Main salt resource utilization device and method for chemical salinization wastewater

Abstract

The invention discloses a main salt resource utilization device and method for chemical salinization wastewater, and the device comprises a chemical salinization wastewater input end, a supercritical reactor, a supercritical cyclone separator, an inorganic filtering structure, a salt dissolving tank, an ionic membrane, an oxidant input end, a plunger pump, a heater and other structures. According to the super-strong removal capacity of supercritical water to organic components and the fact that inorganic salt is almost insoluble in the supercritical water, the chemical salinization wastewater can be subjected to supercritical water oxidation treatment, main salt is separated out while the contained organic components are removed in one step, and part of carnallite with low content is dissolved in the supercritical water to be taken out. The outflowing supercritical water is purified by an inorganic membrane after being subjected to desorption and pressure reduction, and the obtained pure water is used for dissolving the separated main salt and enters an ionic membrane process, so that the product is obtained. According to the method, organic components in the chemical salinization wastewater can be effectively removed, main salt components in the wastewater can be recycled, the process is simple, the cost is low, and harmless treatment and resource utilization of the chemical salinization wastewater can be achieved.

Description

Technical Field

[0001] The present invention belongs to the technical field of waste resource recycling, and particularly relates to a device and method for the resource utilization of main salts in chemical industrial saline wastewater. Background Art

[0002] In recent years, with the rapid development of the chemical industry, the generation amount of saline wastewater has gradually increased, becoming an important source of environmental pollution. Saline wastewater mainly comes from industrial processes such as salt chemical industry, petrochemical industry, and metallurgy, and its characteristics are high concentrations of salts, heavy metals, and organic pollutants. The advantages of resource utilization of saline wastewater are very significant. First, by recovering the salts in the wastewater, the pressure on the exploitation of natural salt mines can be effectively reduced, and sustainable utilization of resources can be achieved. Second, resource utilization helps to reduce the discharge amount of saline wastewater, thereby reducing environmental pollution and burden, which conforms to the concept of sustainable development. In addition, by using advanced separation and extraction technologies (such as membrane separation, evaporation crystallization, etc.), the salts in the wastewater can be efficiently recovered and converted into products such as industrial salts or chemical fertilizers, creating economic benefits. At the same time, this circular economy model can not only reduce the treatment cost, but also help enterprises improve their compliance and social responsibility in environmental protection. In the context of the current global resource shortage and increasing environmental protection pressure, actively promoting the resource utilization of chemical industrial saline wastewater is not only an effective way to solve the problem of wastewater treatment, but also an important measure to achieve industrial green transformation and sustainable development.

[0003] Although there are already some technologies for the treatment of saline wastewater, most of the existing methods still mainly focus on removing pollutants and fail to effectively recover and utilize the main salt components in the wastewater. Due to the constraints of technical and economic factors, the resource utilization of saline wastewater is still in the initial stage of development, resulting in a large amount of renewable resources being directly discharged, forming obvious resource waste, and there is an urgent need to find more efficient resource utilization ways. Summary of the Invention

[0004] The technical problem to be solved by the present invention is to provide a device and method for the resource utilization of main salts in chemical industrial saline wastewater in view of the above-mentioned deficiencies of the prior art.

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

[0006] The main salt resource utilization device for chemical industrial saline wastewater includes an input end of chemical industrial saline wastewater, a supercritical reactor, a supercritical cyclone separator, an inorganic filtration structure, a brine dissolving tank, and an ion membrane. The input end of chemical industrial saline wastewater is connected to the supercritical reactor, and the input end of chemical industrial saline wastewater inputs chemical industrial saline wastewater containing the main salt into the supercritical reactor. The supercritical reactor is connected to the supercritical cyclone separator, and the supercritical reactor inputs the chemical industrial saline wastewater after purifying the organic components into the supercritical cyclone separator. The supercritical cyclone separator is respectively connected to the inorganic filtration structure and the brine dissolving tank. The supercritical cyclone separator is used for swirling and separating the chemical industrial saline wastewater after purifying the organic components. The separated main salt is input into the brine dissolving tank, and the separated miscellaneous salt solution is input into the inorganic filtration structure. The inorganic filtration structure is connected to the brine dissolving tank, and the pure water after purifying the miscellaneous salt solution by the inorganic filtration structure is input into the brine dissolving tank. The brine dissolving tank is connected to the ion membrane, and the ion membrane selectively allows the main salt ions to pass through.

