Combined treatment method and device for glyphosate mother liquor and glyphosine mother liquor

Abstract

An embodiment of the present invention provides a combined treatment method and device for glyphosate mother liquor and glyphosate-N-methyliminodiacetic acid (PMIDA) mother liquor. The treatment method includes performing pretreatment on both the glyphosate mother liquor and the PMIDA mother liquor; subjecting the pretreated glyphosate mother liquor to membrane concentration separation; placing the diluted glyphosate solution obtained from the membrane concentration separation on the feed side of forward osmosis; placing the pretreated PMIDA mother liquor on the draw solution side of forward osmosis; performing ion exchange recovery treatment on the concentrated feed solution; and performing membrane concentration separation and recovery treatment on the diluted draw solution. The present invention utilizes the combined treatment method for glyphosate mother liquor and PMIDA mother liquor for resource recycling. At the same time, by using the salt concentration difference between the glyphosate mother liquor and the PMIDA mother liquor, forward osmosis technology is adopted to concentrate the glyphosate mother liquor and dilute the PMIDA mother liquor respectively, greatly improving the subsequent membrane treatment effect.

Description

Technical Field

[0001] The present invention relates to the technical field of organic phosphine pesticide wastewater treatment, and particularly relates to a combined treatment method and device for glyphosate mother liquor and diglyphosate mother liquor. Background Art

[0002] Glyphosate mother liquor and diglyphosate mother liquor generated during the production of the herbicide glyphosate (IDA method, iminodiacetic acid). It is understood that the utilization rate of total phosphorus in the glyphosate production process is only 60% - 65%, and 30% - 35% of phosphorus enters the mother liquor. If not properly treated and directly discharged into the environment, it will cause serious pollution. Before 2010, enterprises basically adopted the method of concentrating the mother liquor and then adding glyphosate solid and auxiliaries to prepare 10% glyphosate aqueous solution for sale. In February 2009, the Ministry of Industry and Information Technology and the Ministry of Agriculture jointly issued Announcement No. 1158, clearly stipulating that glyphosate aqueous solutions with an active ingredient content of less than 30% should stop production by the end of 2009, and the produced aqueous solutions should stop sales and use by the end of 2011. This means that the mother liquor must be effectively treated. In May 2013, the Ministry of Environmental Protection launched an environmental protection inspection of glyphosate (diglyphosate) production enterprises. Among them, the key inspection is the treatment of the mother liquor, and the verification of the comprehensive utilization rate of total phosphorus and the recovery and treatment of sodium chloride is relatively strict. Therefore, the resource recovery and utilization of the mother liquor is directly related to the survival and development of enterprises. The glyphosate mother liquor contains 1% - 1.5% glyphosate, 3% - 4% formaldehyde, about 2% formic acid, and unreacted diglyphosate, etc., and the salt content is less than 1%; the diglyphosate mother liquor contains 1.5% - 3% diglyphosate, about 1% phosphorous acid, and 0.1% - 3% formaldehyde, etc., and the salt content is relatively high, 15% - 20% (mainly sodium chloride). It can be seen that the components in the glyphosate mother liquor and the diglyphosate mother liquor are complex, and the concentrations of multiple components are relatively high. On the one hand, the treatment difficulty is high, and on the other hand, it has recycling value. Currently, enterprises mostly adopt a combination of membrane separation technology and evaporation crystallization process to recover glyphosate, diglyphosate, and sodium chloride, and a few adopt the incineration method, separating and purifying the mother liquor and then incinerating it to prepare phosphate. In addition, due to the high salt concentration in the diglyphosate mother liquor, there are disadvantages such as low flux, low total phosphorus interception rate, and easy pollution in the application of membrane separation technology. Summary of the Invention

[0003] The embodiments of the present invention provide a combined treatment method and device for glyphosate mother liquor and diglyphosate mother liquor to solve one or more technical problems encountered in the prior art.

