A high-salt concentration system and a concentration process based on the system

Abstract

The application relates to a high-salt concentration system, which comprises a concentration membrane assembly; a first water inlet of the concentration assembly is connected with a water outlet of a raw water pool through a raw water inlet pipeline; a second water inlet of the concentration membrane assembly is connected with the water outlet of the raw water pool through a raw water supplement pipeline; a first water outlet of the concentration membrane assembly is connected with a water inlet of a concentrated water pool through a concentrated water outlet pipeline; a second water outlet of the concentration membrane assembly is connected with a water inlet of a product water pool through a product water outlet pipeline; a pressure relief pipeline is arranged at the second water inlet of the concentration membrane assembly; a circulating pipeline is arranged between a third water outlet of the concentration membrane assembly and the second water inlet of the concentration membrane assembly; and a flushing branch is arranged on the circulating pipeline. The high-salt concentration system has a wider application range, high processing efficiency, lower operation cost, energy recovery, lower energy consumption, controllable and adjustable concentration ratio, solves the problem of blockage, has low equipment cost and is safer in operation.

Description

TECHNICAL FIELD

[0001] The present application relates to the technical field of water treatment in environmental protection, and in particular to a high-salt concentration system and a concentration process based on the system. BACKGROUND

[0002] Atmosphere, water and soil are the three main pollution sources of environmental protection management, wherein water is divided into municipal sewage and industrial wastewater, and salt-containing industrial wastewater is a high-difficulty problem in the water treatment industry. At present, the process commonly used for zero discharge of salt-containing industrial wastewater is: wastewater dosing pretreatment, precision filtration, ultrafiltration, reverse osmosis, nanofiltration to MVR evaporation crystallization (frozen crystallization). After the front-end pretreatment, reverse osmosis and nanofiltration treatment are completed, the high-concentration water of monovalent salt enters the MVR evaporation crystallization. As the last step of zero discharge of working wastewater, the MVR evaporation crystallization can separate the salt and water in the concentrated water to obtain water and salt, but the MVR evaporation crystallization has the disadvantages of high power consumption and high equipment investment cost.

[0003] Therefore, high-salt concentration technology emerges as the times require. This technology mainly concentrates the water of the concentrated water to be entered into the MVR system after nanofiltration and reverse osmosis of high-salt salt, so as to achieve the purpose of reducing the amount of concentrated water. The main high-salt concentration systems on the market at present mainly include high-pressure butterfly pipe reverse osmosis (DTRO) and coiled pipe reverse osmosis (STRO) high-salt concentration technologies. However, both DTRO and STRO have certain disadvantages. How to solve the problems existing in the current high-salt concentration represented by DTRO and STRO, design a reasonably structured device and reduce the cost of the device has become a difficult problem to be solved in the current high-salt concentration field. SUMMARY

[0004] The purpose of the present application is to solve the problems in the prior art, based on the semi-permeation principle and the pressure-driven membrane separation technology, to provide a high-salt concentration system and a concentration process based on the system.

[0005] To achieve the above-mentioned purpose, the technical solution adopted by the present application is as follows:

[0006] The first aspect of the present application is to provide a high-salt concentration system, comprising: a concentration membrane assembly; a first water inlet of the concentration assembly is connected with a water outlet of an original water pool through an original water inlet pipeline, a second water inlet of the concentration membrane assembly is connected with the water outlet of the original water pool through an original water supplement pipeline, a first water outlet of the concentration membrane assembly is connected with a water inlet of a concentrated water pool through a concentrated water outlet pipeline, and a second water outlet of the concentration membrane assembly is connected with a water inlet of a product water pool through a product water outlet pipeline.

[0007] The second water inlet of the concentration membrane assembly is provided with a pressure relief pipeline; the circulation pipeline is arranged between the third water outlet of the concentration membrane assembly and the second water inlet of the concentration membrane assembly; and a flushing branch is arranged on the circulation pipeline;

[0008] The concentration membrane assembly comprises a first SPX energy recovery machine, a first membrane assembly connected between the first water inlet and the second water outlet of the first SPX energy recovery machine, a second SPX energy recovery machine arranged in parallel with the first SPX energy recovery machine, and a second membrane assembly connected between the first water inlet and the second water outlet of the second SPX energy recovery machine.

[0009] The connections are all pipeline connections.

[0010] Preferably, from the water outlet of the raw water tank to the first water inlet of the concentration membrane assembly, the raw water inlet pipeline comprises, in sequence, a sixteenth ball valve, a fourth liquid pump, a fifteenth one-way check valve, a pressure switch, a first ball valve, a buffer tank, a flow switch, a twenty-second pressure relief valve, and a third pneumatic tee ball valve; wherein

[0011] The third pneumatic tee ball valve is connected with the first water inlet of the first SPX energy recovery machine and the first water inlet of the second SPX energy recovery machine, respectively.

