Continuous purification device for glufosinate-ammonium active compound

Abstract

The utility model discloses a glufosinate-ammonium technical continuous purification device which comprises a mother liquor buffer tank, a mother liquor transfer pump, a separation kettle, a heater, a separation kettle transfer pump, a suspension separator, a parallel crystallizer group, an evaporator feed pump, a vacuum scraper type film evaporator and a parallel dispersion kettle group, the mother liquor buffer tank is provided with a first inlet, a second inlet and a first outlet, and the first inlet is suitable for introducing glufosinate-ammonium hydrolysate; an inlet of the mother liquor transfer pump is communicated with a first outlet of the mother liquor buffer tank; the separation kettle is provided with a feeding hole, a gas phase outlet and a liquid phase outlet, the feeding hole is communicated with the outlet of the mother liquor transfer pump, and the separation kettle is suitable for stirring the mother liquor and separating a gas phase and a liquid phase; and the heater is arranged between the outlet of the mother liquor transfer pump and the feed port of the separation kettle. According to the utility model, the energy consumption is reduced, and the purity of the glufosinate-ammonium raw medicine is improved.

Description

Technical Field

[0001] This utility model relates to a continuous purification device for glufosinate technical grade, belonging to the field of chemical technology. Background Technology

[0002] Currently, glufosinate, as a broad-spectrum, non-selective herbicide, possesses both high weed control and broad-spectrum activity. It can be rapidly decomposed by microorganisms in the soil and is widely used for weed control in arable land, orchards, tea gardens, and glufosinate-resistant genetically modified crops. However, in actual glufosinate production, the concentration of synthesized glufosinate is often at a low level of around 10%, and the mixture of ammonium chloride and sodium chloride, which have similar properties, cannot meet the high purity requirements of downstream products for glufosinate technical. Therefore, the separation and purification of the synthesized glufosinate has become a necessary production step.

[0003] Currently, the mainstream purification process on the market is chemical neutralization-step crystallization. Although it has a high degree of industrial maturity, it generally suffers from long processes and high energy consumption. Moreover, in actual production using this process, the degree of automation and continuity is low, resulting in slow production efficiency. Given the current energy shortage and increasingly stringent environmental protection requirements, achieving continuous production of glufosinate purification and improving thermal energy utilization has become an urgent problem to be solved.

[0004] After searching the existing technology, it was found that Chinese patent CN111659330A discloses a process and equipment for continuous production of glufosinate. The patent uses a flash tank and evaporator for concentration, but it was found that the concentration efficiency was low and the energy consumption was high during use. Summary of the Invention

[0005] The technical problem to be solved by this utility model is to overcome the defects of the prior art and provide a continuous purification device for glufosinate technical, which reduces energy consumption and improves the purity of glufosinate technical.

[0006] To solve the above-mentioned technical problems, the technical solution of this utility model is: a continuous purification device for glufosinate technical grade, comprising:

[0007] A mother liquor buffer tank is provided with a first inlet, a second inlet and a first outlet, wherein the first inlet is suitable for introducing glufosinate hydrolysate.

[0008] A mother liquor transfer pump, the inlet of which is connected to the first outlet of the mother liquor buffer tank;

[0009] A separation vessel is provided with a separation vessel inlet, a gas phase outlet and a liquid phase outlet. The separation vessel inlet is connected to the outlet of the mother liquor transfer pump. The separation vessel is suitable for stirring the mother liquor and separating the gas phase and the liquid phase.

[0010] A heater is provided between the outlet of the mother liquor transfer pump and the inlet of the separation vessel, and the heater is adapted to heat the mother liquor output from the mother liquor buffer tank.

[0011] A separation vessel transfer pump, wherein the inlet of the separation vessel transfer pump is connected to the liquid phase outlet of the separation vessel;

[0012] A suspension separator is provided with a suspension separator inlet, an upper liquid phase outlet and a lower solid phase outlet. The suspension separator inlet is connected to the outlet of the separation vessel transfer pump, and the upper liquid phase outlet is connected to the second inlet of the mother liquor buffer tank.