[0004] In a first aspect, the embodiments of the present invention provide a combined treatment method for glyphosate mother liquor and diglyphosate mother liquor, including:

[0005] Performing pretreatment on both the glyphosate mother liquor and the diglyphosate mother liquor;

[0006] Perform membrane concentration separation on the pretreated glyphosate mother liquor;

[0007] Put the diluted glyphosate solution obtained from membrane concentration separation into the feed side of forward osmosis;

[0008] Put the pretreated diglycolic acid mother liquor into the draw solution side of forward osmosis;

[0009] Perform ion exchange recovery treatment on the concentrated feed liquid;

[0010] Perform membrane concentration separation and recovery treatment on the diluted draw solution.

[0011] In a preferred embodiment, the pretreatment of both the glyphosate mother liquor and the diglycolic acid mother liquor includes:

[0012] Adjust the pH of the glyphosate mother liquor and the diglycolic acid mother liquor to 3 - 10;

[0013] Perform fine filtration on the adjusted glyphosate mother liquor and diglycolic acid mother liquor; wherein, the precision of fine filtration is 0.45μm - 50μm.

[0014] In a preferred embodiment, the step of performing membrane concentration separation on the pretreated glyphosate mother liquor includes:

[0015] Perform membrane concentration separation on the pretreated glyphosate mother liquor to obtain concentrated glyphosate solution and diluted glyphosate solution; wherein, the cut-off molecular weight of membrane concentration separation is 150 - 200Da, the operating pressure of membrane concentration separation is 2.0 - 4.0Mpa, and the recovery rate of membrane concentration separation is 50% - 90%;

[0016] Add glyphosate solid to the concentrated glyphosate solution to prepare high-concentration glyphosate aqueous solution; or, cool and crystallize the concentrated glyphosate solution to obtain glyphosate solid.

[0017] In a preferred embodiment, the operating pressure of forward osmosis is 0.01 - 0.05Mpa, and the recovery rate of forward osmosis is 30% - 70%.

[0018] In a preferred embodiment, the step of performing ion exchange recovery treatment on the concentrated feed liquid includes:

[0019] The concentrated glyphosate feed liquid is separated from formic acid through ion exchange, and the remaining formaldehyde solution is reused in the condensation section of the glyphosate production process or ammoniated to prepare hexamine;

[0020] The resin for ion exchange is regenerated with a regenerant solution to obtain a regenerated waste liquid sodium formate solution; wherein, the resin for ion exchange is an acrylic weak basic anion exchange resin, the regenerant solution is NaOH with a mass concentration of 4% - 10%, the working flow rate during ion exchange operation is 1 - 5 BV / h; the working flow rate during resin regeneration is 1 - 3 BV / h.

[0021] In a preferred embodiment, the step of subjecting the diluted extractant to membrane concentration separation and recovery treatment includes:

[0022] The diluted glyphosate extractant is subjected to the first membrane separation and concentration; wherein, the cut-off molecular weight of the first membrane separation and concentration is 150 - 200 Da; the operating pressure of the first membrane separation and concentration is 2.0 - 4.0 Mpa, and the recovery rate of the first membrane separation and concentration is 50% - 90%;

[0023] The glyphosate concentrate obtained from the first membrane separation and concentration is directly recycled to the redox section in the glyphosate production process; or, the glyphosate concentrate obtained from the first membrane separation and concentration is subjected to evaporation crystallization to obtain glyphosate solid;

[0024] The glyphosate dilute solution obtained from the first membrane separation and concentration is subjected to the second membrane separation and concentration; wherein, the cut-off molecular weight of the second membrane separation and concentration is 100 - 200 Da; the operating pressure of the second membrane separation and concentration is 2.0 - 4.0 Mpa, and the recovery rate of the second membrane separation and concentration is 50% - 90%;

[0025] The glyphosate concentrate obtained from the second membrane separation and concentration is recycled to the condensation section in the glyphosate production process;

[0026] The glyphosate dilute solution obtained from the second membrane separation and concentration is used for the crude brine in the chlor-alkali industry; or, the glyphosate dilute solution obtained from the second membrane separation and concentration is subjected to evaporation crystallization to obtain sodium chloride solid.

