CN115443185A - Product recovery method and device used in preparation and use processes of wastewater treatment agent - Google Patents

Product recovery method and device used in preparation and use processes of wastewater treatment agent Download PDF

Info

Publication number
CN115443185A
CN115443185A CN202080099993.6A CN202080099993A CN115443185A CN 115443185 A CN115443185 A CN 115443185A CN 202080099993 A CN202080099993 A CN 202080099993A CN 115443185 A CN115443185 A CN 115443185A
Authority
CN
China
Prior art keywords
reaction
treatment agent
wastewater treatment
product
wastewater
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
CN202080099993.6A
Other languages
Chinese (zh)
Inventor
姚鹤
丁宏铃
李建仓
曾能
唐丽梅
雍红团华
侯晓刚
杨耀华
张福晏
朱竑卫
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Lanzhou Lanshi Zhongke Nano Technology Co ltd
Original Assignee
Lanzhou Lanshi Zhongke Nano Technology Co ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Lanzhou Lanshi Zhongke Nano Technology Co ltd filed Critical Lanzhou Lanshi Zhongke Nano Technology Co ltd
Publication of CN115443185A publication Critical patent/CN115443185A/en
Pending legal-status Critical Current

Links

Images

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J20/00—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof
    • B01J20/02—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material
    • B01J20/04—Solid sorbent compositions or filter aid compositions; Sorbents for chromatography; Processes for preparing, regenerating or reactivating thereof comprising inorganic material comprising compounds of alkali metals, alkaline earth metals or magnesium
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/20—Heavy metals or heavy metal compounds

Abstract

The present application relates to a product recovery method and apparatus for use in the preparation and use of wastewater treatment agents. The method comprises the following steps: obtaining a wastewater treatment agent through a first reaction process; introducing a wastewater treatment agent into wastewater generated by preparing heavy metals, and obtaining a second reaction product through a second reaction process; processing the second reaction product through a third reaction process to obtain a third reaction product, wherein the third reaction product at least comprises a first part and a second part; performing a first recovery treatment on the first part to obtain a reactant for preparing a wastewater treatment agent; and carrying out second recovery treatment on the second part to obtain a reactant for preparing the heavy metal.

