster water pump 125 is connected to the secondary electrically driven ion membrane unit 126. A third booster pump 125 is used to deliver the primary electrically driven brine in the first brine tank 124 to a secondary electrically driven ionic membrane unit 126. The secondary electrically driven ionomeric membrane unit 126 is connected to the second concentrated brine tank 127 and the medium pressure water tank 112. The secondary electrically driven ionic membrane unit 126 is used for carrying out cyclic desalination and concentration wastewater treatment on the wastewater, the obtained secondary electrically driven produced water after treatment is sent into the medium-pressure water tank 112 to be mixed with medium-pressure reverse osmosis concentrated solution in the tank, and secondary electrically driven concentrated solution obtained after treatment enters the second concentrated brine tank 127. The second concentrated brine tank 127 is connected to the salt evaporative crystallization device 131. The second brine tank 127 is used to feed the second electrically driven brine to the evaporative crystallization device 131.

Referring to fig. 2, in a preferred embodiment of the advanced wastewater concentration treatment stage of the present invention, the apparatus includes a first booster pump 117, an activated carbon filter 118, a resin tank 119, an intermediate water tank 120, a second booster pump 111, a third cartridge filter 122, a water inlet adjustment monitoring apparatus 200, a first electrically-driven ionic membrane unit 123, a first concentrated brine tank 124, a third booster pump 125, a second electrically-driven ionic membrane unit 126, a second concentrated brine tank 127, a second reverse osmosis apparatus 128, a fresh water tank 129, and a reuse water tank 130. As shown in fig. 3, the inlet water regulation monitoring device 200 includes: the system comprises a temperature detector 201, a chloride ion detector 202, a heavy metal ion detector 203, a micro particle detector 204, a water temperature regulator 205, a first drain valve 206, a second drain valve 207, a third drain valve 208, a fourth drain valve 209, a distributed A/D acquisition module 210, a distributed digital input and output module 211, a single chip microcomputer 212 and a PC terminal 213.