[0027] In a second aspect, an embodiment of the present invention provides a combined treatment device for glyphosate mother liquor and diglycolic acid mother liquor, including:

[0028] A first pretreatment device, which is used for pretreating the glyphosate mother liquor;

[0029] A second pretreatment device, which is used for pretreating the diglycolic acid mother liquor;

[0030] A first-stage membrane separation and concentration unit, which is connected to the first pretreatment device and is used for membrane concentration separation of the pretreated glyphosate mother liquor;

[0031] An osmotic unit, the feed liquid side of the osmotic unit is connected to the glyphosate dilute liquid outlet of the first-stage membrane separation and concentration unit, and the draw liquid side of the osmotic unit is connected to the second pretreatment device;

[0032] An ion exchange unit, the ion exchange unit is connected to the feed liquid side of the osmotic unit; the ion exchange unit is used for ion exchange recovery treatment of the concentrated feed liquid;

[0033] A multi-stage membrane separation and concentration unit, the multi-stage membrane separation and concentration unit is connected to the draw liquid side of the osmotic unit, and the multi-stage membrane separation and concentration unit is used for membrane concentration separation and recovery treatment of the diluted draw liquid.

[0034] In a preferred embodiment, the osmotic unit includes an osmotic membrane, the osmotic membrane is arranged between the feed liquid side and the draw liquid side, diversion nets are arranged on both sides of the osmotic membrane, the osmotic unit can adopt single-stage osmosis, two-stage osmosis or three-stage osmosis, and the segments are connected by an inter-stage booster pump; the material of the osmotic membrane is aromatic polyamide composite membrane or cellulose acetate, the operating pressure of the osmotic unit is 0.01 - 0.05 Mpa, and the recovery rate of the osmotic unit is 30% - 70%.

[0035] In a preferred embodiment, the ion exchange unit includes ion exchange resin, and the ion exchange resin is acrylic weak basic anion exchange resin; the working flow rate during the operation of the ion exchange unit is 1 - 5 BV / h; the regeneration liquid of the ion exchange unit is NaOH with a mass concentration of 4% - 10%, and the flow rate for resin regeneration of the ion exchange unit is 1 - 3 BV / h.

[0036] In a preferred embodiment, the multi-stage membrane separation and concentration unit includes:

[0037] A secondary membrane separation and concentration unit, the secondary membrane separation and concentration unit is connected to the draw liquid side of the osmotic unit, the secondary membrane separation and concentration unit includes a single-stage first-stage membrane separation and concentration unit, a single-stage two-stage membrane separation and concentration unit or a two-stage two-stage membrane separation and concentration unit, the segments are connected by an inter-stage booster pump, and the stages are connected by an intermediate water tank and a booster pump; the material of the secondary membrane separation and concentration unit includes aromatic polyamide composite membrane or poly(piperazine amide) composite membrane, the cut-off molecular weight of the secondary membrane separation and concentration unit is 150 - 200 Da; the operating pressure of the secondary membrane separation and concentration unit is 2.0 - 4.0 Mpa, and the recovery rate of the secondary membrane separation and concentration unit is 50% - 90%;

[0038] Tertiary membrane separation and concentration unit, the tertiary membrane separation and concentration unit is connected to the secondary membrane separation and concentration unit, the tertiary membrane separation and concentration unit includes one-stage one-stage, one-stage two-stage or two-stage two-stage; the material of the tertiary membrane separation and concentration unit includes aromatic polyamide composite membrane or poly(piperazine amide) composite membrane, the molecular weight cut-off of the tertiary membrane separation and concentration unit is 100 - 200 Da; the operating pressure of the tertiary membrane separation and concentration unit is 2.0 - 4.0 Mpa, and the recovery rate of the tertiary membrane separation and concentration unit is 50% - 90%.

[0039] One of the technical solutions in the above technical solutions has the following advantages or beneficial effects: By using the combined treatment method of glyphosate mother liquor and diglycolic acid mother liquor for resource recycling, and at the same time taking advantage of the salt difference in the glyphosate mother liquor and diglycolic acid mother liquor, the forward osmosis technology is used to concentrate the glyphosate mother liquor and dilute the diglycolic acid mother liquor respectively, which greatly improves the subsequent membrane treatment effect.