[0012] The connections are all pipeline connections.

[0013] Preferably, from the water outlet of the raw water tank to the second water inlet of the concentration membrane assembly, the raw water supplement pipeline comprises, in sequence, a first liquid pump, a nineteenth ball valve, a second liquid pump, a twentieth one-way check valve, a twenty-third safety valve, a thermometer, a first flow meter, a seventh ball valve, a fourteenth pneumatic tee ball valve, a third pressure gauge, a third liquid pump, a first pressure gauge, and a twelfth pneumatic tee ball valve; wherein

[0014] The twelfth pneumatic tee ball valve is connected with the second water inlet of the first membrane assembly and the second water inlet of the second membrane assembly, respectively.

[0015] The connections are all pipeline connections.

[0016] Preferably, from the first water outlet of the concentration membrane assembly to the water inlet of the concentrated water tank, the concentrated water outlet pipeline comprises, in sequence, a third pneumatic tee ball valve, a twenty-second pressure relief valve, a flow switch, a buffer tank, a second ball valve, a fifth liquid pump, a seventeenth one-way check valve, an eighteenth ball valve, and a second flow meter; wherein

[0017] The third pneumatic tee ball valve is connected with the first water outlet of the first SPX energy recovery machine and the first water outlet of the second SPX energy recovery machine, respectively.

[0018] The connections are all pipe connections.

[0019] Preferably, from the second water outlet of the concentrated membrane assembly to the water inlet of the product water tank, the product water outlet pipeline comprises, in sequence, an eighth pneumatic three-way ball valve; wherein,

[0020] The eighth pneumatic three-way ball valve is connected with the second water outlet of the first membrane assembly and the second water outlet of the second membrane assembly, respectively;

[0021] The connections are all pipe connections.

[0022] Preferably, from the third water outlet of the concentrated membrane assembly to the second water inlet of the concentrated membrane assembly, the circulation pipeline comprises, in sequence, a thirteenth pneumatic three-way ball valve, a second pressure gauge, a twenty-first one-way check valve, a fourteenth pneumatic three-way ball valve, a third pressure gauge, a third liquid pump, a first pressure gauge, and a twelfth pneumatic three-way ball valve; wherein,

[0023] The thirteenth pneumatic three-way ball valve is connected with the third water outlet of the first SPX energy recovery machine and the third water outlet of the second SPX energy recovery machine, respectively;

[0024] The twelfth pneumatic three-way ball valve is connected with the second water inlet of the first membrane assembly and the second water inlet of the second membrane assembly, respectively;

[0025] The connections are all pipe connections.

[0026] Preferably, the pressure relief pipeline comprises, in sequence, a ninth ball valve, a tenth pressure relief valve, and a second breather valve from the second water inlet of the first membrane assembly; and a fourth ball valve, an eleventh pressure relief valve, and a first breather valve from the second water inlet of the second membrane assembly;

[0027] The flushing branch comprises a sixth ball valve connected with the fourteenth pneumatic three-way ball valve and a fifth ball valve arranged between the thirteenth pneumatic three-way ball valve and the second pressure gauge;

[0028] The connections are all pipe connections.

[0029] The second aspect of the present application is to provide a high-salt concentration process based on the high-salt concentration system as described above, comprising the following steps:

[0030] S1, the raw water with monovalent salt TDS content of 50000-80000 ppm is transported to the first high salt concentration system, after the treatment of the first high salt concentration system, the produced water with lower monovalent salt TDS content is transported to the seawater desalination reverse osmosis system, and the concentrated water with higher monovalent salt TDS content is transported to the second high salt concentration system;

[0031] S2, after the treatment of the seawater desalination reverse osmosis system, the produced water with lower monovalent salt TDS content is reused, and the concentrated water with higher monovalent salt TDS content is transported back to the first high salt concentration system;

[0032] S3, after the treatment of the second high salt concentration system, the produced water with lower monovalent salt TDS content is transported back to the first high salt concentration system, and the concentrated water with higher monovalent salt TDS content is transported to the third high salt concentration system;

[0033] S4, after the treatment of the third high salt concentration system, the produced water with lower monovalent salt TDS content is transported back to the second high salt concentration system, and the concentrated water with higher monovalent salt TDS content is transported to the MVR evaporation crystallization system.