First booster pump 117 is connected to carbon filter 118. A first booster pump 117 is used to deliver the high pressure reverse osmosis concentrate solution from the second intermediate water sump 116 to an activated carbon filter 118. The activated carbon filter 118 is connected to a resin tank 119. The activated carbon filter 118 is used for adsorbing residual chlorine in the preliminary reduction process, preventing the ion exchange resin from being polluted by free residual oxygen poisoning, adsorbing micromolecular organic matters, colloids and heavy metal ions, and sending the adsorbed concentrated solution to the resin tank 119. The resin tank 119 is connected to the intermediate water tank 120. The resin tank 119 is used to adsorb heavy metal ions in the solution treated by the activated carbon filter 118, and send the treated solution to the intermediate water tank 120. The intermediate water tank 120 is connected to a second booster water pump 121. Second booster pump 121 is connected to third cartridge filter 122. A second booster pump 121 is used to deliver the solution from the intermediate tank 120 to a third cartridge filter 122. Third canister filter 122 is connected to influent adjustment monitoring apparatus 200. The third cartridge filter 122 is used to filter out the fine suspended matters in the solution, and send the filtered wastewater to the influent adjustment monitoring device 200. The feed water adjustment monitoring device 200 is connected to the first-stage electrically driven ion membrane unit 123 through a first drain valve 206. The feed water adjustment monitoring device 200 is connected to the carbon filter 118 through a second drain valve 207. The feed water adjustment monitoring device 200 is connected to the resin tank 119 through a third drain valve 208. The inlet water adjustment monitoring device 200 is connected to the third canister filter 122 through a fourth drain valve 209. The water inlet adjusting and monitoring device 200 transmits the temperature information of the wastewater solution collected by the temperature detector 201 to the single chip microcomputer through the distributed A/D collection module 210. The inlet water adjustment monitoring device 200 transmits the information of the chloride ion concentration of the wastewater solution collected by the chloride ion detector 202 to the single chip microcomputer 212 through the distributed A/D collection module 210. The water inlet adjusting and monitoring device 200 transmits the concentration information of the heavy metal ions in the wastewater solution collected by the heavy metal ion detector 203 to the single chip microcomputer 212 through the distributed A/D collection module 210. The water inlet adjusting and monitoring device 200 transmits the concentration information of the heavy metal ions in the wastewater solution collected by the micro particle detector 204 to the single chip microcomputer 212 through the distributed A/D collection module 210. The water inlet index of the primary electrically driven ionic membrane unit 123 is input to the single chip microcomputer 212 from the PC terminal 213. The single chip microcomputer 212 processes the monitored information of the temperature of the wastewater solution, the content of chloride ions, the content of heavy metal ions and the content of micro particles based on the water inlet requirement of the primary electrically-driven ionic membrane unit 123 input by the PC terminal 213. The single chip microcomputer 212 feeds back the data processing result to the water temperature regulator 205 through the distributed digital input and output module 211, and controls the temperature of the wastewater solution through the water temperature regulator 205. The singlechip 212 feeds back the data processing result to the second drain valve 207 through the distributed digital input and output module 211, and controls whether to discharge the wastewater solution to the activated carbon filter 118 for dechlorination again by controlling the second drain valve 207. The singlechip 212 feeds back the data processing result to the third drain valve 208 through the distributed digital input and output module 211, and controls whether the wastewater solution is drained into the resin tank 119 for secondary metal ion removal treatment by controlling the third drain valve 208. The single chip microcomputer 212 feeds back the data processing result to the fourth drain valve 209 through the distributed digital input and output module 211, and controls whether the wastewater solution flows into the third security filter 122 for secondary impurity removal by controlling the fourth drain valve 209. Until the wastewater monitored by the water inlet adjustment monitoring device 200 reaches the water inlet index of the first-stage electrically-driven ionic membrane unit 123, the single-chip microcomputer 212 feeds back the data processing result to the first drain valve 206 through the distributed digital input and output module 211, and controls the wastewater solution to flow into the first-stage electrically-driven ionic membrane unit 123 through the first drain valve 206. The primary electrically driven ionic membrane unit 123 is connected to a first concentrated brine tank 124 and a secondary reverse osmosis device 128. The first-stage electrically-driven ionic membrane unit 123 is used for performing cyclic desalination and concentration treatment on the wastewater, feeding the treated first-stage electrically-driven produced water into the second-stage reverse osmosis device 128, and feeding the treated first-stage electrically-driven concentrated brine into the first concentrated brine tank 124. The secondary reverse osmosis device 128 is connected to a fresh water tank 129. The secondary reverse osmosis device 128 is used for carrying out secondary reverse osmosis treatment on the produced water entering the secondary reverse osmosis device, the treated secondary reverse osmosis produced water is sent to the reuse water tank 130 through the fresh water tank 129 to realize water resource reuse, and the treated secondary reverse osmosis concentrated brine is sent to the first intermediate water tank 108 to be mixed with the original wastewater. The first rich brine tank 124 is connected to a third booster water pump 125. The third booster water pump 125 is connected to the secondary electrically driven ion membrane unit 126. A third booster pump 125 is used to deliver the primary electrically driven brine in the first brine tank 124 to a secondary electrically driven ionic membrane unit 126. The secondary electrically driven ionomeric membrane unit 126 is connected to the second concentrated brine tank 127 and the medium pressure water tank 112. The secondary electrically driven ionic membrane unit 126 is used for carrying out cyclic desalination and concentration wastewater treatment on the wastewater, the obtained secondary electrically driven produced water after treatment is sent into the medium-pressure water tank 112 to be mixed with medium-pressure reverse osmosis concentrated solution in the tank, and secondary electrically driven concentrated solution obtained after treatment enters the second concentrated brine tank 127. The second concentrated brine tank 127 is connected to the salt evaporative crystallization device 131. The second brine tank 127 is used to feed the second electrically driven brine to the evaporative crystallization device 131.