[0040] The above summary is only for the purpose of the specification and is not intended to be limiting in any way. In addition to the illustrative aspects, embodiments and features described above, by referring to the accompanying drawings and the following detailed description, further aspects, embodiments and features of the present invention will be readily apparent. BRIEF DESCRIPTION OF THE DRAWINGS

[0041] In the drawings, unless otherwise specified, the same reference numerals throughout the several views represent the same or similar components or elements. These drawings are not necessarily drawn to scale. It should be understood that these drawings only depict some embodiments disclosed in accordance with the present invention and should not be regarded as limiting the scope of the present invention.

[0042] Figure 1 Shows a schematic diagram of the overall structural connection of the combined treatment device for glyphosate mother liquor and diglycolic acid mother liquor according to an embodiment of the present invention. DETAILED DESCRIPTION OF THE EMBODIMENTS

[0043] In the following, only some exemplary embodiments are briefly described. As those skilled in the art can recognize, the described embodiments can be modified in various different ways without departing from the spirit or scope of the present invention. Therefore, the drawings and the description are considered to be exemplary in nature and not restrictive.

[0044] Figure 1 Shows a schematic diagram of the overall structural connection of the combined treatment device for glyphosate mother liquor and diglycolic acid mother liquor according to an embodiment of the present invention.

[0045] An embodiment of the present invention provides a combined treatment method for glyphosate mother liquor and diglycolic acid mother liquor, which can be referred to Figure 1 the schematic diagram of the structural connection in

[0046] Pretreat both the glyphosate mother liquor and the diglycolic acid mother liquor. During the pretreatment process, fine particles, SS (suspended solids), and macromolecular substances are removed.

[0047] Perform membrane concentration separation on the pretreated glyphosate mother liquor. After membrane separation and concentration, a glyphosate concentrated solution and a glyphosate dilute solution are obtained. Among them, the glyphosate concentrated solution can be additionally added with glyphosate solid to prepare a high-concentration glyphosate aqueous agent or be cooled and crystallized to obtain glyphosate solid.

[0048] Put the glyphosate dilute solution obtained by membrane concentration separation into the feed solution side of forward osmosis.

[0049] Put the pretreated diglycolic acid mother liquor into the draw solution side of forward osmosis. The feed solution side (glyphosate dilute solution) and the draw solution side (diglycolic acid mother liquor) are separated by a forward osmosis membrane. Since the salt concentration on the draw solution side is much greater than the salt concentration on the feed solution side, the salt concentration difference forms an osmotic pressure difference. Under the driving force of this osmotic pressure difference, the water molecules in the feed solution pass through the forward osmosis membrane and enter the draw solution side. The feed solution is gradually concentrated in the system, and the salt concentration gradually increases; while the draw solution absorbs a large amount of water, and the salt concentration gradually decreases.

[0050] Perform ion exchange recovery treatment on the concentrated feed solution (glyphosate concentrated solution).

[0051] Perform membrane concentration separation and recovery treatment on the diluted draw solution (diglycolic acid diluted solution).

[0052] In a specific embodiment, the pretreatment of both the glyphosate mother liquor and the diglycolic acid mother liquor includes:

[0053] Adjust the pH of the glyphosate mother liquor and the diglycolic acid mother liquor to 3 - 10;

[0054] Perform fine filtration on the adjusted glyphosate mother liquor and diglycolic acid mother liquor; among them, the accuracy of fine filtration is 0.45μm - 50μm, and the fine filtration equipment includes one or a combination of two of a mechanical filter, a bag filter, a precision filter, or a tubular microfilter.

[0055] In a specific embodiment, the step of performing membrane concentration separation on the pretreated glyphosate mother liquor includes:

[0056] Perform membrane concentration separation on the pretreated glyphosate mother liquor to obtain a glyphosate concentrated solution and a glyphosate dilute solution; among them, the molecular weight cut-off of membrane concentration separation is 150 - 200Da, the operating pressure of membrane concentration separation is 2.0 - 4.0Mpa, and the recovery rate of membrane concentration separation is 50% - 90%.