Description

Product recovery method and device used in preparation and use processes of wastewater treatment agent Technical Field
The application relates to the field of wastewater treatment, in particular to a product recovery method and a product recovery device used in the preparation and use processes of a wastewater treatment agent.
Background
With the social development, environmental protection is becoming more and more important, and accordingly, treatment of industrial wastewater, waste gas, and the like is becoming more and more important. For example, if the wastewater containing heavy metal ions is treated improperly, not only great threat is brought to the ecological environment, but also heavy metal resources are wasted. Accordingly, there is a need to provide a product recovery process for use in the preparation and use of wastewater treatment agents.
Disclosure of Invention
One embodiment of the present application provides a method for product recovery during the preparation and use of a wastewater treatment agent. The method comprises the following steps: obtaining a wastewater treatment agent through a first reaction process; introducing the wastewater treatment agent into wastewater generated by preparing heavy metals, and obtaining a second reaction product through a second reaction process, wherein the second reaction product at least comprises a product of the wastewater treatment agent after adsorption; processing the second reaction product through a third reaction process to obtain a third reaction product, wherein the third reaction product at least comprises a first part and a second part; performing a first recovery treatment on the first portion to obtain a reactant for preparing the wastewater treatment agent; and carrying out second recovery treatment on the second part to obtain a reactant for preparing the heavy metal.
In some embodiments, the obtaining of the wastewater treatment agent by the first reaction process comprises: respectively introducing the magnesium salt solution, the precipitator and the coating agent into a reaction device at a preset flow rate; carrying out the reaction under first reaction conditions; and obtaining a product salt solution and the wastewater treatment agent through a first separation process.
In some embodiments, the magnesium salt solution comprises a magnesium sulfate solution or a magnesium chloride solution.
In some embodiments, the precipitating agent comprises a sodium hydroxide solution, ammonia, calcium hydroxide solution.
In some embodiments, the capping agent comprises ammonium oleate, sodium oleate, ammonium stearate, sodium stearate, ammonium hydrodimer, sodium hydrodimer, ammonium dimer, sodium dimer, or potassium octadecyl phosphate.
In some embodiments, the predetermined flow rate is 200mL/min to 20L/min.
In some embodiments, the first reaction conditions include a first reaction temperature of 20 ℃ to 50 ℃.
In some embodiments, the product salt solution comprises a sodium sulfate solution; and, the method further comprises: and crystallizing the sodium sulfate solution to generate mirabilite.
In some embodiments, the introducing the wastewater treatment agent into wastewater generated in the preparation of heavy metals, and obtaining a second reaction product through a second reaction process comprises: the wastewater treatment agent adsorbs heavy metals in the wastewater under a second reaction condition; and carrying out a second separation process on the wastewater subjected to the adsorption action to obtain a product of the wastewater treatment agent subjected to the adsorption action.
In some embodiments, the second reaction conditions include a second reaction temperature of 20 ℃ to 50 ℃.
In some embodiments, the second reaction condition comprises a PH of 5 to 11.
In some embodiments, the wastewater generated by the production of heavy metals includes at least one of nickel, copper, cobalt, arsenic, cadmium, and lead.
In some embodiments, said treating said second reaction product by a third reaction process to obtain a third reaction product comprises: introducing carbon dioxide gas into a product of the wastewater treatment agent after adsorption, and performing desorption reaction under a third reaction condition to obtain a third reaction product; and performing a third separation process on the third reaction product to obtain the first portion and the second portion.
In some embodiments, the third reaction conditions comprise a pressure of 0.3MPa to 0.5MPa of the desorption reaction.
In some embodiments, the first portion comprises a magnesium bicarbonate solution; and the second portion comprises a heavy metal carbonate precipitate.
In some embodiments, said first recycling of said first portion comprises: heating the magnesium bicarbonate solution to obtain magnesium carbonate precipitate; calcining the magnesium carbonate precipitate to obtain a product carbon dioxide gas and a magnesium oxide solid, wherein the product carbon dioxide gas is recycled for a reactant in the third reaction process; and carrying out flue gas desulfurization reaction on the magnesium oxide solid to obtain a magnesium sulfate solution, wherein the magnesium sulfate solution is used for preparing a reactant of the wastewater treatment agent.
One embodiment of the present application provides an apparatus for product recovery during the preparation and use of a wastewater treatment agent. The device comprises: a first device for obtaining a wastewater treatment agent through a first reaction process; the second device is used for introducing the wastewater treatment agent into wastewater generated by preparing heavy metals and obtaining a second reaction product through a second reaction process, wherein the second reaction product at least comprises a product of the wastewater treatment agent after adsorption; a third device, configured to process the second reaction product through a third reaction process to obtain a third reaction product, where the third reaction product at least includes a first portion and a second portion; the first recovery device is used for carrying out first recovery treatment on the first part to obtain a reactant for preparing the wastewater treatment agent; and the second recovery device is used for carrying out second recovery treatment on the second part to obtain a reactant for preparing the heavy metal.
Drawings
The present application will be further explained by way of exemplary embodiments, which will be described in detail by way of the accompanying drawings. These embodiments are not intended to be limiting, and in these embodiments like numerals refer to like structures, wherein:
FIG. 1 is a flow diagram of an exemplary product recovery process for use in wastewater treatment agent preparation and use according to some embodiments of the present application;
FIG. 2 is a schematic illustration of an exemplary product recovery device for use in wastewater treatment agent preparation and use according to some embodiments of the present application; and
FIG. 3 is a schematic illustration of an exemplary product recovery process for use in wastewater treatment agent preparation and use according to some embodiments of the present application.
Detailed Description
In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings used in the description of the embodiments will be briefly described below. It is obvious that the drawings in the following description are only examples or embodiments of the application, from which the application can also be applied to other similar scenarios without inventive effort for a person skilled in the art. Unless otherwise apparent from the context, or otherwise indicated, like reference numbers in the figures refer to the same structure or operation.
It should be understood that "system", "apparatus", "unit" and/or "module" as used herein is a method for distinguishing different components, elements, parts, portions or assemblies at different levels. However, other words may be substituted by other expressions if they accomplish the same purpose.
As used in this application and the appended claims, the terms "a," "an," "the," and/or "the" are not intended to be inclusive in the singular, but rather are intended to be inclusive in the plural unless the context clearly dictates otherwise. In general, the terms "comprises" and "comprising" merely indicate that steps and elements are included which are explicitly identified, that the steps and elements do not form an exclusive list, and that a method or apparatus may include other steps or elements.
Flow charts are used herein to illustrate operations performed by systems according to embodiments of the present application. It should be understood that the preceding or following operations are not necessarily performed in the exact order in which they are performed. Rather, the various steps may be processed in reverse order or simultaneously. Meanwhile, other operations may be added to the processes, or a certain step or several steps of operations may be removed from the processes.
One aspect of the present application relates to a method and apparatus for product recovery during the preparation and use of wastewater treatment agents. The wastewater treatment agent can adsorb heavy metal ions in wastewater generated by preparing heavy metals to obtain a product of the wastewater treatment agent after adsorption and wastewater after adsorption. The content of heavy metal ions in the wastewater after adsorption is reduced, and the wastewater can reach the discharge standard, so that the wastewater can be directly discharged without causing harm to the ecological environment. The product of the wastewater treatment agent after adsorption can be treated and separated, and further recycled to obtain a reactant for preparing the wastewater treatment agent and a reactant for preparing heavy metal, so that the reactants are recycled, the environment is protected, and resources are saved.