[0034] The third aspect of the application is to provide a medium-high salt concentration process based on the high salt concentration system as described above, and the steps include:

[0035] S1, the raw water with monovalent salt TDS content of 80000-120000 ppm is transported to the first high salt concentration system, after the treatment of the first high salt concentration system, the produced water with lower monovalent salt TDS content is transported to the third high salt concentration system, and the concentrated water with higher monovalent salt TDS content is transported to the second high salt concentration system;

[0036] S2, after the treatment of the second high salt concentration system, the produced water with lower monovalent salt TDS content is transported back to the first high salt concentration system, and the concentrated water with higher monovalent salt TDS content is transported to the MVR evaporation crystallization system;

[0037] S3, after the treatment of the third high salt concentration system, the produced water with lower monovalent salt TDS content is transported to the seawater desalination reverse osmosis system, and the concentrated water with higher monovalent salt TDS content is transported back to the first high salt concentration system;

[0038] S4, after the treatment of the seawater desalination reverse osmosis system, the produced water with lower monovalent salt TDS content is reused, and the concentrated water with higher monovalent salt TDS content is transported back to the third high salt concentration system.

[0039] The fourth aspect of the application is to provide a super-high salt concentration process based on the high salt concentration system as described above, and the steps include:

[0040] S1, the raw water with monovalent salt TDS content of 120000-160000 ppm is transported to the first high salt concentration system, after the treatment of the first high salt concentration system, the produced water with lower monovalent salt TDS content is transported to the second high salt concentration system, and the concentrated water with higher monovalent salt TDS content is transported to the MVR evaporation crystallization system;

[0041] S2, after the treatment of the second high salt concentration system, the produced water with lower monovalent salt TDS content is transported to the third high salt concentration system, and the concentrated water with higher monovalent salt TDS content is transported back to the first high salt concentration system;

[0042] S3, after the treatment of the third high salt concentration system, the produced water with lower monovalent salt TDS content is transported to the seawater desalination reverse osmosis system, and the concentrated water with higher monovalent salt TDS content is transported back to the second high salt concentration system;

[0043] S4, after the treatment of the seawater desalination reverse osmosis system, the produced water with lower monovalent salt TDS content is reused, and the concentrated water with higher monovalent salt TDS content is transported back to the third high salt concentration system.

[0044] Compared with the prior art, the above technical scheme has the following technical effects:

[0045] ①The application range is wider: the application range of the raw water mainly containing monovalent salt can reach TDS: 50000-160000 ppm, and the concentrated water TDS can reach 160000-210000 ppm after concentration. Different processes can be selected according to different salinity, the treatment method is more flexible, and the concentrated water concentration of STRO and DTRO is only 80000-140000 ppm, which has a significant advantage, and the concentration ratio can be increased by more than one time;

[0046] ②High processing efficiency: the working mode of circulating cross flow is adopted, the molecular weight of the high salt concentration membrane is 80-100 dal, the water production rate is 30%-85%, even higher, the best water production rate is 40%-65%, and the ratio can be adjusted according to different water conditions. Compared with the water production rate of 40%-50% of STRO and DTRO, the processing efficiency is higher;

[0047] ③Lower operation cost, energy can be recycled and energy consumption is lower: the operation pressure range is 4.5-6.5 Mpa, and the self-developed SPX energy recovery machine is equipped, the power consumption per ton of water is only 3.5-6.5 kw·h / ton, compared with DTRO and STRO, the energy consumption is saved by more than 1 / 2;

[0048] 4. The concentration ratio is controllable and adjustable: the design of the circulating cross flow makes the concentration ratio adjustable. In the range of 4.5-6.5Mpa allowed by the pressure level, the corresponding concentration ratio can be adjusted according to the calculation, the water production rate can be 30%-85%, and according to the different raw water concentration, the concentrated water range can be 100000-210000ppm, and the optimal concentrated water range is 160000-210000ppm;

[0049] 5. The problem of blockage is effectively solved: the circulating cross flow mode of the raw water entering the system and the original concentrated water mixing has the effect of self-cleaning, which effectively reduces the problem of blockage that may exist in the high-salt concentration system;

[0050] 6. The equipment cost is low: the concentrated water one-price salt TDS range is about 160000-210000ppm, and the highest operating pressure is lower than 7.5Mpa. The pressure level of the existing DTRO and STRO high-salt salt equipment is 7.5Mpa, 9Mpa, 12Mpa, and 16Mpa. Compared with the above, the lower pressure level makes the equipment cost reduce to about 1 / 3 of the original, or even lower;

[0051] 7. The operation is safer: the lower operating pressure level not only makes the equipment cost per ton lower and reduces the operating power consumption, but also makes the safety of the equipment guaranteed. BRIEF DESCRIPTION OF DRAWINGS

[0052] Figure 1 It is a structural schematic diagram of the high-salt concentration system in the application;