Referring to fig. 2, the wastewater treatment of the present invention further comprises a wastewater evaporative crystallization stage, wherein the wastewater evaporative crystallization apparatus comprises a salt evaporative crystallization apparatus 131, a fresh water tank 129 and a reuse water tank 130. The salt evaporation and crystallization device 131 is connected with the fresh water tank 129. The device is used for carrying out evaporation crystallization treatment on the secondary electrically driven concentrated salt solution fed into the device, the produced water generated by treatment is fed into a reuse water tank 130 through a fresh water tank 129 for realizing water resource reuse, and the crystallized salt 132 generated by treatment is comprehensively treated by salts.

Example 1

The wastewater pretreatment process of the present invention is explained with reference to fig. 1. The high-salinity wastewater 101 is homogenized, equalized and regulated through a regulating reservoir 102. The high-salt-content wastewater 101 is discharged from a circulating water system in industrial sewage treatment and discharged from a production process. The wastewater after the conditioning treatment is sent to a high density pond 104 through a lift pump 103. Lime or sodium hydroxide, sodium carbonate, polyaluminium chloride and polyacrylamide are sequentially added into the high-density tank 104 through a dosing device 136, and the wastewater is adjusted to be in an alkaline environment. The added sodium hydroxide and sodium carbonate are used for softening wastewater, the sodium hydroxide is prepared into a 20% solution, the adding amount is 1.5g/L, the sodium carbonate is prepared into a 15% solution, the adding amount is 3g/L, the added polyaluminum chloride and polyacrylamide are used for coagulating wastewater, the polyaluminum chloride is prepared into a 20% solution, the drug is added according to the amount of 30mg/L, the polyacrylamide is prepared into a 0.3% solution, the drug is added according to the amount of 3mg/L, the drug adding amounts of the sodium hydroxide, the sodium carbonate, the polyaluminum chloride and the polyacrylamide are not excessive, the adjustment is carried out according to the change condition of each ion concentration of actual inlet water of the wastewater, otherwise, the pollution of a reverse osmosis membrane and an electrically driven ionic membrane is easily caused, and the service life of the membrane is influenced. Coagulant and softener are added into the wastewater stock solution in the high density tank 104, then precipitation is carried out, and the precipitate is discharged into a sludge tank 133. The precipitated wastewater stock solution is sent to a tubular micro-filter 106 for filtration. The retention time of the wastewater in the tubular micro-filter 106 is 2.5 hours, under the action of natural sedimentation, the supernatant enters the filter element filter 107 through the tubular micro-filter 106, and the chemical precipitate is sent into a high-density tank for sedimentation and discharged into a sludge tank 133. The wastewater stock solution in the filter element filter 107 is filtered to send produced water into a first intermediate water tank 108, so that the wastewater pretreatment process is completed.

Example 2

The wastewater reduction treatment process of the present invention will be described with reference to FIGS. 2 and 3. In order to realize the recycling of the wastewater, the wastewater reduction process comprises the processes of primary wastewater reduction treatment and deep wastewater concentration treatment.

The second booster pump 109 delivers the wastewater pretreated in the first intermediate water sump 108 to the first safety filter 110. The first safety filter 110 is used for filtering micro suspended matters in the wastewater, and the filtered wastewater is sent to the medium-pressure reverse osmosis device 111.

According to a preferred embodiment, the medium-pressure reverse osmosis device 111 adopts a medium-pressure membrane element with a membrane material of 1.651mm and a channel width of the aromatic polyamide composite material, and performs reverse osmosis treatment on the wastewater under the condition that the operating pressure is 2.0-3.5 MPa, and the medium-pressure reverse osmosis device 111 is not easy to generate ion scaling and organic fouling due to special channel and structure design. The recovery rate of the waste water is more than 70 percent in the medium-pressure reverse osmosis treatment process, 97.5 percent of salt substances can be intercepted, and raw water with the average TDS of 6500mg/L can be concentrated to the TDS of more than 21600 mg/L. The recovered medium pressure reverse osmosis produced water is sent to a secondary reverse osmosis device 128, the medium pressure reverse osmosis concentrated solution is sent to the medium pressure water tank 112, the medium pressure reverse osmosis produced water is subjected to secondary reverse osmosis treatment, the secondary reverse osmosis produced water enters a fresh water tank 129, and the secondary reverse osmosis concentrated solution is sent to the first intermediate water tank 8 again.