FIG. 1 is an exemplary flow diagram of a product recovery process for use in wastewater treatment agent preparation and use according to some embodiments of the present application. In some embodiments, process 100 may be performed automatically by a control system. For example, the process 100 may be implemented by control instructions, and the control system controls the respective devices to perform the respective operations of the process 100 based on the control instructions. In some embodiments, process 100 may be performed semi-automatically. For example, one or more operations of process 100 may be performed manually by an operator. In some embodiments, one or more additional operations not described may be added and/or one or more operations discussed herein may be deleted upon completion of process 100. Additionally, the order of the operations shown in FIG. 1 is not intended to be limiting.
And 110, obtaining the wastewater treatment agent through a first reaction process. In some embodiments, the first reaction process may be carried out by a first apparatus.
In some embodiments, the wastewater treatment agent may be a nano-water treatment agent. For example, the wastewater treatment agent may be nano magnesium hydroxide. In some embodiments, the reactants to make the wastewater treatment agent may include a magnesium salt solution, a precipitant, and a capping agent. In some embodiments, the magnesium salt solution, the precipitant, and the coating agent may be introduced into the first reaction device at predetermined flow rates, and the first reaction device may perform a reaction under a first reaction condition, and then perform a first separation process to obtain a product salt solution and a wastewater treatment agent. In some embodiments, the first reaction device may be a bubble liquid membrane reactor, which includes at least a reaction cylinder and a stirring device. Further description of bubble liquid membrane reactors may be found in chinese application cn200610033823.X filed on 28.2.2006 and in international application PCT/CN2020/088001 filed on 30.4.2020, which are incorporated herein by reference in their entirety.
In some embodiments, the magnesium salt solution may include a magnesium sulfate solution, a magnesium chloride solution, a magnesium nitrate solution, and the like. In some embodiments, the concentration of the magnesium salt solution may be 0.5mol/L to 3mol/L. In some embodiments, the concentration of the magnesium salt solution may be 0.7mol/L to 2.8mol/L. In some embodiments, the concentration of the magnesium salt solution may be 0.9mol/L to 2.6mol/L. In some embodiments, the concentration of the magnesium salt solution may be 1.1mol/L to 2.4mol/L. In some embodiments, the concentration of the magnesium salt solution may be 1.3mol/L to 2.2mol/L. In some embodiments, the concentration of the magnesium salt solution may be 1.5mol/L to 2.0mol/L. In some embodiments, the concentration of the magnesium salt solution may be 1.7mol/L to 1.8mol/L.
In some embodiments, a precipitating agent may be used to precipitate the magnesium salt solution. In some embodiments, the precipitating agent may include a sodium hydroxide solution, ammonia, calcium hydroxide solution, or the like. In some embodiments, the precipitating agent may also include ammonia gas and the like. In some embodiments, the concentration of the precipitating agent may be determined based on the concentration of the magnesium salt solution and the flow rates of the magnesium salt solution and the precipitating agent into the first reaction apparatus such that the stoichiometric ratio of the magnesium salt and the precipitating agent participating in the reaction is 1: 2. For example, if the flow rates of the magnesium salt solution and the precipitant into the first reaction device are the same, the concentration of the magnesium sulfate solution may be 1.1mol/L to 2.4mol/L, and the concentration of the corresponding precipitant sodium hydroxide solution may be 2.2mol/L to 4.8mol/L, or the concentration of the magnesium chloride solution may be 1.1mol/L to 2.4mol/L, and the concentration of the corresponding precipitant sodium hydroxide solution may be 2.2mol/L to 4.8mol/L. For another example, if the flow rate of the magnesium salt solution and the precipitant into the first reaction device is 1: 2, the concentration of the magnesium chloride solution may be 1.1mol/L to 2.4mol/L, and the concentration of the corresponding precipitant sodium hydroxide solution may be 1.1mol/L to 2.4mol/L.
In some embodiments, gas may also be used in the preparation of the wastewater treatment agent to mix the reactants evenly and enhance the mass and heat transfer between the phases. The gas can separate the reactant into bubble liquid film, the bubble is the disperse phase, the liquid film is the continuous phase, and the nano reaction environment is formed. The magnesium salt solution and the precipitant can react in the liquid membrane to generate nano particles. In some embodiments, the gas may be an inert gas, such as nitrogen, helium, and the like.
In some embodiments, the capping agent may include fatty acids, polyunsaturated fatty acids, sulfonates, sulfates, phosphates, titanates, silicates, and the like bearing at least one hydroxyl group on the S, P, ti or Si central atom. In some embodiments, the capping agent may include ammonium oleate, sodium oleate, ammonium stearate, sodium stearate, ammonium hydrodimer, sodium hydrodimer, ammonium dimer, sodium dimer, potassium octadecyl phosphate, and the like. The non-polar part of the coating agent may extend into the interior of the bubble and the polar part may extend into the liquid film. The coating agent can be combined with the surface of the newly generated nano particles at the interface of the bubble and the liquid film to form a coating layer, so that nano capsule particles (namely nano wastewater treatment agents) are generated. In some embodiments, the concentration of the coating agent may be 0.005mol/L to 0.02mol/L. In some embodiments, the concentration of the coating agent may be 0.006mol/L to 0.019mol/L. In some embodiments, the concentration of the capping agent may be 0.007mol/L to 0.018mol/L. In some embodiments, the concentration of the coating agent may be 0.008mol/L to 0.017mol/L. In some embodiments, the concentration of the coating agent can be 0.009mol/L to 0.016mol/L. In some embodiments, the concentration of the coating agent may be 0.01mol/L to 0.015mol/L. In some embodiments, the concentration of the capping agent may be 0.011mol/L to 0.014mol/L. In some embodiments, the concentration of the capping agent may be 0.012mol/L to 0.013mol/L.
In some embodiments, the predetermined flow rates for separately introducing the magnesium salt solution, the precipitant, and the coating agent into the first reaction device may be 200mL/min to 20000mL/min. In some embodiments, the preset flow rate may be 210mL/min to 15000mL/min. In some embodiments, the preset flow rate may be 220mL/min to 10000mL/min. In some embodiments, the preset flow rate may be 230mL/min to 6000mL/min. In some embodiments, the preset flow rate may be 240mL/min to 2000mL/min. In some embodiments, the preset flow rate may be 250mL/min to 800mL/min. In some embodiments, the preset flow rate may be 260mL/min to 600mL/min. In some embodiments, the preset flow rate may be 270mL/min to 400mL/min. In some embodiments, the preset flow rate may be 280mL/min to 360mL/min. In some embodiments, the preset flow rate may be 290mL/min to 320mL/min. In some embodiments, the preset flow rate may be 300mL/min.
In some embodiments, the first reaction conditions may include a first reaction temperature. In some embodiments, the first reaction temperature may be from 20 ℃ to 50 ℃. In some embodiments, the first reaction temperature may be from 21 ℃ to 45 ℃. In some embodiments, the first reaction temperature may be from 22 ℃ to 40 ℃. In some embodiments, the first reaction temperature may be 23 ℃ to 35 ℃. In some embodiments, the first reaction temperature may be from 24 ℃ to 30 ℃. In some embodiments, the first reaction temperature may be from 25 ℃ to 28 ℃. In some embodiments, the first reaction temperature may be between 26 ℃ and 27 ℃.
In some embodiments, the first reaction conditions may include a stirring speed of the bubble liquid membrane reactor. In some embodiments, the stirring speed may be 1000r/min to 6000r/m. In some embodiments, the stirring speed may be from 1500r/min to 5500r/m. In some embodiments, the stirring speed may be 2000r/min to 5000r/m. In some embodiments, the stirring speed may be from 2500r/min to 4500r/m. In some embodiments, the stirring speed may be 3000r/min to 4000r/m. In some embodiments, the stirring speed may be 3200r/min to 3800r/m. In some embodiments, the stirring speed may be 3400r/min to 3600r/m. In some embodiments, the stirring speed may be 3500r/m.
In some embodiments, the reaction product after the reaction under the first reaction conditions may be a foamed reaction product. The first separation process may include filtering, washing, drying, etc., the reaction product (e.g., a foamy reaction product). In some embodiments, the first separation process may be achieved by a first separation device. In some embodiments, the reaction product may be subjected to a first separation process to obtain a product salt solution and a wastewater treatment agent.
In some embodiments, the product salt solution may include a sodium sulfate solution, a sodium chloride solution, a sodium nitrate solution, an ammonium sulfate solution, an ammonium chloride solution, an ammonium nitrate solution, a calcium sulfate solution, a calcium chloride solution, a calcium nitrate solution, and the like. In some embodiments, if the product salt solution is a sodium sulfate solution, the sodium sulfate solution may also be subjected to a crystallization process to form mirabilite (sodium sulfate decahydrate). In some embodiments, the crystallization temperature of the crystallization process may be from-4 ℃ to-10 ℃. In some embodiments, the crystallization temperature of the crystallization process may be from-4.2 ℃ to-9.5 ℃. In some embodiments, the crystallization temperature of the crystallization process may be from-4.4 ℃ to-9 ℃. In some embodiments, the crystallization temperature of the crystallization process may be from-4.6 ℃ to-8.5 ℃. In some embodiments, the crystallization temperature of the crystallization process may be from-4.8 ℃ to-8 ℃. In some embodiments, the crystallization temperature of the crystallization process may be from-5 ℃ to-7.5 ℃. In some embodiments, the crystallization temperature of the crystallization process may be from-5.2 ℃ to-7 ℃. In some embodiments, the crystallization temperature of the crystallization process may be from-5.4 ℃ to-6.8 ℃. In some embodiments, the crystallization temperature of the crystallization process may be from-5.6 ℃ to-6.6 ℃. In some embodiments, the crystallization temperature of the crystallization process may be from-5.8 ℃ to-6.4 ℃. In some embodiments, the crystallization temperature of the crystallization process may be from-6 ℃ to-6.2 ℃.