[0053] Wherein, the reference signs include: raw water pool 1; Concentration membrane assembly 2; First SPX energy recovery machine 21; First membrane assembly 22; Second SPX energy recovery machine 23; Second membrane assembly 24; Concentrated water pool 3; Water production pool 4; Buffer tank 5; First ball valve V1; Second ball valve V2; Third pneumatic tee ball valve V3; Fourth ball valve V4; Fifth ball valve V5; Sixth ball valve V6; Seventh ball valve V7; Eighth pneumatic tee ball valve V8; Ninth ball valve V9; Tenth pressure relief valve V10; Eleventh pressure relief valve V11; Twelfth pneumatic tee ball valve V12; Thirteenth pneumatic tee ball valve V13; Fourteenth pneumatic tee ball valve V14; Fifteenth check valve V15; Sixteenth ball valve V16; Seventeenth check valve V17; Eighteenth ball valve V18; Nineteenth ball valve V19; Twentieth check valve V20; Twenty-first check valve V21; Twenty-second pressure relief valve V22; Twenty-third safety valve V23; First breathing valve H1; Second breathing valve H2; First liquid pump M0; Second liquid pump M1; Third liquid pump M2; Fourth liquid pump M3; Fifth liquid pump M4; Pressure switch Pk; Flow switch Qk; Thermometer T1; First flow meter Q1; Second flow meter Q2; First pressure gauge P1; Second pressure gauge P2; Third pressure gauge Pmax;

[0054] Figure 2 It is the flow chart of the high salt concentration process in the application;

[0055] Figure 3 It is the flow chart of the high salt concentration process in the application;

[0056] Figure 4 It is the flow chart of the high salt concentration process in the application. DETAILED DESCRIPTION

[0057] The technical solutions in the embodiments of the application will be clearly and completely described below with reference to the drawings in the embodiments of the application. Obviously, the described embodiments are only part of the embodiments of the application, rather than all the embodiments of the application. Based on the embodiments in the application, all other embodiments obtained by those skilled in the art without creative work fall within the protection scope of the application.

[0058] It should be noted that the embodiments in the application and the features in the embodiments can be combined with each other without conflict.

[0059] The application will be further described below with reference to the drawings and specific embodiments, but the application is not limited by the embodiments.

[0060] Embodiment 1

[0061] As Figure 1As shown, the embodiment provides a high-salt concentration system, comprising: a concentration membrane assembly 2; the concentration assembly 2 comprises: a first SPX energy recovery machine 21, a first membrane assembly 22 connected with the first water inlet and the second water outlet of the first SPX energy recovery machine 21, a second SPX energy recovery machine 23 arranged in parallel with the first SPX energy recovery machine 21, and a second membrane assembly 24 connected with the first water inlet and the second water outlet of the second SPX energy recovery machine 23; wherein,

[0062] The water outlet of the raw water tank is connected with the sixteenth ball valve V16 and the first liquid pump M0 respectively, the sixteenth ball valve V16, the fourth liquid pump M3, the fifteenth check valve V15, the pressure switch Pk, the first ball valve V1, the buffer tank 5, the flow switch Qk, the twenty-second pressure relief valve V22 and the third pneumatic three-way ball valve V3 are connected in sequence, the third pneumatic three-way ball valve V3 is connected with the first water inlet of the first SPX energy recovery machine 21 and the first water inlet of the second SPX energy recovery machine 23 respectively; the first liquid pump M0, the nineteenth ball valve V19, the second liquid pump M1, the twentieth check valve V20, the twenty-third safety valve V23, the thermometer T1, the first flow meter Q1, the seventh ball valve V7, the fourteenth pneumatic three-way ball valve V14, the third pressure gauge Pmax, the third liquid pump M2, the first pressure gauge P1 and the twelfth pneumatic three-way ball valve V12 are connected in sequence, the twelfth pneumatic three-way ball valve V12 is connected with the second water inlet of the first membrane assembly 22 and the second water inlet of the second membrane assembly 24 respectively;

[0063] The first water inlets of the first SPX energy recovery machine 21 and the second SPX energy recovery machine 23 are the first water outlets of the first SPX energy recovery machine 21 and the second SPX energy recovery machine 23 respectively; in this way, the third pneumatic three-way ball valve V3, the twenty-second pressure relief valve V22, the flow switch Qk, the buffer tank 5, the second ball valve V2, the fifth liquid pump M4, the seventeenth check valve V17, the eighteenth ball valve V18 and the second flow meter Q2 connected with the first water outlets of the first SPX energy recovery machine 21 and the second SPX energy recovery machine 23 respectively are connected to the water inlet of the concentrated water tank 3 in sequence;

[0064] The second water outlets of the first membrane assembly 22 and the second membrane assembly 24 are connected with the eighth pneumatic three-way ball valve V8 respectively, and the eighth pneumatic three-way ball valve V8 is connected to the water inlet of the product water tank 4;