[0007] To optimize the above technical solution, the specific measures taken also include:

[0008] The main salt resource utilization device for chemical industrial saline wastewater further includes an oxidant input end. The oxidant input end is connected to the supercritical reactor, and the oxidant input end is used for inputting an oxidant into the supercritical reactor.

[0009] A plunger pump is installed on the connecting pipeline between the input end of chemical industrial saline wastewater and the supercritical reactor. The plunger pump is used for pumping the chemical industrial saline wastewater into the supercritical reactor.

[0010] A heater is installed on the connecting pipeline between the input end of chemical industrial saline wastewater and the supercritical reactor. The heater is used for heating the chemical industrial saline wastewater before it enters the supercritical reactor.

[0011] The inorganic filtration structure is an ultrafiltration membrane separator.

[0012] Sampling points are arranged on the connecting pipeline between the input end of chemical industrial saline wastewater and the supercritical reactor, on the connecting pipeline between the supercritical reactor and the supercritical cyclone separator, on the connecting pipeline between the supercritical cyclone separator and the inorganic filtration structure, on the connecting pipeline between the supercritical cyclone separator and the brine dissolving tank, and on the connecting pipeline between the inorganic filtration structure and the brine dissolving tank. The sampling points can take out the transmission substances in the corresponding connecting pipelines.

[0013] The oxidant is an oxygen-containing gas or hydrogen peroxide.

[0014] The main salt resource utilization method for chemical industrial saline wastewater uses the above-mentioned main salt resource utilization device for chemical industrial saline wastewater, and specifically includes the following steps:

[0015] Step 1: Input the chemical industrial salt wastewater into the supercritical reactor through the input end of the chemical industrial salt wastewater, a plunger pump, and a heater, and input the oxidant into the supercritical reactor through the input end of the oxidant, so that the supercritical state is reached in the supercritical reactor;

[0016] Step 2: The chemical industrial salt wastewater is oxidized under the supercritical state to remove the organic components in the chemical industrial salt wastewater. At the same time, the main salts and some of the miscellaneous salts in the chemical industrial salt wastewater precipitate, and the remaining miscellaneous salts are dissolved in the supercritical water, obtaining the chemical industrial salt wastewater after purifying the organic components;

[0017] Step 3: The chemical industrial salt wastewater after purifying the organic components is transported to the supercritical cyclone separator. The supercritical cyclone separator performs cyclone separation on the chemical industrial salt wastewater after purifying the organic components. The main salts are transported to the salt dissolving tank, and the supercritical water dissolved with miscellaneous salts is transported to the inorganic filtration structure after pressure reduction and temperature reduction;

[0018] Step 4: The inorganic filtration structure filters the water dissolved with miscellaneous salts to obtain deionized water;

[0019] Step 5: The deionized water is input into the salt dissolving tank to obtain the main salt ion water with a small amount of impurities;

[0020] Step 6: The main salt ion water with a small amount of impurities is filtered through an ion membrane to obtain the refined main salt ion water, and the refined main salt ion water is used for resource utilization.

[0021] The COD of the chemical industrial salt wastewater is 2000 - 400000 mg / L, and the salt concentration is 1000 - 300000 mg / L; the temperature in the supercritical reactor and the supercritical cyclone separator is 350 - 600 °C, and the pressure is 20 - 35 MPa; in Step 2, the COD of the chemical industrial salt wastewater after purifying the organic components is < 100 mg / L; in Step 3, the supercritical water dissolved with miscellaneous salts is transported to the inorganic filtration structure after being depressurized and cooled to normal pressure and normal temperature; in Step 3, the concentration of the miscellaneous salts in the supercritical water entering the inorganic filtration structure is < 200 mg / L.

[0022] In Step 5, the concentration of the main salt ion water is 800 - 300000 mg / L.