And step 120, introducing the wastewater treatment agent into wastewater generated by preparing heavy metals, and obtaining a second reaction product through a second reaction process. In some embodiments, the second reaction process may be carried out by a second apparatus.
In some embodiments, the wastewater generated from the production of heavy metals may be generated by a heavy metal smelting plant (or heavy metal smelting line). In some embodiments, the wastewater from the production of heavy metals may include at least one of nickel, copper, cobalt, arsenic, cadmium, and lead. In some embodiments, the nickel content may be 20mg/L to 40mg/L. In some embodiments, the copper content may be 3mg/L to 6mg/L. In some embodiments, the cobalt content may be 0.2mg/L to 1.0mg/L. In some embodiments, the arsenic content may be 2mg/L to 6mg/L. In some embodiments, the cadmium can be present in an amount of 0.02mg/L to 0.06mg/L. In some embodiments, the lead content may be 1mg/L to 3mg/L.
In some embodiments, the wastewater treatment agent may adsorb heavy metals in the wastewater under the second reaction condition; and then, carrying out a second separation process on the wastewater subjected to the adsorption action to obtain a product of the wastewater treatment agent subjected to the adsorption action. In some embodiments, the adsorption process may be accomplished by a second reaction device. In some embodiments, the second reaction device may be an adsorption reactor. In some embodiments, the wastewater treatment agent and the wastewater may be metered into the second reaction device according to the saturated adsorption capacity of the wastewater treatment agent for various types of heavy metal ions. For example, the saturated adsorption capacity of the nano magnesium hydroxide wastewater treatment agent on heavy metal ions in wastewater is as follows: 74.07mg/g, i.e., 1g of nano magnesium hydroxide wastewater treatment agent can adsorb 74.07mg of heavy metal ions.
In some embodiments, the second reaction conditions may include a second reaction temperature. In some embodiments, the second reaction temperature may be 20 ℃ to 50 ℃. In some embodiments, the second reaction temperature may be from 21 ℃ to 45 ℃. In some embodiments, the second reaction temperature may be 22 ℃ to 40 ℃. In some embodiments, the second reaction temperature may be 23 ℃ to 35 ℃. In some embodiments, the second reaction temperature may be from 24 ℃ to 30 ℃. In some embodiments, the second reaction temperature may be from 25 ℃ to 28 ℃. In some embodiments, the second reaction temperature may be between 26 ℃ and 27 ℃.
In some embodiments, the second reaction conditions may include a pH. In some embodiments, the pH may be 5 to 11. In some embodiments, the pH may be 5.5 to 10.5. In some embodiments, the pH may be 6 to 10. In some embodiments, the pH may be 6.5 to 9.5. In some embodiments, the pH may be 7 to 9. In some embodiments, the pH may be 7.5 to 8.5. In some embodiments, the pH may be 8.
In some embodiments, the second reaction conditions may further include a stirring time. The stirring time can affect the adsorption speed of the wastewater treatment agent on the heavy metal ions in the wastewater. In some embodiments, the stirring time may be 10min to 60min. In some embodiments, the stirring time may be 15min to 55min. In some embodiments, the stirring time may be 20min to 50min. In some embodiments, the stirring time may be 25min to 45min. In some embodiments, the stirring time may be 30min to 40min. In some embodiments, the stirring time may be 32min to 38min. In some embodiments, the stirring time may be 34min to 36min. In some embodiments, the stirring time may be 35min.
In some embodiments, the second separation process may include filtering the wastewater after adsorption (including the products of the wastewater treatment agent after adsorption, i.e., the solid matter having heavy metal ions adsorbed thereon). After filtration, a second reaction product can be obtained. The second reaction product at least comprises a product of the wastewater treatment agent after adsorption. In some embodiments, the second separation process may be achieved by a second separation device. In some embodiments, after filtering the second reaction product, the contents of heavy metal ions in the wastewater after adsorption are: 1.0mg/L of total nickel, 1.0mg/L of total cobalt, 0.5mg/L of total copper, 0.1mg/L of total cadmium and 0.5mg/L of total arsenic. Therefore, after the wastewater generated by preparing heavy metal is adsorbed by the wastewater treating agent, the obtained wastewater subjected to adsorption can reach the discharge standard, and therefore, the wastewater can be directly discharged.
And step 130, processing the second reaction product through a third reaction process to obtain a third reaction product. In some embodiments, the third reaction process may be carried out by a third apparatus.
In some embodiments, carbon dioxide gas may be introduced into the second reaction product to perform the desorption reaction under the third reaction condition to obtain the third reaction product. The third reaction product can include at least a first portion and a second portion. Further, a third separation process may be performed on the third reaction product to yield a first portion and a second portion. In some embodiments, the desorption reaction may be achieved by a third reaction device. In some embodiments, the third reaction device may be a desorption reactor. Specifically, the second reaction product (i.e., the product of the wastewater treatment agent after adsorption) may be mixed with soft water and stirred to disperse the second reaction product (the product of the wastewater treatment agent after adsorption). And further, the dispersed second reaction product is introduced into a desorption reactor through a slurry pump to carry out desorption reaction.
In some embodiments, the third reaction conditions may include the pressure of the desorption reaction, i.e., the pressure of the gas in the third reaction apparatus in which the third reaction product is located. In some embodiments, the pressure of the desorption reaction may comprise 0.3MPa to 0.5MPa. In some embodiments, the pressure of the desorption reaction may comprise 0.31MPa to 0.49MPa. In some embodiments, the pressure of the desorption reaction may comprise 0.32MPa to 0.48MPa. In some embodiments, the pressure of the desorption reaction may comprise 0.33MPa to 0.47MPa. In some embodiments, the pressure of the desorption reaction may comprise 0.34MPa to 0.46MPa. In some embodiments, the pressure of the desorption reaction may comprise 0.35MPa to 0.45MPa. In some embodiments, the pressure of the desorption reaction may comprise 0.36MPa to 0.44MPa. In some embodiments, the pressure of the desorption reaction may comprise 0.37MPa to 0.43MPa. In some embodiments, the pressure of the desorption reaction may comprise 0.38MPa to 0.42MPa. In some embodiments, the pressure of the desorption reaction may comprise 0.39MPa to 0.41MPa. In some embodiments, the pressure of the desorption reaction may comprise 0.4 MPa.
In some embodiments, the third reaction conditions may include a pressure hold time for the desorption reaction. In some embodiments, the pressure maintenance time may comprise 1h to 6h. In some embodiments, the pressure maintenance time may comprise 1.5 hours to 5.5 hours. In some embodiments, the pressure maintenance time may comprise 2h to 5h. In some embodiments, the pressure maintenance time may comprise 2.5h to 4.5h. In some embodiments, the pressure maintenance time may comprise 2.7 hours to 4.3 hours. In some embodiments, the pressure maintenance time may comprise 2.9 hours to 4.1 hours. In some embodiments, the pressure maintenance time may comprise 3.1h to 3.9h. In some embodiments, the pressure maintenance time may comprise 3.3 hours to 3.7 hours. In some embodiments, the pressure maintenance time may comprise 3.4 hours to 3.6 hours. In some embodiments, the pressure maintenance time may comprise 3.5 hours.
In some embodiments, the third reaction conditions may include a temperature of the desorption reaction. In some embodiments, the temperature of the desorption reaction may comprise 20 ℃ to 50 ℃. In some embodiments, the temperature of the desorption reaction may comprise 22 ℃ to 48 ℃. In some embodiments, the temperature of the desorption reaction may comprise from 24 ℃ to 46 ℃. In some embodiments, the temperature of the desorption reaction may comprise 26 ℃ to 44 ℃. In some embodiments, the temperature of the desorption reaction may comprise from 28 ℃ to 42 ℃. In some embodiments, the temperature of the desorption reaction may comprise 30 ℃ to 40 ℃. In some embodiments, the temperature of the desorption reaction may comprise 31 ℃ to 39 ℃. In some embodiments, the temperature of the desorption reaction may comprise 32 ℃ to 38 ℃. In some embodiments, the temperature of the desorption reaction may comprise 33 ℃ to 37 ℃. In some embodiments, the temperature of the desorption reaction may comprise 34 ℃ to 36 ℃. In some embodiments, the temperature of the desorption reaction may comprise 35 ℃.
In some embodiments, the first portion of the third reaction product may comprise a magnesium bicarbonate solution and the second portion may comprise a heavy metal carbonate precipitate.