[0065] The third water outlet of the first SPX energy recovery machine 21 and the third water outlet of the second SPX energy recovery machine 23 are connected with the thirteenth pneumatic three-way ball valve V13, the thirteenth pneumatic three-way ball valve V13, the second pressure gauge P2, the twenty-first one-way check valve V21 are sequentially connected to the fourteenth pneumatic three-way ball valve V14, and are connected to the second water inlet of the first membrane assembly 22 and the second water inlet of the second membrane assembly 24 through the third pressure gauge Pmax, the third liquid pump M2, the first pressure gauge P1 and the twelfth pneumatic three-way ball valve V12;

[0066] The second water inlet of the first membrane assembly 22 is sequentially connected with the ninth ball valve V9, the tenth pressure relief valve V10 and the second breathing valve H2; the second water inlet of the second membrane assembly 24 is sequentially connected with the fourth ball valve V4, the eleventh pressure relief valve V11 and the first breathing valve H1;

[0067] The fourteenth pneumatic three-way ball valve V14 is connected with the sixth ball valve V6, and the fifth ball valve V5 is connected between the thirteenth pneumatic three-way ball valve V13 and the second pressure gauge P2.

[0068] The connections are all pipeline connections.

[0069] Embodiment 2

[0070] The embodiment provides a control method of the high-salt concentration system as described in Embodiment 1, and the steps include:

[0071] S1, open V1, V9, V16, V18, V19, close V5, V6, switch to V3ac, V12ab, V8ab, V13ab, V14bc, start M3, until Pk feedback signal;

[0072] S2, switch to V3bc, V8bc, V12bc, V13ac, V14bc, close V9, open V4, keep M3 started, start M0 and M2 at power frequency, open V7, start M1 at the frequency of the frequency converter, set the working period T1 and the upper limit of pressure Pmax, when T1 or Pmax is reached, the working period ends;

[0073] S3, until Pk feedback signal, close M3, close V1, switch to V12ab, V13ab, V8ab, V3ac, V14bc, keep MO, M1, M2 started, open V9; after the pressure relief is completed, open V2, start M4, when the QK feedback signal is cut off, close M4, close V2;

[0074] S4, open V1, V9, keep V3ac, V12ab, V8ab, V13ab, V14bc, start M3, until Pk feedback signal;

[0075] S5, close M3, close V1, V9, switch V3bc, V12bc, V8bc, V13ac, V14bc, keep M0, M1, M2 on, open V4; after pressure relief, open V2, start M4, when QK feedback signal is broken, close M4, close V2;

[0076] S6, open V1, V4, keep V3bc, V12bc, V13ac, V8bc, V14bc, start M3, until Pk feedback signal;

[0077] S7, repeat steps S3-S6;

[0078] S8, when the membrane front and back pressure difference reaches the set flushing pressure difference, open V5, V6, close V7, V4, keep V3ac, V12ab, V8bc, V13ab, V14ac, start M2, after flushing, switch V3bc, V12bc, V8ab, V13ac, V14ac, close V7, V9, continue flushing; after all flushing is completed, repeat steps S1-S7.

[0079] Example 3

[0080] As shown in Figure 2 , the embodiment provides a high-salt concentration process based on the high-salt concentration system as described in Example 1, the steps comprising:

[0081] S1, the raw water with monovalent salt TDS content of 50000-80000 ppm is transported to the first high-salt concentration system, after being treated by the first high-salt concentration system with an operating pressure of 4.5-5.2 MPa, the produced water with monovalent salt TDS content of 25000-40000 ppm is transported to the seawater desalination reverse osmosis system, and the concentrated water with monovalent salt TDS content of 65000-105000 ppm is transported to the second high-salt concentration system;

[0082] S2, after being treated by the seawater desalination reverse osmosis system, the produced water with lower monovalent salt TDS content is reused, and the concentrated water with monovalent salt TDS content of 50000-75000 ppm is transported back to the first high-salt concentration system;

[0083] S3, after being treated by the second high-salt concentration system with an operating pressure of 4.8-5.5 MPa, the produced water with monovalent salt TDS content of 45000-80000 ppm is transported back to the first high-salt concentration system, and the concentrated water with monovalent salt TDS content of 85000-140000 ppm is transported to the third high-salt concentration system;

[0084] S4, after the third high-salt concentration system with an operating pressure of 5.0-6.5 MPa is processed, the produced water with a monovalent salt TDS content of 60,000-120,000 ppm is transported back to the second high-salt concentration system, and the concentrated water with a monovalent salt TDS content of 160,000-210,000 ppm is transported to the MVR evaporation crystallization system.