[0057] Add glyphosate solid to the glyphosate concentrated solution to prepare a high-concentration glyphosate aqueous agent; or, cool and crystallize the glyphosate concentrated solution to obtain glyphosate solid.

[0058] In a specific embodiment, the operating pressure of the forward osmosis is 0.01 to 0.05 Mpa, and the recovery rate of the forward osmosis is 30% to 70%. Among them, the recovery rate can be set according to the water quality indexes and requirements of the glyphosate mother liquor and the diglycolic acid mother liquor.

[0059] In a specific embodiment, the step of subjecting the concentrated feed liquid to ion exchange recovery treatment includes:

[0060] The concentrated glyphosate feed liquid is separated from formic acid through ion exchange, and the remaining formaldehyde solution is recycled to the condensation section in the glyphosate production process or used for ammoniation to prepare hexamine.

[0061] The resin for ion exchange is regenerated with a regenerant solution to obtain a regenerated waste liquid sodium formate solution. Among them, the resin for ion exchange is an acrylic weak basic anion exchange resin, the regenerant solution is NaOH with a mass concentration of 4% to 10%, the working flow rate during ion exchange operation is 1 to 5 BV / h; the working flow rate during resin regeneration is 1 to 3 BV / h.

[0062] In a specific embodiment, the step of subjecting the diluted draw solution to membrane concentration separation and recovery treatment includes:

[0063] The diluted diglycolic acid draw solution is subjected to the first membrane separation and concentration; among them, the cut-off molecular weight of the first membrane separation and concentration is 150 to 200 Da; the operating pressure of the first membrane separation and concentration is 2.0 to 4.0 Mpa, and the recovery rate of the first membrane separation and concentration is 50% to 90%.

[0064] The concentrated diglycolic acid solution obtained by the first membrane separation and concentration is directly recycled to the redox section in the glyphosate production process; or, the concentrated diglycolic acid solution obtained by the first membrane separation and concentration is subjected to evaporation crystallization to obtain diglycolic acid solid.

[0065] The diluted diglycolic acid solution obtained by the first membrane separation and concentration is subjected to the second membrane separation and concentration; among them, the cut-off molecular weight of the second membrane separation and concentration is 100 to 200 Da; the operating pressure of the second membrane separation and concentration is 2.0 to 4.0 Mpa, and the recovery rate of the second membrane separation and concentration is 50% to 90%.

[0066] The concentrated diglycolic acid solution obtained by the second membrane separation and concentration is recycled to the condensation section in the glyphosate production process.

[0067] The diluted diglycolic acid solution obtained by the second membrane separation and concentration is used for the crude brine in the chlor-alkali industry; or, the diluted diglycolic acid solution obtained by the second membrane separation and concentration is subjected to evaporation crystallization to obtain sodium chloride solid.

[0068] Second aspect, an embodiment of the present invention provides a combined treatment device for glyphosate mother liquor and glyphosate-N-methyliminodiacetic acid mother liquor. Refer to Figure 1 As shown, the device includes a first pretreatment device 110, a second pretreatment device 130, a first-stage membrane separation and concentration unit 120, a forward osmosis unit 140, an ion exchange unit 150, and a multi-stage membrane separation and concentration unit 160.

[0069] The first pretreatment device 110 is used to pretreat the glyphosate mother liquor. During the pretreatment process, fine particles, SS (suspended solids), and macromolecular substances are removed.

[0070] The second pretreatment device 130 is used to pretreat the glyphosate-N-methyliminodiacetic acid mother liquor.

[0071] Among them, the filtration accuracy of the first pretreatment device 110 and the second pretreatment device 130 is 0.45μm to 50μm. The fine filtration equipment of the first pretreatment device 110 and the second pretreatment device 130 includes one or a combination of two of a mechanical filter, a bag filter, a precision filter, or a tubular microfilter.

[0072] The first-stage membrane separation and concentration unit 120 is connected to the first pretreatment device 110, and the first-stage membrane separation and concentration unit 120 is used to perform membrane concentration separation on the pretreated glyphosate mother liquor.