[0013] A parallel crystallizer group is provided with a parallel crystallizer group inlet, an ammonia water inlet, and a mother liquor outlet. The parallel crystallizer group inlet is connected to the lower solid phase outlet of the suspension separator. The ammonia water inlet is adapted to introduce ammonia water to adjust the pH value of the mother liquor in the parallel crystallizer group.

[0014] An evaporator feed pump, the inlet of which is connected to the mother liquor outlet of the parallel crystallizer group;

[0015] A vacuum scraped thin-film evaporator is provided with a vacuum scraped thin-film evaporator inlet, a gas phase outlet and a concentrated liquid outlet, wherein the vacuum scraped thin-film evaporator inlet is connected to the outlet of the evaporator feed pump.

[0016] A parallel dispersion vessel group is provided, which has a parallel dispersion vessel group inlet, a solvent inlet and an outlet. The parallel dispersion vessel group inlet is connected to the concentrated liquid outlet of the vacuum scraped thin film evaporator. The solvent inlet is suitable for introducing methanol. The parallel dispersion vessel group is suitable for mixing and dispersing the concentrated liquid output from the vacuum scraped thin film evaporator with methanol to output glufosinate methanol solution.

[0017] Furthermore, it also includes: a condenser, the inlet of which is connected to the gas phase outlet of the separation vessel;

[0018] A dilute acid storage tank, the inlet of which is connected to the outlet of the condenser.

[0019] Furthermore, it also includes: a second condenser, the inlet of which is connected to the gas phase outlet of the vacuum scraped thin film evaporator, the second condenser being adapted to condense the gas phase output from the vacuum scraped thin film evaporator into dilute ammonia water;

[0020] A dilute ammonia water storage tank, the inlet of which is connected to the outlet of the second condenser.

[0021] Furthermore, it also includes a control valve assembly, the control valve assembly comprising:

[0022] A first control valve is disposed between the first outlet of the mother liquor buffer tank and the inlet of the mother liquor transfer pump;

[0023] The second control valve is located between the liquid phase outlet of the separation vessel and the inlet of the separation vessel transfer pump.

[0024] The third control valve is located between the lower solid phase outlet of the suspension separator and the feed inlet of the parallel crystallizer group.

[0025] The fourth control valve is located between the mother liquor outlet of the parallel crystallizer group and the inlet of the evaporator feed pump;

[0026] The fifth control valve is located between the concentrate outlet of the vacuum scraper thin film evaporator and the feed inlet of the parallel dispersion vessel group.

[0027] Furthermore, the parallel crystallizer group includes:

[0028] A first crystallizer and a second crystallizer are connected in parallel.

[0029] The diversion pipe has an inlet end connected to the feed inlet of the parallel crystallizer group, and an outlet end connected to the inlets of the first crystallizer and the second crystallizer, respectively.

[0030] A merging pipe is provided, the inlet end of which is connected to the outlet of the first crystallizer and the outlet end of the second crystallizer, respectively, and the outlet end of the merging pipe is connected to the mother liquor outlet.

[0031] Furthermore, the parallel dispersion reactor assembly includes:

[0032] The first dispersion vessel and the second dispersion vessel are arranged in parallel;

[0033] A dispersing vessel diversion pipe, wherein the inlet end of the dispersing vessel diversion pipe is connected to the feed inlet of the parallel dispersing vessel group, and the outlet end of the dispersing vessel diversion pipe is connected to the inlets of the first dispersing vessel and the second dispersing vessel respectively;

[0034] A confluence pipe for the dispersion vessels is provided, wherein the inlet end of the confluence pipe is connected to the outlet of the first dispersion vessel and the outlet of the second dispersion vessel, respectively, and the outlet end of the confluence pipe is connected to the discharge port.

[0035] Furthermore, the separation vessel is equipped with a stirring device, which is adapted to stir the mother liquor inside the separation vessel.