The concentrated medium pressure reverse osmosis solution is filtered by a second cartridge filter 114 and sent to a high pressure reverse osmosis device 115. According to a preferred embodiment, the high-pressure reverse osmosis device 115 adopts a high-pressure membrane element with a membrane material of 2.032mm and a channel width of an aromatic polyamide composite material, and performs high-pressure reverse osmosis treatment on the filtered medium-pressure reverse osmosis concentrated solution under the condition that the operating pressure is 3.5-4.5 MPa, and the high-pressure reverse osmosis device 111 is not easy to generate ion scaling and organic fouling due to special channel and structural design. The recovery rate of the waste water is more than 65% in the high-pressure reverse osmosis treatment process, more than 97.2% of salt substances can be intercepted, and raw water with average TDS of 21600mg/L can be concentrated to TDS more than 50000 mg/L. The recovered high-pressure reverse osmosis produced water is sent to a second-stage reverse osmosis device 28 for second-stage reverse osmosis treatment, the second-stage reverse osmosis produced water enters a fresh water tank 129, the second-stage reverse osmosis concentrated solution is sent to the first intermediate water tank 108 again, and the high-pressure reverse osmosis concentrated solution is sent to the second intermediate water tank 116 for deep concentration treatment.

According to a preferred embodiment, the high pressure reverse osmosis concentrated solution is treated by a carbon filter 118 and a resin tank 119, filtered by a security filter 122 and sent to a feed water regulation monitoring device 200.

According to a preferred embodiment, the water inlet index of the primary electrically driven ionic membrane unit 123 is: the water inlet temperature is 5-40 ℃; the content of residual chlorine is not more than 0.05 mg/L; the content of heavy metal ions is not more than 0.1 mg/L; the sewage quality index SDI is not more than 3.0.

The water inlet adjusting and monitoring device 200 transmits information detected by the temperature detector 201, the chloride ion detector 202, the heavy metal ion detector 203 and the micro particle detector 204 to the single chip microcomputer 212 through the distributed A/D acquisition module 210, and the single chip microcomputer 212 performs data processing on the monitoring information based on the water inlet requirement of the primary electrically driven ionic membrane unit 123 input by the PC terminal 213.

The single chip microcomputer 212 feeds back the data processing result to the water temperature regulator 205 through the distributed digital input and output module 211, and controls the temperature of the wastewater solution through the water temperature regulator 205. The singlechip 212 feeds back the data processing result to the second drain valve 207 through the distributed digital input and output module 211, and controls whether to discharge the wastewater solution to the activated carbon filter 118 for dechlorination again by controlling the second drain valve 207. The singlechip 212 feeds back the data processing result to the third drain valve 208 through the distributed digital input and output module 211, and controls whether the wastewater solution is drained into the resin tank 119 for secondary metal ion removal treatment by controlling the third drain valve 208. The single chip microcomputer 212 feeds back the data processing result to the fourth drain valve 209 through the distributed digital input and output module 211, and controls whether the wastewater solution flows into the third security filter 122 for secondary impurity removal by controlling the fourth drain valve 209. Until the wastewater monitored by the water inlet adjusting and monitoring device 200 reaches the water inlet index of the first-stage electrically-driven ionic membrane unit 123, the single-chip microcomputer 212 feeds back the data processing result to the first drain valve 206 through the distributed digital input and output module 211, and controls the wastewater solution to flow into the first-stage electrically-driven ionic membrane unit 123 for deep concentration processing by controlling the first drain valve 206.