[0023] The beneficial effects of the present invention are:

[0024] According to the super-strong removal ability of supercritical water for organic components (almost 100%) and the fact that inorganic salts are almost insoluble in supercritical water, the chemical industrial salinization wastewater can be treated by supercritical water oxidation. While removing the organic components contained therein in one step, the main salt is precipitated and separated, and some low-content miscellaneous salts are dissolved in the supercritical water and carried out. The outflowing supercritical water is purified by an inorganic membrane after decompression by analysis, and the obtained pure water is used to dissolve the separated main salt and enter the ion membrane process, and then the product is obtained. The present invention can effectively recycle the main salt components in the wastewater, and the process is simple and the cost is low. Brief Description of the Drawings

[0025] Figure 1 is a schematic structural diagram of the present invention;

[0026] The reference numerals therein are: the input end 1 of the chemical industrial salinization wastewater, the supercritical reactor 2, the supercritical cyclone separator 3, the inorganic filtration structure 4, the salt dissolving tank 5, the ion membrane 6, the oxygen input end 7, the plunger pump 8, and the heater 9. Detailed Embodiments

[0027] In order to make the objectives, technical solutions and advantages of the present application clearer, the present application will be described and explained below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are only used to explain the present application and are not used to limit the present application. Based on the embodiments provided in the present application, all other embodiments obtained by those of ordinary skill in the art without making creative efforts belong to the scope of protection of the present application.

[0028] Obviously, the accompanying drawings in the following description are only some examples or embodiments of the present application. For those of ordinary skill in the art, without making creative efforts, the present application can also be applied to other similar scenarios based on these drawings. In addition, it can also be understood that although the efforts made in this development process may be complex and lengthy, for those of ordinary skill in the art related to the content disclosed in the present application, some design, manufacturing or production changes based on the technical content disclosed in the present application are only conventional technical means and should not be understood as the content disclosed in the present application being insufficient.

[0029] Referring to "embodiments" in the present application means that the specific features, structures or characteristics described in combination with the embodiments can be included in at least one embodiment of the present application. The phrase appears in various positions in the specification does not necessarily refer to the same embodiment, nor is it an independent or alternative embodiment mutually exclusive with other embodiments. Those of ordinary skill in the art explicitly and implicitly understand that the embodiments described in the present application can be combined with other embodiments without conflict.

[0030] Unless otherwise defined, the technical terms or scientific terms involved in this application shall have the ordinary meanings understood by those with ordinary skills in the technical field to which this application belongs. The words such as "a", "an", "one", "the" and the like involved in this application do not indicate a quantity limitation and may represent a singular or plural number. The terms "comprise", "include", "have" and any variations thereof involved in this application are intended to cover non-exclusive inclusion; for example, a process, method, system, product or device that includes a series of steps or units (units) is not limited to the listed steps or units, but may further include steps or units not listed, or may further include other steps or units inherent to these processes, methods, products or devices. The similar words such as "connected", "coupled" and "linked" involved in this application are not limited to physical or mechanical connections, but may include electrical connections, whether direct or indirect. The "multiple" / "several" involved in this application refers to two or more. "And / or" describes the association relationship of associated objects and indicates that three relationships may exist. For example, "A and / or B" may represent: A exists alone, A and B exist simultaneously, and B exists alone. The character " / " generally represents an "or" relationship between the front and rear associated objects. The terms "first", "second", "third" and the like involved in this application are only used to distinguish similar objects and do not represent a specific order of the objects.

[0031] The main salt resource utilization device for chemical industrial salinized wastewater of the present invention mainly comprises a chemical industrial salinized wastewater input end 1, a supercritical reactor 2, a supercritical cyclone separator 3, an inorganic filtration structure 4, a salt dissolving tank 5, an ion membrane 6, an oxidant input end 7, a plunger pump 8, and a heater 9.

[0032] As Figure 1 shown in the figure, in the figure: P is the plunger pump; T is the heater; R is the supercritical reactor; F is the supercritical cyclone separator; UF is the ultrafiltration membrane separator; V is the salt dissolving tank. ① to ⑤ are sampling points.

[0033] The plunger pump 8 and the heater 9 are both installed on the connecting pipeline between the chemical industrial salinized wastewater input end 1 and the supercritical reactor 2. The supercritical reactor 2, the supercritical cyclone separator 3, the inorganic filtration structure 4, the salt dissolving tank 5 and the ion membrane 6 are connected in sequence. Among them, the supercritical cyclone separator 3 is also connected to the salt dissolving tank 5 and can directly input salt precipitation crystals into the salt dissolving tank 5.