[0036] By adopting the above technical solution, this utility model has the following beneficial effects:

[0037] In this invention, glufosinate hydrolysate is fed into a mother liquor buffer tank, and a mother liquor transfer pump transports the hydrolysate to a heater for heating. The heated mixture then flows into a separation vessel, where part evaporates and the other part enters a suspension separator. The suspension separator separates the mixture into an upper liquid layer and a lower solid layer. The upper liquid layer returns to the mother liquor buffer tank for recycling, while the lower solid layer enters the subsequent cooling crystallization process. The lower solid layer is introduced into a parallel crystallizer group, and 25% ammonia is added to adjust the pH to 6-7 to improve the crystallization effect. A vacuum scraped-film evaporator is used to further concentrate the pH-adjusted mother liquor, while simultaneously recovering ammonia gas to a dilute ammonia storage tank to avoid resource waste. The concentrated liquid enters a dispersion vessel where methanol is added and dispersed. Subsequently, centrifugation is used to obtain ammonium chloride solid and glufosinate methanol solution, achieving effective solid-liquid separation and product purification.

[0038] In summary, the continuous concentration and separation purification process provided by this utility model achieves efficient conversion of glufosinate hydrolysate, maximizes the recovery of process resources, and effectively controls by-products. It has significant beneficial effects such as high production efficiency, low energy consumption, good separation effect, and environmental friendliness. Attached Figure Description

[0039] Figure 1 This is a schematic diagram of the continuous purification device for glufosinate technical grade of this utility model. Detailed Implementation

[0040] To make the content of this utility model easier to understand, the present utility model will be further described in detail below with reference to specific embodiments and accompanying drawings.

[0041] like Figure 1 As shown, a continuous purification device for glufosinate technical grade includes:

[0042] Mother liquor buffer tank 1, mother liquor buffer tank 1 is provided with a first inlet 11, a second inlet 12 and a first outlet 13, the first inlet 11 is suitable for introducing glufosinate hydrolysate;

[0043] Mother liquor transfer pump 2, the inlet of mother liquor transfer pump 2 is connected to the first outlet 13 of mother liquor buffer tank 1;

[0044] Separation vessel 3 is provided with a separation vessel inlet 31, a gas phase outlet 32 ​​and a liquid phase outlet 33. The separation vessel inlet 31 is connected to the outlet of the mother liquor transfer pump 2. The separation vessel 3 is suitable for stirring the mother liquor and separating the gas phase and the liquid phase.

[0045] Heater 14 is located between the outlet of the mother liquor transfer pump 2 and the inlet 31 of the separation vessel 3. Heater 14 is suitable for heating the mother liquor output from the mother liquor buffer tank 1.

[0046] Separator transfer pump 4, the inlet of which is connected to the liquid phase outlet 33 of separator 3;

[0047] The suspension separator 5 is provided with a suspension separator inlet 51, an upper liquid phase outlet 52 and a lower solid phase outlet 53. The suspension separator inlet 51 is connected to the outlet of the separation vessel transfer pump 4, and the upper liquid phase outlet 52 is connected to the second inlet 12 of the mother liquor buffer tank 1.

[0048] Parallel crystallizer group 6 is provided with parallel crystallizer group inlet 61, ammonia water inlet (not shown in the figure) and mother liquor outlet 62. Parallel crystallizer group inlet 61 is connected to the lower solid phase outlet 53 of suspension separator 5. Ammonia water inlet is suitable for passing ammonia water to adjust the pH value of mother liquor in parallel crystallizer group 6.

[0049] Evaporator feed pump 7, the inlet of which is connected to the mother liquor outlet 62 of parallel crystallizer group 6;

[0050] The vacuum scraped thin film evaporator 8 is provided with a vacuum scraped thin film evaporator inlet 81, a gas phase outlet 82 and a concentrate outlet 83. The vacuum scraped thin film evaporator inlet 81 is connected to the outlet of the evaporator feed pump 7.

[0051] The parallel dispersion vessel group 9 is provided with a parallel dispersion vessel group inlet 91, a solvent inlet (not shown in the figure) and a discharge port 93. The parallel dispersion vessel group inlet 91 is connected to the concentrate outlet 83 of the vacuum scraped thin film evaporator 8. The solvent inlet is suitable for introducing methanol. The parallel dispersion vessel group 9 is suitable for mixing and dispersing the concentrate output from the vacuum scraped thin film evaporator 8 with methanol, and outputting glufosinate methanol solution.