[0073] The feed liquid side of the forward osmosis unit 140 is connected to the glyphosate dilute liquid outlet of the first-stage membrane separation and concentration unit 120, and the draw solution side of the forward osmosis unit 140 is connected to the second pretreatment device 130.

[0074] The ion exchange unit 150 is connected to the feed liquid side of the forward osmosis unit 140; the ion exchange unit 150 is used to perform ion exchange recovery treatment on the concentrated feed liquid.

[0075] The multi-stage membrane separation and concentration unit 160 is connected to the draw solution side of the forward osmosis unit 140, and the multi-stage membrane separation and concentration unit 160 is used to perform membrane concentration separation and recovery treatment on the diluted draw solution.

[0076] In a specific embodiment, the forward osmosis unit 140 includes a forward osmosis membrane. The forward osmosis membrane is arranged between the feed liquid side and the draw solution side. Flow guiding nets are provided on both sides of the forward osmosis membrane. The forward osmosis unit can adopt single-stage forward osmosis, two-stage forward osmosis, or three-stage forward osmosis. The stages are connected by an inter-stage booster pump; the material of the forward osmosis membrane is an aromatic polyamide composite membrane or cellulose acetate. The operating pressure of the forward osmosis unit is 0.01 to 0.05 Mpa, and the recovery rate of the forward osmosis unit is 30% to 70%.

[0077] In a specific embodiment, the ion exchange unit 150 includes ion exchange resin, and the ion exchange resin is acrylic weak-base anion exchange resin; when the ion exchange unit operates, the working flow rate is 1-5 BV / h; the regeneration liquid of the ion exchange unit is NaOH with a mass concentration of 4%-10%, and the flow rate for resin regeneration of the ion exchange unit is 1-3 BV / h.

[0078] In a specific embodiment, the multi-stage membrane separation and concentration unit 160 includes a secondary membrane separation and concentration unit 162 and a tertiary membrane separation and concentration unit 161.

[0079] The secondary membrane separation and concentration unit 162 is connected to the draw solution side of the forward osmosis unit 140. The secondary membrane separation and concentration unit 162 includes a one-stage one-level membrane separation and concentration unit, a one-stage two-level membrane separation and concentration unit, or a two-stage two-level membrane separation and concentration unit. Between stages, they are connected by an inter-stage booster pump, and between levels, they are connected by an intermediate water tank and a booster pump; the material of the secondary membrane separation and concentration unit 162 includes aromatic polyamide composite membrane or poly(piperazine amide) composite membrane, and the cut-off molecular weight of the secondary membrane separation and concentration unit 162 is 150-200 Da; the operating pressure of the secondary membrane separation and concentration unit 162 is 2.0-4.0 Mpa, and the recovery rate of the secondary membrane separation and concentration unit 162 is 50%-90%.

[0080] The tertiary membrane separation and concentration unit 161 is connected to the secondary membrane separation and concentration unit 162. The tertiary membrane separation and concentration unit 161 includes one-stage one-level, one-stage two-level, or two-stage two-level; the material of the tertiary membrane separation and concentration unit 161 includes aromatic polyamide composite membrane or poly(piperazine amide) composite membrane, and the cut-off molecular weight of the tertiary membrane separation and concentration unit 161 is 100-200 Da; the operating pressure of the tertiary membrane separation and concentration unit 161 is 2.0-4.0 Mpa, and the recovery rate of the tertiary membrane separation and concentration unit 161 is 50%-90%.

[0081] In the description of this specification, the description referring to terms such as "one embodiment", "some embodiments", "example", "specific example", or "some examples", etc. means that the specific features, structures, materials, or characteristics described in connection with that embodiment or example are included in at least one embodiment or example of the present invention. Moreover, the specific features, structures, materials, or characteristics described can be combined in a suitable manner in any one or more embodiments or examples. In addition, without contradiction, those skilled in the art can combine and combine the different embodiments or examples described in this specification and the features of different embodiments or examples.

[0082] Furthermore, the terms "first" and "second" are for descriptive purposes only and should not be construed as indicating or implying relative importance or implicitly specifying the quantity of the indicated technical features. Thus, features defined with "first" and "second" may explicitly or implicitly include at least one such feature. In the description of the present invention, "a plurality of" means two or more unless otherwise specifically defined.