[0034] The main salt resource utilization method for chemical industrial salinized wastewater comprises the following steps:

[0035] Step 1: Input the chemical industrial salinized wastewater through the chemical industrial salinized wastewater input end 1, the plunger pump 8, and the heater 9 into the supercritical reactor 2, and input the oxidant through the oxidant input end 7 into the supercritical reactor 2 to make the inside of the supercritical reactor 2 reach the supercritical state;

[0036] Step 2: Supercritical water is used to oxidize the chemical industrial salinized wastewater to remove the organic components in the chemical industrial salinized wastewater. Meanwhile, the main salts and some miscellaneous salts in the chemical industrial salinized wastewater precipitate, and the remaining miscellaneous salts dissolve in the supercritical water, obtaining the chemical industrial salinized wastewater after purifying the organic components.

[0037] Step 3: The chemical industrial salinized wastewater after purifying the organic components is transported to the supercritical cyclone separator 3. The supercritical cyclone separator 3 performs cyclone separation on the chemical industrial salinized wastewater after purifying the organic components. The main salts are transported to the salt dissolving tank 5, and the supercritical water dissolved with miscellaneous salts is transported to the inorganic filtration structure 4 after pressure reduction and temperature reduction.

[0038] Step 4: The inorganic filtration structure 4 filters the water dissolved with miscellaneous salts to obtain deionized water.

[0039] Step 5: The deionized water is input into the salt dissolving tank 5 to obtain the main salt ion water with little impurity.

[0040] Step 6: The main salt ion water with little impurity is filtered through the ion membrane 6 to obtain the refined main salt ion water, and the refined main salt ion water is used for resource utilization.

[0041] The following is an explanation with specific cases:

[0042] Example 1:

[0043] A device and method for resource utilization of the main salts in coking wastewater specifically include: Coking wastewater (COD 10000mg / L, salt concentration 15000mg / L) is pressurized to 30MPa by a plunger pump and preheated to 400°C by a heater at the input end of the chemical industrial salinized wastewater and then input into the supercritical reactor. The oxidant (pure oxygen) is pressurized to 30MPa at the input end of the oxidant and input into the supercritical reactor. The coking wastewater is oxidized in the supercritical state to remove the organic components in the chemical industrial salinized wastewater. Meanwhile, the main salts and some miscellaneous salts in the chemical industrial salinized wastewater precipitate, and the remaining miscellaneous salts dissolve in the supercritical water, obtaining the chemical industrial salinized wastewater after purifying the organic components (COD reduced to 50mg / L); The chemical industrial salinized wastewater after purifying the organic components is transported to the supercritical cyclone separator. The supercritical cyclone separator performs cyclone separation on the chemical industrial salinized wastewater after purifying the organic components. The main salts are transported to the salt dissolving tank, and the supercritical water dissolved with miscellaneous salts (salt concentration 100mg / L) is transported to the inorganic filtration structure after pressure reduction and temperature reduction to normal temperature and pressure; The inorganic filtration structure filters the water dissolved with miscellaneous salts to obtain deionized water; The deionized water is input into the salt dissolving tank to obtain the main salt ion water with little impurity (salt concentration 14900mg / L); The main salt ion water with little impurity is filtered through the ion membrane to obtain the refined main salt ion water, and the refined main salt ion water is used for resource utilization.

[0044] Example 2:

[0045] An apparatus and method for resource utilization of the main salts in chemical industrial wastewater, specifically including: Chemical industrial wastewater (COD 2000 mg / L, salt concentration 1000 mg / L) is pressurized to 20 MPa by a plunger pump through the input end of the chemical industrial salt wastewater, preheated to 350 °C by a heater, and then input into a supercritical reactor. An oxidant (pure oxygen) is pressurized to 20 MPa through the input end of the oxidant and input into the supercritical reactor. The coking wastewater is oxidized under supercritical conditions to remove the organic components in the chemical industrial salt wastewater. At the same time, the main salts and some of the miscellaneous salts in the chemical industrial salt wastewater precipitate, and the remaining miscellaneous salts dissolve in the supercritical water, obtaining the chemical industrial salt wastewater after purifying the organic components (COD reduced to 10 mg / L); The chemical industrial salt wastewater after purifying the organic components is transported to a supercritical cyclone separator. The supercritical cyclone separator performs cyclone separation on the chemical industrial salt wastewater after purifying the organic components. The main salts are transported to a salt dissolving tank. The supercritical water containing dissolved miscellaneous salts (salt concentration 50 mg / L) is transported to an inorganic filtration structure after being depressurized and cooled to normal temperature and pressure; The inorganic filtration structure filters the water containing dissolved miscellaneous salts to obtain deionized water; The deionized water is input into the salt dissolving tank to obtain the main salt ion water with slightly miscellaneous salts (salt concentration 950 mg / L); The main salt ion water with slightly miscellaneous salts is filtered through an ion membrane to obtain the refined main salt ion water, and the refined main salt ion water is used for resource utilization.