In some embodiments, the third separation process may include filtration. The third reaction product is subjected to a filtration operation, thereby obtaining the first and second fractions described above. In some embodiments, the third separation process may be achieved by a third separation device.
Step 140, a first recovery treatment is performed on the first portion to obtain a reactant for preparing the wastewater treatment agent. In some embodiments, the first recycling process may be implemented by the first recycling apparatus.
In some embodiments, the first portion may comprise a magnesium bicarbonate solution, as described in step 130. Correspondingly, the magnesium bicarbonate solution can be heated to obtain basic magnesium carbonate precipitate. In some embodiments, the heating temperature may be 50 ℃ to 80 ℃. The magnesium carbonate precipitate may then be calcined to yield the product carbon dioxide gas and magnesium oxide solids, wherein the product carbon dioxide gas is recycled for use as a reactant in the third reaction process described above. In some embodiments, the temperature of the calcination process may be 600 ℃ to 700 ℃. Further, the magnesium oxide solid can be subjected to flue gas desulfurization reaction to obtain a magnesium sulfate solution. Specifically, the magnesium oxide solids can be mixed with water to form a magnesium oxide slurry, and then the flue gas (which can include at least one of sulfur dioxide and sulfur trioxide, for example) can be brought into counter-current flow contact with the magnesium oxide slurry to effect a sufficient reaction thereof to produce a magnesium sulfite solution. In some embodiments, the flue gas may be conducted multiple times (e.g., two) with the magnesium oxide slurrySecondary and tertiary) reverse flow contact, so that sulfur dioxide and/or sulfur trioxide gas in the flue gas is fully absorbed, the treated flue gas reaches the emission standard, and the treated flue gas can be directly discharged. For example, if the content of particulate matter in the treated flue gas is 19mg/m 3 The content of sulfur dioxide is 48mg/m 3 The content of nitrogen oxides is 190mg/m 3 The blackness of the smoke is 1mg/m 3 The flue gas can be directly discharged. Still further, the magnesium sulfite solution can be subjected to an oxidation reaction (e.g., with oxygen or air) to produce a magnesium sulfate solution. The magnesium sulfate solution may be used as a reactant (i.e., magnesium salt solution) for the preparation of wastewater treatment agents. In some embodiments, in order to ensure the purity of the magnesium sulfate solution, the magnesium sulfate solution after the oxidation reaction can be subjected to solid-liquid separation, and the clear liquid obtained after filtration can be used for preparing a reactant of the wastewater treatment agent.
And 150, carrying out second recovery treatment on the second part to obtain a reactant for preparing the heavy metal. In some embodiments, the second recycling process may be accomplished by a second recycling device.
In some embodiments, the second portion may include heavy metal carbonate precipitation, as described in step 130. Correspondingly, the heavy metal carbonate precipitate can be recycled and smelted, and the recycling of the heavy metal is completed.
It should be noted that the above embodiments are only used for illustrating the technical solutions of the present invention and not for limiting the technical solutions, and those skilled in the art should understand that the technical solutions of the present invention are modified or replaced with equivalent solutions without departing from the spirit and scope of the technical solutions, and all should be covered in the claims of the present invention.
FIG. 2 is a schematic illustration of an exemplary product recovery unit for use in wastewater treatment agent preparation and use according to some embodiments of the present application.
As shown in fig. 2, the product recovery apparatus used in the preparation and use of the wastewater treatment agent may include a first apparatus, a second apparatus, a third apparatus, a first recovery apparatus, and a second recovery apparatus.
The first device may be used to obtain the wastewater treatment agent through a first reaction process. In some embodiments, the first means may comprise at least a first reaction means (e.g., a bubble-liquid membrane reactor) and a first separation means (e.g., a filter). In some embodiments, the magnesium salt solution, the precipitant, and the coating agent may be introduced (e.g., fed through a metering pump) into the first reaction device at predetermined flow rates, and reacted under the first reaction condition, followed by the first separation process to obtain the product salt solution and the wastewater treatment agent. Specifically, while introducing the reactant, inert gas is introduced into the first reaction device, the gas is dispersed into a bubble flow of a polygonal polyhedron, the reactant is divided into liquid films by the bubbles, the bubbles are dispersed phases, the liquid films are continuous phases, a nano reaction environment is formed, and the reactant reacts in the liquid films to generate nano capsule particles (namely, the nano wastewater treatment agent). Then the product salt solution and the wastewater treatment agent are obtained through a first separation device. More description of the first reaction process can be found elsewhere in this application, such as in FIG. 1 and its description.
The second device can be used for introducing the wastewater treatment agent into wastewater generated by preparing heavy metals, and obtaining a second reaction product through a second reaction process, wherein the second reaction product at least comprises a product of the wastewater treatment agent after adsorption. In some embodiments, the second device may include at least a second reaction device (e.g., an adsorption reactor) and a second separation device (e.g., a filter). In some embodiments, a wastewater treatment agent (e.g., nano magnesium hydroxide) may be introduced into wastewater generated by heavy metal smelting, and the wastewater treatment agent adsorbs heavy metal ions such as nickel, copper, cobalt, arsenic, cadmium, lead, etc. in the wastewater, and then the wastewater after adsorption (including the product of the wastewater treatment agent after adsorption) is subjected to a second separation process by using a second separation device, so as to obtain a product of the wastewater treatment agent after adsorption. More description of the second reaction process can be found elsewhere in this application, such as in FIG. 1 and its description.
The third device may be configured to process the second reaction product via a third reaction process to obtain a third reaction product, wherein the third reaction product includes at least a first portion and a second portion. In some embodiments, the third device may include at least a third reaction device (e.g., a desorption reactor) and a third separation device (e.g., a filter). Specifically, carbon dioxide gas may be introduced into the product of the wastewater treatment agent (e.g., nano magnesium hydroxide) after adsorption, and a desorption reaction may be performed under a third reaction condition to obtain a third reaction product (including the first portion and the second portion, e.g., a magnesium bicarbonate solution and a heavy metal carbonate precipitate). Further, the third reaction product is subjected to a third separation process by a third separation device to obtain a first portion and a second portion. Further description of the third reaction process can be found elsewhere in this application, for example, in FIG. 1 and its description.
The first recovery device may be configured to perform a first recovery treatment on the first portion to obtain a reactant for preparing the wastewater treatment agent. In some embodiments, the first portion may comprise a magnesium bicarbonate solution. Accordingly, the first recycling device may include at least a first heating device (e.g., a furnace), a calcining device (e.g., a calciner), and a flue gas desulfurization device. Specifically, the magnesium bicarbonate solution can be heated by the first heating device to obtain basic magnesium carbonate precipitate. And calcining the basic magnesium carbonate precipitate by using a calcining device to obtain a product carbon dioxide gas and a magnesium oxide solid, wherein the product carbon dioxide gas can be recycled for a reactant in a third reaction process. Furthermore, a flue gas desulfurization reaction can be carried out on the magnesium oxide solid through a flue gas desulfurization device to obtain a magnesium sulfate solution, and the magnesium sulfate solution is used for preparing a reactant of the wastewater treatment agent.
The second recovery device may be configured to perform a second recovery treatment on the second portion to obtain a reactant for producing a heavy metal. In some embodiments, the second portion may comprise a heavy metal carbonate precipitate. Correspondingly, the second recovery device can comprise a smelting recovery device for recovering and smelting the heavy metal carbonate precipitate to complete the recovery and utilization of the heavy metal.
It should be noted that the above embodiments are only used for illustrating the technical solutions of the present invention and not for limiting the technical solutions, and those skilled in the art should understand that the technical solutions of the present invention are modified or replaced with equivalent solutions without departing from the spirit and scope of the technical solutions, and all should be covered in the claims of the present invention.
FIG. 3 is a schematic illustration of an exemplary product recovery process for use in wastewater treatment agent preparation and use according to some embodiments of the present application. For convenience, the nano magnesium hydroxide wastewater treatment agent prepared by magnesium sulfate salt solution, sodium hydroxide solution and sodium oleate solution is described as an example below, and is not intended to limit the scope of the present application.