[0083] As described above, the above are only specific embodiments of the present invention, but the protection scope of the present invention is not limited thereto. Any person skilled in the art within the technical scope disclosed by the present invention can easily think of various changes or substitutions, and these should all be covered within the protection scope of the present invention. Therefore, the protection scope of the present invention should be subject to the protection scope of the claims.

Claims

1. A method for jointly treating glyphosate mother liquor and diglyphosate mother liquor, characterized in that: include: Both glyphosate mother liquor and diglyphosate mother liquor were pretreated; The pretreated glyphosate mother liquor is subjected to membrane concentration and separation; The glyphosate dilute solution separated by membrane concentration is placed into the forward osmosis feed liquid side; The pretreated dimethylphosphine mother liquor is placed in the forward osmosis draw liquid side; The concentrated liquid is subjected to ion exchange recovery treatment; The diluted drawn liquid is subjected to membrane concentration, separation and recovery treatment; The step of performing membrane concentration and separation on the pretreated glyphosate mother liquor comprises: The pretreated glyphosate mother liquor is subjected to membrane concentration separation to obtain a glyphosate concentrate and a glyphosate dilute solution; wherein the molecular weight cut-off of the membrane concentration separation is 150 to 200 Da, the operating pressure of the membrane concentration separation is 2.0 to 4.0 MPa, and the recovery rate of the membrane concentration separation is 50% to 90%; Adding glyphosate solid to glyphosate concentrate to prepare a high-concentration glyphosate aqueous solution; or cooling and crystallizing the glyphosate concentrate to obtain glyphosate solid; The operating pressure of the forward osmosis is 0.01-0.05 MPa, and the recovery rate of the forward osmosis is 30%-70%.

2. The method for combined treatment of glyphosate mother liquor and diglyphosate mother liquor according to claim 1, wherein: The pretreatment of the glyphosate mother liquor and the diglyphosate mother liquor comprises: Adjust the pH of glyphosate mother solution and diglyphosate mother solution to 3-10; The adjusted glyphosate mother liquor and diglyphosate mother liquor are finely filtered; wherein the precision of the fine filtration is 0.45 μm to 50 μm.

3. The combined treatment method of glyphosate mother liquor and diglyphosate mother liquor according to claim 1, wherein: The step of performing ion exchange recovery treatment on the concentrated feed liquid comprises: The concentrated glyphosate solution is subjected to ion exchange to separate the formic acid, and the remaining formaldehyde solution is recycled to the condensation stage in the glyphosate production process or used for ammonia production to prepare hexamethylenetetramine; The resin undergoing ion exchange is regenerated using a regeneration liquid, and a sodium formate solution of the regeneration waste liquid is obtained; wherein the resin undergoing ion exchange is an acrylic acid-based weakly alkaline anion exchange resin, the regeneration liquid is NaOH with a mass concentration of 4% to 10%, the working flow rate during the ion exchange operation is 1 to 5 BV / h, and the working flow rate during the resin regeneration operation is 1 to 3 BV / h.

4. The method for combined treatment of glyphosate mother liquor and diglyphosate mother liquor according to claim 1, wherein: The step of carrying out membrane concentration, separation and recovery treatment on the diluted drawn liquid comprises: The diluted diglycophosphine extract is subjected to a first membrane separation and concentration; wherein the molecular weight cut-off of the first membrane separation and concentration is 150 to 200 Da; the operating pressure of the first membrane separation and concentration is 2.0 to 4.0 MPa, and the recovery rate of the first membrane separation and concentration is 50% to 90%; The diglycol phosphine concentrate obtained by the first membrane separation and concentration is directly recycled to the redox stage of the glyphosate production process; or the diglycol phosphine concentrate obtained by the first membrane separation and concentration is evaporated and crystallized to obtain diglycol phosphine solid; The diglycophosphine dilute solution obtained by the first membrane separation and concentration is subjected to a second membrane separation and concentration; wherein the molecular weight cut-off of the second membrane separation and concentration is 100 to 200 Da; the operating pressure of the second membrane separation and concentration is 2.0 to 4.0 MPa, and the recovery rate of the second membrane separation and concentration is 50% to 90%; The diglyphosate concentrate obtained by the second membrane separation and concentration is recycled to the condensation stage in the glyphosate production process; The dilute dimethylaminophosphine obtained by the second membrane separation and concentration is used as crude brine in the chlor-alkali industry; or the dimethylaminophosphine obtained by the second membrane separation and concentration is evaporated and crystallized to obtain sodium chloride solid.