The first stage electrically driven ionic membrane unit 123 further concentrates the high pressure reverse osmosis concentrated solution by using an electrically driven ionic membrane, so that the high salt water with TDS of 50000mg/L can be concentrated to 120000mg/L, the produced water enters the second stage reverse osmosis device 128, and the concentrated solution enters the first concentrated salt water tank 124. The first-stage electric drive produced water is treated by the second-stage reverse osmosis, the second-stage reverse osmosis produced water enters the fresh water tank 129, and the second-stage reverse osmosis concentrated solution is delivered to the first intermediate water tank 108 again. The concentrated salt solution in the first concentrated salt water tank 124 is sent to a second-level electrically-driven ionic membrane unit 126 through a third booster water pump 125, the high-pressure reverse osmosis concentrated solution is further concentrated by utilizing an electrically-driven ionic membrane, the high-salt water with the TDS of 120000mg/L can be concentrated to 200000mg/L, the water produced by the second-level electrically-driven ionic membrane unit is sent to the medium-pressure water tank 112 to be mixed with the medium-pressure reverse osmosis concentrated solution, and the residual concentrated solution in the second-level electrically-driven ionic membrane unit is sent to a second concentrated salt water tank 127.

After the high-salt-content wastewater 101 is subjected to preliminary reduction treatment and deep concentration treatment, more than 95% of wastewater solution can be recovered to the fresh water tank 129, and the wastewater is recycled.

It should be noted that the above-mentioned embodiments are exemplary, and that those skilled in the art, having benefit of the present disclosure, may devise various arrangements that are within the scope of the present disclosure and that fall within the scope of the invention. It should be understood by those skilled in the art that the present specification and figures are illustrative only and are not limiting upon the claims. The scope of the invention is defined by the claims and their equivalents.

Claims (8)

1. The water inlet control system based on the high-salinity wastewater reduction process is characterized in that the water inlet control system monitors parameter indexes of the high-salinity wastewater (101) subjected to reduction treatment in real time through a water inlet adjusting and monitoring device (200) and adjusts the parameter indexes according to the water inlet indexes of a later process, wherein,

the high-salt-content wastewater (101) is subjected to a reduction process to obtain a high-pressure reverse osmosis concentrated solution, the later-stage process is a deep concentration treatment of the high-pressure reverse osmosis concentrated solution based on a first-stage electrically-driven ionic membrane unit (123) and a second-stage electrically-driven ionic membrane unit (126) in sequence, wherein,

residual chlorine, heavy metal ions and colloid in the high-pressure reverse osmosis concentrated solution are adsorbed by an activated carbon filter (118) and a resin tank (119), tiny suspended matters and colloid are filtered by a third security filter (122), and the filtered wastewater is sent to the water inlet adjustment monitoring device (200), wherein,

based on the water inlet index of a primary electrically-driven ionic membrane unit (123) and the parameter index monitored by the water inlet adjusting and monitoring device (200), performing at least one circulation treatment on the filtered wastewater by using at least one treatment device selected from a water temperature regulator (205), an activated carbon filter (118), a resin tank (119) and a third security filter (122) under the control of the water inlet adjusting and monitoring device (200) until the filtered wastewater reaches the water inlet index of the primary electrically-driven ionic membrane unit (123);

the high-salt-content wastewater reduction process at least comprises the following steps: the wastewater is adjusted to an alkaline environment based on a pretreatment process by adopting a dosing mode, wherein,

homogenizing and homogenizing the high-salt-content wastewater (101), adding more than one coagulant selected from lime, sodium hydroxide, sodium carbonate, polyaluminium chloride and polyacrylamide and more than one softener for precipitation, adjusting the wastewater to be in an alkaline environment, discharging the precipitate into a sludge tank, feeding the precipitated wastewater into a tubular micro-filter (106) for filtration,

wherein the dosage is adjusted according to the change condition of each ion concentration of the actual inlet water of the high-salinity wastewater (101);

and the pretreated high-salt-content wastewater (101) is subjected to reduction treatment sequentially by a medium-pressure reverse osmosis device (111) adopting a medium-pressure membrane element with the width of a flow channel being 1.524-1.778 mm and a high-pressure reverse osmosis device (115) adopting a high-pressure membrane element with the width of the flow channel being 1.905-2.159 mm,