Step 1: adding a magnesium sulfate solution with the concentration of 1mol/L, a sodium hydroxide solution with the concentration of 2mol/L and a sodium oleate aqueous solution with the concentration of 0.01mol/L into a bubble liquid membrane reactor R301 at the temperature of 20-50 ℃ by using a metering pump at the flow rate of 300mL/min respectively, and introducing inert gas. The gas divides each reactant into a bubble liquid film, and the magnesium sulfate solution and the sodium hydroxide solution continuously react in the bubble liquid film to generate the nano magnesium hydroxide. Then, after being filtered by the first filtering device F301, 17.4g (i.e., 17.4 g/min) of the nano magnesium hydroxide wastewater treatment agent and 900mL (i.e., 900 mL/min) of a sodium sulfate solution (wherein the yield of sodium sulfate is 42.6 g/min) are obtained every minute. The sodium sulfate solution can also be introduced into a crystallizing device R304 for low-temperature crystallization to obtain mirabilite.
Step 2: 2L of heavy metal wastewater is introduced into the adsorption reactor R302, and the contents of heavy metals in the heavy metal wastewater are respectively as follows: ni of 100mg/L, co of 0mg/L, cu of 50mg/L. Adding 5.4g of nano magnesium hydroxide wastewater treatment agent into an adsorption reactor R302, controlling the pH value of liquid in the adsorption reactor R302 to be 5-11 at the temperature of 20-50 ℃, and stirring for 10-60 min to complete the adsorption of heavy metal ions in heavy metal wastewater. Then, after filtering by a second filtering device F302, 5.8g of the nano magnesium hydroxide wastewater treating agent (i.e. the product of the wastewater treating agent after adsorption) which adsorbs heavy metals and 2L of wastewater after adsorption are obtained. The content of heavy metals in the wastewater after adsorption is respectively as follows: ni is 0.01mg/L, co and 0.01mg/L, cu and 0.01mg/L, so that the standard of direct discharge is met, and the direct discharge can be realized.
And step 3: 5.8g of the nano magnesium hydroxide wastewater treatment agent absorbing heavy metals is mixed with 0.2L of soft water, the mixture is stirred for 10 to 60 minutes to completely disperse the solid, and then the mixture is pumped into a desorption reactor R303 by a slurry pump. Introducing CO 2 Keeping the pressure in the desorption reactor R303 at 0.3 MPa-0.5 MPa for 1-6 h, and carrying out pressure desorption reaction at 20-50 ℃. Then, after filtration by a third filtration device F303, 0.2L of a magnesium bicarbonate solution (wherein the content of magnesium bicarbonate is 13.59 g) and 0.798g of a heavy metal carbonate precipitate were obtained.
And 4, step 4: 0.798g of the heavy metal carbonate precipitate is smelted and recovered by a smelting and recovering device R305.
And 5: heating the magnesium bicarbonate solution to obtain 6-10 g of basic magnesium carbonate precipitate. Calcining 6-10 g of basic magnesium carbonate precipitate by a calciner T301 at the temperature of 600-700 ℃ to obtain a product of carbon dioxide gas and 3.75g of magnesium oxide solid. This product carbon dioxide gas may be stored in the collection tank F304 and may be used as the desorption gas in the desorption reactor R303.
Step 6: mixing 3.75g of magnesium oxide solid soft water to form magnesium oxide slurry, introducing the magnesium oxide slurry and the flue gas into a flue gas desulfurization device T302, and enabling the flue gas to be in reverse flow contact with the magnesium oxide slurry for multiple times, so that sulfur dioxide and/or sulfur trioxide gas in the flue gas is fully absorbed, and a magnesium sulfite solution is generated. The contents of sulfur dioxide and sulfur trioxide in the treated flue gas reach the emission standard and can be directly emitted. The magnesium sulfite solution reacts with oxygen or air to form a magnesium sulfate solution, and the magnesium sulfate solution can be used as a reactant magnesium sulfate solution for preparing the nano magnesium hydroxide wastewater treatment agent.
The beneficial effects that may be brought by the embodiments of the present application include, but are not limited to: (1) The waste water treatment agent can be prepared and used for adsorbing heavy metal ions in waste water generated by preparing heavy metals so as to enable the heavy metal ions to reach the emission standard and protect the environment; (2) The product of the wastewater treatment agent after adsorption can be recycled to obtain a reactant for preparing the wastewater treatment agent, so that part of the product of the wastewater treatment agent can be recycled, and resources are saved; (3) The product of the wastewater treatment agent after adsorption can be recycled to obtain the reactant for preparing heavy metal, so that heavy metal ions in the wastewater can be recycled, the environment is protected, and resources are saved.
It is to be noted that different embodiments may produce different advantages, and in different embodiments, any one or combination of the above advantages may be produced, or any other advantages may be obtained.
Having thus described the basic concept, it will be apparent to those skilled in the art that the foregoing detailed disclosure is to be considered merely illustrative and not restrictive of the broad application. Various modifications, improvements and adaptations to the present application may occur to those skilled in the art, although not explicitly described herein. Such modifications, improvements and adaptations are proposed in the present application and thus fall within the spirit and scope of the exemplary embodiments of the present application.
Also, this application uses specific language to describe embodiments of the application. Reference throughout this specification to "one embodiment," "an embodiment," and/or "some embodiments" means that a particular feature, structure, or characteristic described in connection with at least one embodiment of the present application is included in at least one embodiment of the present application. Therefore, it is emphasized and should be appreciated that two or more references to "an embodiment" or "one embodiment" or "an alternative embodiment" in various places throughout this specification are not necessarily all referring to the same embodiment. Furthermore, some features, structures, or characteristics of one or more embodiments of the present application may be combined as appropriate.
Additionally, the order in which elements and sequences of the processes described herein are processed, the use of alphanumeric characters, or the use of other designations, is not intended to limit the order of the processes and methods described herein, unless explicitly claimed. While various presently contemplated embodiments of the invention have been discussed in the foregoing disclosure by way of example, it is to be understood that such detail is solely for that purpose and that the appended claims are not limited to the disclosed embodiments, but, on the contrary, are intended to cover all modifications and equivalent arrangements that are within the spirit and scope of the embodiments herein. For example, although the system components described above may be implemented by hardware devices, they may also be implemented by software-only solutions, such as installing the described system on an existing server or mobile device.
Similarly, it should be noted that in the preceding description of embodiments of the application, various features are sometimes grouped together in a single embodiment, figure, or description thereof for the purpose of streamlining the disclosure aiding in the understanding of one or more of the embodiments. This method of disclosure, however, is not intended to require more features than are expressly recited in the claims. Indeed, the embodiments may be characterized as having less than all of the features of a single embodiment disclosed above.
Numerals describing the number of components, attributes, etc. are used in some embodiments, it being understood that such numerals used in the description of the embodiments are modified in some instances by the use of the modifier "about", "approximately" or "substantially". Unless otherwise indicated, "about", "approximately" or "substantially" indicates that the number allows a variation of ± 20%. Accordingly, in some embodiments, the numerical parameters used in the specification and claims are approximations that may vary depending upon the desired properties of the individual embodiments. In some embodiments, the numerical parameter should take into account the specified significant digits and employ a general digit preserving approach. Notwithstanding that the numerical ranges and parameters setting forth the broad scope of the range are approximations, in the specific examples, such numerical values are set forth as precisely as possible within the scope of the application.
The entire contents of each patent, patent application publication, and other material cited in this application, such as articles, books, specifications, publications, documents, and the like, are hereby incorporated by reference into this application. Except where the application is filed in a manner inconsistent or contrary to the present disclosure, and except where the claim is filed in its broadest scope (whether present or later appended to the application) as well. It is noted that the descriptions, definitions and/or use of terms in this application shall control if they are inconsistent or contrary to the statements and/or uses of the present application in the material attached to this application.
Finally, it should be understood that the embodiments described herein are merely illustrative of the principles of the embodiments of the present application. Other variations are also possible within the scope of the present application. Thus, by way of example, and not limitation, alternative configurations of the embodiments of the present application can be viewed as being consistent with the teachings of the present application. Accordingly, the embodiments of the present application are not limited to only those embodiments explicitly described and depicted herein.