[0085] Example 4

[0086] As shown in Figure 3 , the present embodiment provides a medium-high salt concentration process based on the high-salt concentration system as described in Example 1, the steps comprising:

[0087] S1, the raw water with a monovalent salt TDS content of 80,000-120,000 ppm is transported to the first high-salt concentration system, after the first high-salt concentration system with an operating pressure of 4.8-5.5 MPa is processed, the produced water with a monovalent salt TDS content of 50,000-80,000 ppm is transported to the third high-salt concentration system, and the concentrated water with a monovalent salt TDS content of 100,000-160,000 ppm is transported to the second high-salt concentration system;

[0088] S2, after the second high-salt concentration system with an operating pressure of 5.0-6.5 MPa is processed, the produced water with a monovalent salt TDS content of 60,000-120,000 ppm is transported back to the first high-salt concentration system, and the concentrated water with a monovalent salt TDS content of 160,000-210,000 ppm is transported to the MVR evaporation crystallization system;

[0089] S3, after the third high-salt concentration system with an operating pressure of 4.8-5.2 MPa is processed, the produced water with a monovalent salt TDS content of 25,000-40,000 ppm is transported to the seawater desalination reverse osmosis system, and the concentrated water with a monovalent salt TDS content of 65,000-105,000 ppm is transported back to the first high-salt concentration system;

[0090] S4, after the seawater desalination reverse osmosis system is processed, the produced water with a lower monovalent salt TDS content is reused, and the concentrated water with a monovalent salt TDS content of 50,000-75,000 ppm is transported back to the third high-salt concentration system.

[0091] Example 5

[0092] As shown in Figure 4 , the present embodiment provides a super-high salt concentration process based on the high-salt concentration system as described in Example 1, the steps comprising:

[0093] S1, the raw water with monovalent salt TDS content of 120000 ppm-160000 ppm is transported to the first high salt concentration system, after the treatment of the first high salt concentration system with the operation pressure of 5.0 Mpa-6.5 Mpa, the produced water with monovalent salt TDS content of 60000 ppm-120000 ppm is transported to the second high salt concentration system, and the concentrated water with monovalent salt TDS content of 160000 ppm-210000 ppm is transported to the MVR evaporation crystallization system;

[0094] S2, after the treatment of the second high salt concentration system with the operation pressure of 4.8 Mpa-5.5 Mpa, the produced water with monovalent salt TDS content of 50000 ppm-80000 ppm is transported to the third high salt concentration system, and the concentrated water with monovalent salt TDS content of 100000 ppm-160000 ppm is transported back to the first high salt concentration system;

[0095] S3, after the treatment of the third high salt concentration system with the operation pressure of 4.5 Mpa-5.2 Mpa, the produced water with monovalent salt TDS content of 25000 ppm-40000 ppm is transported to the seawater desalination reverse osmosis system, and the concentrated water with monovalent salt TDS content of 65000 ppm-105000 ppm is transported back to the second high salt concentration system;

[0096] S4, after the treatment of the seawater desalination reverse osmosis system, the produced water with lower monovalent salt TDS content is reused, and the concentrated water with monovalent salt TDS content of 50000 ppm-75000 ppm is transported back to the third high salt concentration system.

[0097] Application example

[0098] The main component of the raw water is NaCl, and the content is 121943 mg / L, Cl - The content is 74000 mg / L, and the medium-high salt concentration process is used as described in example 4:

[0099] 1, the raw water flow is 200 L / h, the additional backflow water is added, the total flow of the inlet water is 386 L / min, after the treatment of the first high salt concentration system, the produced water flow is adjusted to 1.0 L / min, the initial working pressure is 4.99 MPa, the flow of the high-pressure pump is 26 L / min, the working period T1 is set, after the treatment of the first high salt concentration system, the produced water rate is 40%, the highest working pressure is 5.18 Mpa, the comprehensive concentrated water NaCl content is 151605 mg / L, a total of 231 L / min, enters the third high salt concentration system, the produced water NaCl content is 79098 mg / L, and the produced water is used as the inlet water of the second high salt concentration system, and the flow is 155 L / min;

[0100] 2. The concentrated water of the first high-salt concentration section is used as the feed water of the second high-salt concentration section, the water production flow rate is adjusted to 0.75 L / min, the initial working pressure is 5.30 MPa, the flow rate of the high-pressure pump is 26 L / min, the working cycle T2 is set, after the first high-salt concentration system, the water production rate is 45%, the maximum working pressure is 5.37 MPa, the total concentrated water NaCl content is 184563 mg / l, the MVR evaporation crystallization concentrated water flow rate is 127 L / min, the water production NaCl content is 118647 mg / l, the flow rate is 104 L / min, and the water production is used as the feed water of the first high-salt concentration system;