[0052] In this embodiment, as Figure 1 As shown, the working process of the glufosinate technical continuous purification device is as follows: glufosinate hydrolysate enters the mother liquor buffer tank 1 through the first inlet 11. The mother liquor transfer pump transports the hydrolysate to the heater for heating. The heated mixture flows into the separation vessel 3. In the separation vessel 3, the stirring device stirs the mother liquor and performs separation at the same time, so that the gaseous substances in the mother liquor are discharged from the gas phase outlet 32, and the liquid substances are transported to the suspension separator 5 through the liquid phase outlet 33 and the separation vessel transfer pump 4.

[0053] Within the suspension separator 5, the mother liquor is separated into an upper liquid phase and a lower solid phase. The upper liquid phase is returned to the second inlet 12 of the mother liquor buffer tank 1 through the upper liquid phase outlet 52 to form a circulation. The lower solid phase enters the parallel crystallizer group 6 through the lower solid phase outlet 53. Within the parallel crystallizer group 6, 25% ammonia water is introduced into the mother liquor through the ammonia water inlet to adjust the pH value to 6-7. The adjusted mother liquor is then transported to the vacuum scraped thin-film evaporator 8 for further concentration through the mother liquor outlet 62 and the evaporator feed pump 7.

[0054] The vacuum scraped-film evaporator 8 separates the mother liquor into a gas phase and a concentrated liquid. The gas phase is discharged through the gas phase outlet 82, and the concentrated liquid enters the parallel dispersion vessel group 9 through the concentrated liquid outlet 83. The parallel dispersion vessel group 9 introduces methanol through the solvent inlet, mixes the concentrated liquid with methanol, and performs dispersion treatment. Finally, the parallel dispersion vessel group separates ammonium chloride solid and glufosinate methanol solution, completing the continuous purification process of glufosinate technical. Furthermore, in this embodiment, the ammonia water pipeline connected to the ammonia water inlet of the parallel crystallizer group 6... Figure 1 Not shown in the image.

[0055] Specifically, such as Figure 1 As shown, the continuous purification device for glufosinate technical grade also includes:

[0056] Condenser 100, the inlet of condenser 100 is connected to the gas phase outlet 32 ​​of separator 3;

[0057] The dilute acid storage tank 110 has its inlet connected to the outlet of the condenser 100.

[0058] In this embodiment, as Figure 1 As shown, during the operation of the continuous purification unit for glufosinate technical grade, the gas phase generated in the separation vessel 3 enters the condenser 100 through the gas phase outlet 32. The condenser 100 condenses the gas phase into a liquid substance. The condensed liquid flows through the outlet of the condenser 100 into the dilute acid storage tank 110 for collection, reducing material loss.

[0059] Specifically, such as Figure 1 As shown, the continuous purification device for glufosinate technical grade also includes:

[0060] The inlet of the second condenser 120 is connected to the gas phase outlet 82 of the vacuum scraped film evaporator 8. The second condenser 120 is suitable for condensing the gas phase output from the vacuum scraped film evaporator 8 into dilute ammonia water.

[0061] The inlet of the dilute ammonia water storage tank 130 is connected to the outlet of the second condenser 120.

[0062] In this embodiment, as Figure 1As shown, during the operation of the continuous purification unit for glufosinate technical grade, the gaseous substances generated by the vacuum scraped thin-film evaporator 8 enter the second condenser 120 through the gas outlet 82. The second condenser 120 condenses these gaseous substances, converting them into liquid dilute ammonia water. The resulting dilute ammonia water flows through the outlet of the second condenser 120 into the dilute ammonia water storage tank 130 for collection and storage.

[0063] Specifically, such as Figure 1 As shown, the continuous purification unit for glufosinate technical grade also includes a control valve group, which includes:

[0064] The first control valve 15 is located between the first outlet 13 of the mother liquor buffer tank 1 and the inlet of the mother liquor transfer pump 2.