Claims (17)

  1. A method for product recovery during the manufacture and use of a wastewater treatment agent, the method comprising:
    obtaining a wastewater treatment agent through a first reaction process;
    introducing the wastewater treatment agent into wastewater generated by preparing heavy metals, and obtaining a second reaction product through a second reaction process, wherein the second reaction product at least comprises a product of the wastewater treatment agent after adsorption;
    processing the second reaction product through a third reaction process to obtain a third reaction product, wherein the third reaction product at least comprises a first part and a second part;
    performing a first recovery treatment on the first portion to obtain a reactant for preparing the wastewater treatment agent; and
    and carrying out second recovery treatment on the second part to obtain a reactant for preparing the heavy metal.
  2. The method of claim 1, wherein the obtaining of the wastewater treatment agent through the first reaction process comprises:
    respectively introducing the magnesium salt solution, the precipitator and the coating agent into a reaction device at a preset flow rate;
    carrying out the reaction under first reaction conditions; and
    and obtaining a product salt solution and the wastewater treatment agent through a first separation process.
  3. The method of claim 2, wherein the magnesium salt solution comprises a magnesium sulfate solution or a magnesium chloride solution.
  4. A process according to claim 2 or 3, wherein the precipitating agent comprises a sodium hydroxide solution, ammonia, calcium hydroxide solution.
  5. The method of any of claims 2-4, wherein the capping agent comprises ammonium oleate, sodium oleate, ammonium stearate, sodium stearate, ammonium hydrodimer, sodium hydrodimer, ammonium dimer, sodium dimer, or potassium octadecyl phosphate.
  6. The method of any one of claims 2 to 5, wherein the preset flow rate is from 200 to 20L/min.
  7. The process of any one of claims 2 to 6, wherein the first reaction conditions comprise a first reaction temperature of from 20 ℃ to 50 ℃.
  8. The method of any one of claims 2-7, wherein the product salt solution comprises a sodium sulfate solution; and, the method further comprises:
    and crystallizing the sodium sulfate solution to generate mirabilite.
  9. The method of any one of claims 1 to 8, wherein the introducing the wastewater treatment agent into wastewater generated in the production of heavy metals to obtain a second reaction product through a second reaction process comprises:
    the wastewater treatment agent adsorbs heavy metals in the wastewater under a second reaction condition; and
    and carrying out a second separation process on the wastewater subjected to the adsorption action to obtain a product of the wastewater treatment agent subjected to the adsorption action.
  10. The process of any one of claims 1 to 9, wherein the second reaction conditions comprise a second reaction temperature of 20 ℃ to 50 ℃.
  11. The process of any one of claims 1 to 10, wherein the second reaction conditions comprise a PH of 5 to 11.
  12. The method of any one of claims 1 to 11, wherein the wastewater produced by the production of heavy metals comprises at least one of nickel, copper, cobalt, arsenic, cadmium, lead.
  13. The method of any one of claims 1-12, wherein the processing the second reaction product by a third reaction process to obtain a third reaction product comprises:
    introducing carbon dioxide gas into a product of the wastewater treatment agent after adsorption, and performing desorption reaction under a third reaction condition to obtain a third reaction product; and
    subjecting the third reaction product to a third separation process to obtain the first portion and the second portion.
  14. The process of claim 13, wherein the third reaction conditions comprise a pressure of 0.3 to 0.5MPa for the desorption reaction.
  15. The method according to any one of claims 1 to 14,
    the first portion comprises a magnesium bicarbonate solution; and
    the second fraction comprises a heavy metal carbonate precipitate.
  16. The method of claim 15, wherein the first recycling process on the first portion comprises:
    heating the magnesium bicarbonate solution to obtain magnesium carbonate precipitate;
    calcining the magnesium carbonate precipitate to obtain a product carbon dioxide gas and a magnesium oxide solid, wherein the product carbon dioxide gas is recycled for a reactant in the third reaction process; and
    and carrying out flue gas desulfurization reaction on the magnesium oxide solid to obtain a magnesium sulfate solution, wherein the magnesium sulfate solution is used for preparing a reactant of the wastewater treatment agent.
  17. An apparatus for product recovery during the preparation and use of a wastewater treatment agent, the apparatus comprising:
    a first device for obtaining a wastewater treatment agent through a first reaction process;
    the second device is used for introducing the wastewater treatment agent into wastewater generated by preparing heavy metals and obtaining a second reaction product through a second reaction process, wherein the second reaction product at least comprises a product of the wastewater treatment agent after adsorption;
    a third device, configured to process the second reaction product through a third reaction process to obtain a third reaction product, where the third reaction product at least includes a first portion and a second portion;
    the first recovery device is used for carrying out first recovery treatment on the first part to obtain a reactant for preparing the wastewater treatment agent; and
    and the second recovery device is used for carrying out second recovery treatment on the second part to obtain a reactant for preparing the heavy metal.
CN202080099993.6A 2020-05-22 2020-05-22 Product recovery method and device used in preparation and use processes of wastewater treatment agent Pending CN115443185A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/CN2020/091714 WO2021232391A1 (en) 2020-05-22 2020-05-22 Product recovery method and device used in preparation and use processes of wastewater treatment agent