[0101] 3. The water production NaCl content in step 1 is 79098 mg / L, the flow rate is 155 L / min, and the concentrated water NaCl content after the second high-salt concentration system is 124055 mg / L, the flow rate is 109 L / min, the water production NaCl content is 34901 mg / l, the flow rate is 109 L / min, the initial working pressure is 4.78 MPa, the water production rate is 40%, and the maximum working pressure is 4.83 MPa;

[0102] 4. The water production NaCl content in step 3 is 34901 mg / L, which is used as the feed water of the seawater desalination reverse osmosis system, after the seawater desalination reverse osmosis, the water production salinity is 226 mg / L, the flow rate is 46 L / min, the concentrated water salinity is 55000 mg / L, the flow rate is 63 L / min, the water production rate is about 42%, the initial working pressure is 3.65 MPa, the maximum working pressure is 5.82 MPa, the concentrated water of the seawater desalination reverse osmosis system and the water production of the first high-salt concentration system are combined to be used as the feed water of the second high-salt concentration system, and the flow rate is 217 L / min.

[0103] The above only describes the preferred embodiments of the present application, and does not limit the implementation and protection scope of the present application. For those skilled in the art, it should be realized that any equivalent replacement and obvious changes made according to the content of the present application description and drawings should be included in the protection scope of the present application.

Claims

1. A high salt concentration system, comprising: The concentrated membrane assembly (2) is characterized in that the first water inlet of the concentrated membrane assembly (2) is connected with the water outlet of the raw water pool (1) through a raw water inlet pipeline, the second water inlet of the concentrated membrane assembly (2) is connected with the water outlet of the raw water pool (1) through a raw water supplement pipeline, the first water outlet of the concentrated membrane assembly (2) is connected with the water inlet of the concentrated water pool (3) through a concentrated water outlet pipeline, and the second water outlet of the concentrated membrane assembly (2) is connected with the water inlet of the product water pool (4) through a product water outlet pipeline. A second water inlet of the concentrated membrane assembly (2) is provided with a pressure relief pipeline, a third water outlet of the concentrated membrane assembly (2) and the second water inlet of the concentrated membrane assembly (2) are provided with a circulating pipeline, and the circulating pipeline is provided with a flushing branch. The concentrated membrane assembly (2) comprises a first SPX energy recovery machine (21), a first membrane assembly (22) with a first water inlet connected with a second water outlet of the first SPX energy recovery machine (21), a second SPX energy recovery machine (23) arranged in parallel with the first SPX energy recovery machine (21), and a second membrane assembly (24) with a first water inlet connected with a second water outlet of the second SPX energy recovery machine (23). From the water outlet of the raw water pool (1) to the first water inlet of the concentrated membrane assembly (2), the raw water inlet pipeline comprises, in sequence, a sixteenth ball valve (V16), a fourth liquid pump (M3), a fifteenth one-way check valve (V15), a pressure switch (Pk), a first ball valve (V1), a buffer tank (5), a flow switch (Qk), a twenty-second pressure relief valve (V22), and a third pneumatic three-way ball valve (V3). The third pneumatic three-way ball valve (V3) is connected with a first water inlet of the first SPX energy recovery machine (21) and a first water inlet of the second SPX energy recovery machine (23) respectively. From the water outlet of the raw water pool (1) to the second water inlet of the concentrated membrane assembly (2), the raw water supplement pipeline comprises, in sequence, a first liquid pump (M0), a nineteenth ball valve (V19), a second liquid pump (M1), a twentieth one-way check valve (V20), a twenty-third safety valve (V23), a thermometer (T1), a first flowmeter (Q1), a seventh ball valve (V7), a fourteenth pneumatic three-way ball valve (V14), a third pressure gauge (Pmax), a third liquid pump (M2), a first pressure gauge (P1), and a twelfth pneumatic three-way ball valve (V12). The twelfth pneumatic three-way ball valve (V12) is connected with a second water inlet of the first membrane assembly (22) and a second water inlet of the second membrane assembly (24) respectively. From the first water outlet of the concentrating membrane assembly (2) to the water inlet of the concentrated water tank (3), the concentrated water outlet pipeline comprises, in sequence, a third pneumatic three-way ball valve (V3), a twenty-second pressure relief valve (V22), a flow switch (Qk), a buffer tank (5), a second ball valve (V2), a fifth liquid pump (M4), a seventeenth one-way check valve (V17), an eighteenth ball valve (V18), and a second flow meter (Q2); The third pneumatic three-way ball valve (V3) is connected with the first water outlet of the first SPX energy recovery machine (21) and the first water outlet of the second SPX energy recovery machine (23) respectively. From the second water outlet of the concentrating membrane assembly (2) to the water inlet of the product water tank (4), the product water outlet pipeline comprises, in sequence, an eighth pneumatic three-way ball valve (V8); The eighth pneumatic three-way ball valve (V8) is connected with the second water outlet of the first membrane assembly (22) and the second water outlet of the second membrane assembly (24) respectively. From the third water outlet of the concentrating membrane assembly (2) to the second water inlet of the concentrating membrane assembly (2), the circulating pipeline comprises, in sequence, a thirteenth pneumatic three-way ball valve (V13), a second pressure gauge (P2), a twenty-first one-way check valve (V21), a fourteenth pneumatic three-way ball valve (V14), a third pressure gauge (Pmax), a third liquid pump (M2), a first pressure gauge (P1), and a twelfth pneumatic three-way ball valve (V12); The thirteenth pneumatic three-way ball valve (V13) is connected with the third water outlet of the first SPX energy recovery machine (21) and the third water outlet of the second SPX energy recovery machine (23) respectively. The twelfth pneumatic three-way ball valve (V12) is connected with the second water inlet of the first membrane assembly (22) and the second water inlet of the second membrane assembly (24) respectively. The pressure relief pipeline comprises, in sequence from the second water inlet of the first membrane assembly (22), a ninth ball valve (V9), a tenth pressure relief valve (V10), and a second breather valve (H2); and in sequence from the second water inlet of the second membrane assembly (24), a fourth ball valve (V4), an eleventh pressure relief valve (V11), and a first breather valve (H1); The flushing branch comprises a sixth ball valve (V6) connected with the fourteenth pneumatic three-way ball valve (V14) and a fifth ball valve (V5) arranged between the thirteenth pneumatic three-way ball valve (V13) and the second pressure gauge (P2); The connections are all pipeline connections.