5. A combined treatment device for glyphosate mother liquor and diglyphosate mother liquor, characterized in that: include: a first pretreatment device, wherein the first pretreatment device is used to pretreat the glyphosate mother liquor; a second pretreatment device, the second pretreatment device being used to pretreat the monoglyphosate mother liquor; a primary membrane separation and concentration unit, the primary membrane separation and concentration unit being connected to the first pretreatment device, and the primary membrane separation and concentration unit being used to perform membrane concentration and separation on the pretreated glyphosate mother liquor; A forward osmosis unit, wherein the feed liquid side of the forward osmosis unit is connected to the glyphosate dilute liquid outlet of the primary membrane separation and concentration unit, and the draw liquid side of the forward osmosis unit is connected to the second pretreatment device; An ion exchange unit, the ion exchange unit being connected to the feed liquid side of the forward osmosis unit; the ion exchange unit being used to perform ion exchange recovery treatment on the concentrated feed liquid; A multi-stage membrane separation and concentration unit, the multi-stage membrane separation and concentration unit is connected to the draw liquid side of the forward osmosis unit, and the multi-stage membrane separation and concentration unit is used to perform membrane concentration separation and recovery treatment on the diluted draw liquid; The forward osmosis unit includes a forward osmosis membrane, which is arranged between the feed liquid side and the draw liquid side. A guide net is provided on both sides of the forward osmosis membrane. The forward osmosis unit can adopt one-stage forward osmosis, two-stage forward osmosis, or three-stage forward osmosis, and the stages are connected by an inter-stage booster pump. The forward osmosis membrane is made of an aromatic polyamide composite membrane or cellulose acetate. The operating pressure of the forward osmosis unit is 0.01-0.05 MPa, and the recovery rate of the forward osmosis unit is 30%-70%. The ion exchange unit includes an ion exchange resin, which is an acrylic acid-based weakly basic anion exchange resin; the operating flow rate of the ion exchange unit during operation is 1 to 5 BV / h; the regeneration liquid of the ion exchange unit is NaOH with a mass concentration of 4% to 10%, and the flow rate of the ion exchange unit for resin regeneration is 1 to 3 BV / h.

6. The combined treatment device for glyphosate mother liquor and disodium glyphosate mother liquor according to claim 5, characterized in that: The multi-stage membrane separation and concentration unit comprises: A secondary membrane separation and concentration unit connected to the draw liquid side of the forward osmosis unit, the secondary membrane separation and concentration unit comprising a single-stage membrane separation and concentration unit, a single-stage two-stage membrane separation and concentration unit, or two-stage two-stage membrane separation and concentration units, the sections connected by inter-section booster pumps, and the stages connected by intermediate water tanks and booster pumps; the secondary membrane separation and concentration unit is made of an aromatic polyamide composite membrane or a polypiperazineamide composite membrane, has a molecular weight cutoff of 150-200 Da, has an operating pressure of 2.0-4.0 MPa, and has a recovery rate of 50%-90%; A three-stage membrane separation and concentration unit is connected to the two-stage membrane separation and concentration unit. The three-stage membrane separation and concentration unit includes one stage with one level, one stage with two levels, or two stages with two levels. The material of the three-stage membrane separation and concentration unit includes an aromatic polyamide composite membrane or a polypiperazineamide composite membrane. The molecular weight cutoff of the three-stage membrane separation and concentration unit is 100-200Da. The operating pressure of the three-stage membrane separation and concentration unit is 2.0-4.0Mpa. The recovery rate of the three-stage membrane separation and concentration unit is 50%-90%.

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