the preliminary reduction processing includes the steps of: the pretreated wastewater is filtered by a first cartridge filter (110) and then is sent to the medium-pressure reverse osmosis device (111); treating the wastewater by the medium-pressure reverse osmosis device (111) to obtain medium-pressure reverse osmosis produced water and medium-pressure reverse osmosis concentrated solution, wherein the medium-pressure reverse osmosis produced water is sent to a secondary reverse osmosis device (128), and the medium-pressure reverse osmosis concentrated solution is filtered by a second cartridge filter (114) and then sent to the high-pressure reverse osmosis device (115); the filtered medium-pressure reverse osmosis concentrated solution is treated by the high-pressure reverse osmosis device (115) to obtain high-pressure reverse osmosis produced water and a high-pressure reverse osmosis concentrated solution, wherein the high-pressure reverse osmosis produced water is sent to a secondary reverse osmosis device (128), and the high-pressure reverse osmosis concentrated solution is subjected to deep concentration treatment;

the water inlet adjusting and monitoring device (200) monitors the high-salt-content wastewater (101) subjected to reduction treatment through a temperature detector (201), a chloride ion detector (202), a heavy metal ion detector (203) and a fine particle detector (204) to obtain the parameter index.

2. The water inlet control system as claimed in claim 1, wherein the temperature detector (201) is used for monitoring wastewater temperature, the chloride ion detector (202) is used for monitoring wastewater chloride ion concentration, the heavy metal ion detector (203) is used for monitoring heavy metal ion concentration, and the fine particle detector (204) is used for monitoring colloid and fine suspended matter content;

the water inlet control system further comprises: a water temperature regulator (205) for regulating the temperature of the wastewater, a first drain valve (206) for controlling the wastewater to flow into the primary electrically-driven ionic membrane unit (123), a second drain valve (207) for controlling the wastewater to flow into the activated carbon filter (118), a third drain valve (208) for controlling the wastewater to flow into the resin tank (119), and a fourth drain valve (209) for controlling the wastewater to flow into the third security filter (122);

the system comprises a distributed A/D acquisition module (210) for receiving monitoring data, a single chip microcomputer (212) for data processing, a PC terminal (213) for controlling the single chip microcomputer (212) and a distributed digital input and output module (211) for feeding back control information.

3. The water inlet control system of claim 2, wherein the water inlet adjusting and monitoring device (200) transmits information detected by the temperature detector (201), the chloride ion detector (202), the heavy metal ion detector (203) and the micro particle detector (204) to the single chip microcomputer (212) through a distributed A/D acquisition module (210), the single chip microcomputer (212) performs data processing on the monitoring information based on the water inlet requirement of the first-stage electrically-driven ionic membrane unit (123) input by the PC terminal (213), and the processing result is fed back to the water temperature and drain valve regulator (205), the first drain valve (206), the second drain valve (207), the third drain valve (208) and the fourth drain valve (209) through a distributed digital input and output module (211).

4. The water inlet control system as claimed in claim 1, wherein the water inlet index of the primary electrically driven ionic membrane unit (123) is: the water inlet temperature is 5-40 ℃; the content of residual chlorine is not more than 0.05 mg/L; the content of heavy metal ions is not more than 0.1 mg/L; the sewage quality index SDI is not more than 3.0.

5. The water inlet control system of claim 1, wherein the deep concentration process comprises the steps of:

the high-pressure reverse osmosis concentrated solution is treated by the water inlet control system and then is sent to a first-stage electric driven ionic membrane unit (123);

the water is treated by the primary electric-driven ionic membrane unit (123) to obtain primary electric-driven strong brine and primary electric-driven water production, wherein the primary electric-driven water production enters a secondary reverse osmosis device (128), and the primary electric-driven strong brine is sent to a secondary electric-driven ionic membrane unit (126) through a third booster water pump (125);

and (3) processing the concentrated solution by the secondary electric drive ionic membrane unit (126) to obtain secondary electric drive concentrated salt solution and secondary electric drive produced water, wherein the secondary electric drive produced water is sent to a medium-pressure water pool (112), and the secondary electric drive concentrated salt solution is sent to a second concentrated salt water tank (127).