2. A high salt concentration process based on the high salt concentration system of claim 1, characterized by the steps of Comprise: S1, deliver the raw water with monovalent salt TDS content of 50000ppm-80000ppm to the first high-salt concentration system, after treatment by the first high-salt concentration system, deliver the product water with lower monovalent salt TDS content to the seawater desalination reverse osmosis system, and deliver the concentrated water with higher monovalent salt TDS content to the second high-salt concentration system; S2, after the seawater desalination reverse osmosis system treatment, the monovalent salt TDS content of the lower water reuse, and the monovalent salt TDS content of the higher concentrated water is transported back to the first high salt concentration system; S3, after the second high salt concentration system treatment, the monovalent salt TDS content of the lower water is transported back to the first high salt concentration system, and the monovalent salt TDS content of the higher concentrated water is transported to the third high salt concentration system; S4, after the third high salt concentration system treatment, the monovalent salt TDS content of the lower water is transported back to the second high salt concentration system, and the monovalent salt TDS content of the higher concentrated water is transported to the MVR evaporation crystallization system.

3. A medium-high salt concentration process based on the high salt concentration system of claim 1, characterized by the steps of Comprising: S1, the monovalent salt TDS content of the original water of 80000-120000 ppm is transported to the first high salt concentration system, after the first high salt concentration system treatment, the monovalent salt TDS content of the lower water is transported to the third high salt concentration system, and the monovalent salt TDS content of the higher concentrated water is transported to the second high salt concentration system; S2, after the second high salt concentration system treatment, the monovalent salt TDS content of the lower water is transported back to the first high salt concentration system, and the monovalent salt TDS content of the higher concentrated water is transported to the MVR evaporation crystallization system; S3, after the third high salt concentration system treatment, the monovalent salt TDS content of the lower water is transported to the seawater desalination reverse osmosis system, and the monovalent salt TDS content of the higher concentrated water is transported back to the second high salt concentration system; S4, after the seawater desalination reverse osmosis system treatment, the monovalent salt TDS content of the lower water reuse, and the monovalent salt TDS content of the higher concentrated water is transported back to the third high salt concentration system.

4. A process for concentrating ultra-high salt based on the high salt concentration system as claimed in claim 1, wherein the steps of Comprising: S1, the monovalent salt TDS content of the original water of 80000-120000 ppm is transported to the first high salt concentration system, after the first high salt concentration system treatment, the monovalent salt TDS content of the lower water is transported to the third high salt concentration system, and the monovalent salt TDS content of the higher concentrated water is transported to the second high salt concentration system; S2, after the second high salt concentration system treatment, the monovalent salt TDS content of the lower water is transported back to the first high salt concentration system, and the monovalent salt TDS content of the higher concentrated water is transported to the MVR evaporation crystallization system; S3, after the third high salt concentration system treatment, the monovalent salt TDS content of the lower water is transported to the seawater desalination reverse osmosis system, and the monovalent salt TDS content of the higher concentrated water is transported back to the second high salt concentration system; S4, after the seawater desalination reverse osmosis system treatment, the monovalent salt TDS content of the lower water reuse, and the monovalent salt TDS content of the higher concentrated water is transported back to the third high salt concentration system.

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