Publications (1)

Publication Number Publication Date
CN115443185A true CN115443185A (en) 2022-12-06

Family

ID=78708986

Family Applications (1)

Application Number Title Priority Date Filing Date
CN202080099993.6A Pending CN115443185A (en) 2020-05-22 2020-05-22 Product recovery method and device used in preparation and use processes of wastewater treatment agent

Country Status (2)

Country Link
CN (1) CN115443185A (en)
WO (1) WO2021232391A1 (en)

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1803272A (en) * 2005-12-02 2006-07-19 杨第伦 Air bubble liquid membrane method for producing nanometer granule material
CN102190345A (en) * 2010-03-10 2011-09-21 中国科学院福建物质结构研究所 Method for enriching low-concentration heavy metal in water by recyclable magnesium hydroxide adsorbent
CN103910367A (en) * 2013-01-06 2014-07-09 北京化工大学 Method for preparing transparent magnesium hydroxide liquid phase dispersion
CN103911021A (en) * 2013-01-06 2014-07-09 北京化工大学 Transparent magnesium hydroxide liquid phase dispersion, preparation method and application thereof

Family Cites Families (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE10318746A1 (en) * 2003-04-25 2004-11-18 Dr. Ecker Gmbh Purification of liquids, especially water containing heavy metal ions, involves bonding the impurities on or in magnesium hydroxide
US8507004B2 (en) * 2008-12-17 2013-08-13 Sandia Corporation Use of MgO doped with a divalent or trivalent metal cation for removing arsenic from water
KR20180000231A (en) * 2016-06-22 2018-01-02 광운대학교 산학협력단 A heavy metal adsorbent, a fixed column having the same and a method of adsorbing heavy metal using the same
CN106379924B (en) * 2016-08-26 2018-09-25 中山华明泰科技股份有限公司 A kind of nano magnalium hydrotalcite and preparation method thereof
CN106809908B (en) * 2017-01-20 2020-06-16 北京航空航天大学 Method for degrading heavy metal ions under assistance of gas

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN1803272A (en) * 2005-12-02 2006-07-19 杨第伦 Air bubble liquid membrane method for producing nanometer granule material
CN102190345A (en) * 2010-03-10 2011-09-21 中国科学院福建物质结构研究所 Method for enriching low-concentration heavy metal in water by recyclable magnesium hydroxide adsorbent
CN103910367A (en) * 2013-01-06 2014-07-09 北京化工大学 Method for preparing transparent magnesium hydroxide liquid phase dispersion
CN103911021A (en) * 2013-01-06 2014-07-09 北京化工大学 Transparent magnesium hydroxide liquid phase dispersion, preparation method and application thereof

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
郝吉明: "《大气污染控制工程实验》", 中国建材工业出版社, pages: 137 *

Also Published As

Publication number Publication date
WO2021232391A1 (en) 2021-11-25

Similar Documents

Publication Publication Date Title
JP5652503B2 (en) Scandium recovery method
JP3344194B2 (en) Method for producing high-purity rare earth metal oxide from oxidized ore
CN108588446B (en) Method for extracting molybdenum and rhenium from rhenium-containing molybdenum concentrate
CN111250148A (en) Catalyst for preparing cyclohexylbenzene by benzene hydroalkylation and preparation method and application thereof
CN106512999A (en) Dry-gas reforming catalyst for methane and preparation method for dry-gas reforming catalyst for methane
CN112473665A (en) Supported silver-manganese catalyst and preparation method and application thereof
CN106068242B (en) Activation U3O8 is so that it is converted into hydration UO4 method
CN110237864B (en) Heterogeneous catalyst and preparation method and application thereof
CN115443185A (en) Product recovery method and device used in preparation and use processes of wastewater treatment agent
CN111455192A (en) Method for recovering palladium from low-grade palladium-containing indissolvable waste catalyst
CN116832777A (en) Carbon-based material, preparation method and application thereof, and uranium-containing wastewater purification method
CN114836635B (en) Method for preparing high-purity metal arsenic by nonferrous smelting arsenic-containing solid waste short process
CN113634274B (en) Method for efficiently decomposing hydrogen peroxide by graphene-coated cobalt catalyst under acidic condition
CN110280213B (en) Nano magnetic composite iron-copper oxide dearsenization adsorbent and preparation method and application thereof
CN114367267A (en) Mesoporous composite material and preparation method and application thereof
CN110357164B (en) Method for green purification of manganese oxide ore slurry by coupling circulating efficient flue gas desulfurization with manganese sulfate
CN115041127B (en) Magnetic cerium-based metal oxide adsorbent and preparation method and application thereof
US3402026A (en) Precipitation of phosphorus values from aqueous media
US2816819A (en) Process of removing ferrous sulfate from sulfate solutions containing nickel and/or cobalt
JPH0431323A (en) Purification of manganese sulfate solution
CN109364734B (en) Method for reducing output of waste acid in non-ferrous metal smelting flue gas treatment process
CN113213537B (en) Method for separating and preparing vanadium trioxide from mixed solution of vanadium and chromium
CN116477679B (en) Method for preparing chloroiridium acid by recycling and purifying iridium catalyst with alumina carrier
CN114471517B (en) Lithium-based catalyst, preparation method thereof and application thereof in persulfate degradation of wastewater
CN113732297B (en) High-purity vanadium purification process

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
REG Reference to a national code

Ref country code: HK

Ref legal event code: DE

Ref document number: 40084886

Country of ref document: HK