[0046] Example 3:

[0047] An apparatus and method for resource utilization of the main salts in chemical industrial wastewater, specifically including: Chemical industrial wastewater (COD 400000 mg / L, salt concentration 300000 mg / L) is pressurized to 35 MPa by a plunger pump through the input end of the chemical industrial salt wastewater, preheated to 600 °C by a heater, and then input into a supercritical reactor. An oxidant (pure oxygen) is pressurized to 35 MPa through the input end of the oxidant and input into the supercritical reactor. The coking wastewater is oxidized under supercritical conditions to remove the organic components in the chemical industrial salt wastewater. At the same time, the main salts and some of the miscellaneous salts in the chemical industrial salt wastewater precipitate, and the remaining miscellaneous salts dissolve in the supercritical water, obtaining the chemical industrial salt wastewater after purifying the organic components (COD reduced to 100 mg / L); The chemical industrial salt wastewater after purifying the organic components is transported to a supercritical cyclone separator. The supercritical cyclone separator performs cyclone separation on the chemical industrial salt wastewater after purifying the organic components. The main salts are transported to a salt dissolving tank. The supercritical water containing dissolved miscellaneous salts (salt concentration 200 mg / L) is transported to an inorganic filtration structure after being depressurized and cooled to normal temperature and pressure; The inorganic filtration structure filters the water containing dissolved miscellaneous salts to obtain deionized water; The deionized water is input into the salt dissolving tank to obtain the main salt ion water with slightly miscellaneous salts (salt concentration 300000 mg / L); The main salt ion water with slightly miscellaneous salts is filtered through an ion membrane to obtain the refined main salt ion water, and the refined main salt ion water is used for resource utilization.

Claims

1. The main salt resource utilization device for chemical industrial saline wastewater, characterized in that: It includes an input end (1) of chemical industrial salinized wastewater, a supercritical reactor (2), a supercritical cyclone separator (3), an inorganic filtration structure (4), a brine dissolving tank (5) and an ion membrane (6). The input end (1) of chemical industrial salinized wastewater is connected to the supercritical reactor (2), and the input end (1) of chemical industrial salinized wastewater inputs chemical industrial salinized wastewater containing main salts into the supercritical reactor (2). The supercritical reactor (2) is connected to the supercritical cyclone separator (3), and the supercritical reactor (2) inputs the chemical industrial salinized wastewater after purifying the organic components into the supercritical cyclone separator (3). The supercritical cyclone separator (3) is respectively connected to the inorganic filtration structure (4) and the brine dissolving tank (5). The supercritical cyclone separator (3) is used for cyclone separation of the chemical industrial salinized wastewater after purifying the organic components. The separated main salts are input into the brine dissolving tank (5), and the separated miscellaneous salt solution is input into the inorganic filtration structure (4). The inorganic filtration structure (4) is connected to the brine dissolving tank (5), and the inorganic filtration structure (4) inputs the pure water after purifying the miscellaneous salt solution into the brine dissolving tank (5). The brine dissolving tank (5) is connected to the ion membrane (6), and the ion membrane (6) selectively allows the main salt ions to pass through.

2. The main salt resource utilization device for chemical industrial saline wastewater according to claim 1, wherein: It further includes an oxidant input end (7). The oxidant input end (7) is connected to the supercritical reactor (2), and the oxidant input end (7) is used for inputting an oxidant into the supercritical reactor (2).