6. The feed water control system as claimed in claim 5 wherein the product water fed to the secondary reverse osmosis unit (128) is treated to produce secondary reverse osmosis product water and secondary reverse osmosis concentrate, wherein the secondary reverse osmosis product water is fed to a fresh water tank (129) and the secondary reverse osmosis concentrate is fed to the first intermediate water tank (108).

7. The water inlet control system as recited in claim 1, characterized in that the activated carbon filter (118) is configured to adsorb chlorine not removed during the reduction process, while adsorbing small organic molecules, colloids, and heavy metal ions; the resin tank (119) is provided with ion exchange resin for adsorbing heavy metal ions in the solution treated by the activated carbon filter (118); the third cartridge filter (122) is used for filtering micro suspended matters and colloids in the solution.

8. A reduction treatment method of high-salt-content wastewater is characterized by comprising a wastewater pretreatment process, a wastewater reduction treatment process and a wastewater deep concentration treatment process, wherein,

in the wastewater pretreatment process, after homogenizing and homogenizing the high-salinity wastewater (101), adding more than one coagulant selected from lime, sodium hydroxide, sodium carbonate, polyaluminium chloride and polyacrylamide and more than one softener for precipitation, and adjusting the wastewater to be in an alkaline environment, wherein the dosage is adjusted according to the change condition of each ion concentration of the actual inflow water of the high-salinity wastewater (101);

in the wastewater reduction treatment process, the pretreated high-salt-content wastewater (101) is subjected to reduction treatment by sequentially passing through a medium-pressure reverse osmosis device (111) adopting a medium-pressure membrane element with the width of a flow channel of 1.524-1.778 mm and a high-pressure reverse osmosis device (115) adopting a high-pressure membrane element with the width of a flow channel of 1.905-2.159 mm,

the preliminary reduction processing includes the steps of: the pretreated wastewater is filtered by a first cartridge filter (110) and then is sent to the medium-pressure reverse osmosis device (111); treating the wastewater by the medium-pressure reverse osmosis device (111) to obtain medium-pressure reverse osmosis produced water and medium-pressure reverse osmosis concentrated solution, wherein the medium-pressure reverse osmosis produced water is sent to a secondary reverse osmosis device (128), and the medium-pressure reverse osmosis concentrated solution is filtered by a second cartridge filter (114) and then sent to the high-pressure reverse osmosis device (115); the filtered medium-pressure reverse osmosis concentrated solution is treated by the high-pressure reverse osmosis device (115) to obtain high-pressure reverse osmosis produced water and a high-pressure reverse osmosis concentrated solution, wherein the high-pressure reverse osmosis produced water is sent to a secondary reverse osmosis device (128), and the high-pressure reverse osmosis concentrated solution is subjected to deep concentration treatment;

the advanced wastewater concentration treatment process is sequentially based on a primary electric driven ionic membrane unit (123) and a secondary electric driven ionic membrane unit (126) to treat wastewater passing through the wastewater pretreatment process and the wastewater reduction treatment process, wherein after residual chlorine, heavy metal ions and colloid of the wastewater entering the advanced wastewater concentration treatment process are adsorbed by an activated carbon filter (118) and a resin tank (119) through a water inlet control system, tiny suspended matters and colloid are filtered out through a third security filter (122), and the filtered wastewater is sent to a water inlet adjustment monitoring device (200),

based on the degree of depth concentrated in-process one-level electric drive ionic membrane unit (123) index of intaking with it adjusts monitoring devices (200) monitoring to intake the waste water information after the filtration, under the control of the adjustment monitoring devices that intakes (200), use temperature regulator (205), activated carbon filter (118), at least one processing apparatus in resin jar (119) and third safety filter (122) to carry out once at least circulation treatment to the waste water after the filtration, until waste water after the filtration reaches one-level electric drive ionic membrane unit (123) index of intaking.

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