3. The main salt resource utilization device for chemical industrial saline wastewater according to claim 1, wherein: A plunger pump (8) is installed on the connecting pipeline between the input end (1) of chemical industrial salinized wastewater and the supercritical reactor (2), and the plunger pump (8) is used for pumping the chemical industrial salinized wastewater into the supercritical reactor (2).

4. The main salt resource utilization device for chemical industrial saline wastewater according to claim 1, characterized in that: A heater (9) is installed on the connecting pipeline between the input end (1) of chemical industrial salinized wastewater and the supercritical reactor (2), and the heater (9) is used for heating the chemical industrial salinized wastewater before it enters the supercritical reactor (2).

5. The main salt resource utilization device for chemical industrial saline wastewater according to claim 1, characterized in that: The inorganic filtration structure (4) is a ultrafiltration membrane separator.

6. The main salt resource utilization device for chemical industrial saline wastewater according to claim 1, characterized in that: Sampling points are arranged on the connecting pipeline between the input end (1) of chemical industrial salinized wastewater and the supercritical reactor (2), on the connecting pipeline between the supercritical reactor (2) and the supercritical cyclone separator (3), on the connecting pipeline between the supercritical cyclone separator (3) and the inorganic filtration structure (4), on the connecting pipeline between the supercritical cyclone separator (3) and the brine dissolving tank (5), and on the connecting pipeline between the inorganic filtration structure (4) and the brine dissolving tank (5). The sampling points can take out the transported substances in the corresponding connecting pipelines.

7. The main salt resource utilization device for chemical industrial saline wastewater according to claim 2, characterized in that: The oxidant is an oxygen-containing gas or hydrogen peroxide.

8. A method for resource utilization of main salts in chemical industrial saline wastewater, characterized in that: Applying the main salt resource utilization device for chemical industrial salinized wastewater as claimed in claim 1, specifically includes the following steps: Step 1: Input the chemical industrial salinized wastewater through the input end (1) of chemical industrial salinized wastewater, the plunger pump (8) and the heater (9) into the supercritical reactor (2), and input the oxidant through the oxidant input end (7) into the supercritical reactor (2) to make the inside of the supercritical reactor (2) reach the supercritical state; Step 2: The chemical industrial saline wastewater is oxidized under supercritical conditions to remove the organic components in the chemical industrial saline wastewater. Meanwhile, the main salts and some of the miscellaneous salts in the chemical industrial saline wastewater precipitate, and the remaining miscellaneous salts dissolve in the supercritical water, obtaining the chemical industrial saline wastewater after purifying the organic components; Step 3: The chemical industrial saline wastewater after purifying the organic components is transported to the supercritical cyclone separator (3). The supercritical cyclone separator (3) performs cyclone separation on the chemical industrial saline wastewater after purifying the organic components. The main salts are transported to the salt dissolving tank (5), and the supercritical water containing dissolved miscellaneous salts is transported to the inorganic filtration structure (4) after pressure reduction and temperature reduction; Step 4: The inorganic filtration structure (4) filters the water containing dissolved miscellaneous salts to obtain deionized water; Step 5: The deionized water is input into the salt dissolving tank (5) to obtain the main salt ion water with a small amount of impurities; Step 6: The main salt ion water with a small amount of impurities is filtered through the ion membrane (6) to obtain the refined main salt ion water, and the refined main salt ion water is used for resource utilization.

9. The method for resource utilization of main salts in chemical industrial saline wastewater according to claim 8, characterized in that: The COD of the chemical industrial saline wastewater is 2000 - 400000 mg / L, and the salt concentration is 1000 - 300000 mg / L; the temperature in the supercritical reactor (2) and the supercritical cyclone separator (3) is 350 - 600 °C, and the pressure is 20 - 35 MPa; in Step 2, the COD of the chemical industrial saline wastewater after purifying the organic components is < 100 mg / L; in Step 3, the supercritical water containing dissolved miscellaneous salts is transported to the inorganic filtration structure (4) after being depressurized and cooled to normal pressure and normal temperature; in Step 3, the concentration of the miscellaneous salts in the supercritical water entering the inorganic filtration structure (4) is < 200 mg / L.

10. The method for resource utilization of main salts in chemical industrial saline wastewater according to claim 8, characterized in that: In Step 5, the concentration of the main salt ion water is 800 - 300000 mg / L.

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