[0065] The second control valve 16 is located between the liquid phase outlet 33 of the separator 3 and the inlet of the separator transfer pump 4.

[0066] The third control valve 17 is located between the lower solid phase outlet 53 of the suspension separator 5 and the parallel crystallizer group inlet 61 of the parallel crystallizer group 6.

[0067] The fourth control valve 18 is located between the mother liquor outlet 62 of the parallel crystallizer group 6 and the inlet of the evaporator feed pump 7.

[0068] The fifth control valve 19 is located between the concentrate outlet 83 of the vacuum scraper thin film evaporator 8 and the feed inlet 91 of the parallel dispersion vessel group 9.

[0069] In this embodiment, as Figure 1 As shown, the control valve group is used to regulate the material flow in each stage of the continuous purification unit for glufosinate technical. The first control valve 15 is located between the first outlet 13 of the mother liquor buffer tank 1 and the inlet of the mother liquor transfer pump 2, controlling the material flowing out of the mother liquor buffer tank 1. The second control valve 16 is installed between the liquid phase outlet 33 of the separator 3 and the inlet of the separator transfer pump 4, used to regulate the liquid phase material discharged from the separator 3. The third control valve 17 is located between the solid phase outlet 53 of the suspension separator 5 and the parallel crystallizer group inlet 61 of the parallel crystallizer group 6, controlling the flow rate of solid phase material entering the crystallizer.

[0070] The fourth control valve 18 is located between the mother liquor outlet 62 of the parallel crystallizer group 6 and the inlet of the evaporator feed pump 7, regulating the amount of material flowing from the crystallizer to the vacuum scraped thin film evaporator 8. The fifth control valve 19 is installed between the concentrate outlet 83 of the vacuum scraped thin film evaporator 8 and the parallel dispersion group inlet 91 of the parallel dispersion group 9, controlling the flow rate of the concentrate entering the parallel dispersion group 9.

[0071] Specifically, such as Figure 1 As shown, the parallel crystallizer group 6 includes:

[0072] The first crystallizer and the second crystallizer are arranged in parallel.

[0073] The diversion pipe has its inlet end connected to the feed inlet 61 of the parallel crystallizer group, and its outlet end connected to the inlet of the first crystallizer and the second crystallizer respectively.

[0074] The merging pipe has its inlet end connected to the outlets of the first crystallizer and the second crystallizer, respectively, and its outlet end connected to the mother liquor outlet 62.

[0075] In this embodiment, as Figure 1 As shown, the parallel crystallizer group 6 adopts a structure design with two crystallizers operating in parallel. Solid material from the suspension separator 5 enters the diversion pipe through the parallel crystallizer group inlet 61. The diversion pipe splits the material into two streams, which are then fed into the first and second crystallizers for processing. This parallel setup allows both crystallizers to operate simultaneously, or one crystallizer can be operated independently as needed, facilitating equipment maintenance and repair. After processing in the crystallizers, the material flows through its respective outlet into the merging pipe, and after converging, is discharged uniformly through the mother liquor outlet 62.

[0076] When one crystallizer requires maintenance or cleaning, another crystallizer can continue operating without interrupting the entire production process. This ensures the stable operation of the crystallization stage and the continuity of material flow during the continuous purification of glufosinate technical.

[0077] Specifically, such as Figure 1 As shown, the parallel dispersion vessel group 9 includes:

[0078] The first dispersion vessel and the second dispersion vessel are arranged in parallel;

[0079] The dispersing vessel diversion pipe has its inlet end connected to the feed inlet 91 of the parallel dispersing vessel group, and its outlet end connected to the inlets of the first dispersing vessel and the second dispersing vessel, respectively.

[0080] The inlet end of the merging pipe of the dispersion vessel is connected to the outlet of the first dispersion vessel and the outlet end of the merging pipe of the dispersion vessel and the outlet 93.

[0081] In this embodiment, as Figure 1 As shown, the parallel dispersion vessel group 9 adopts a parallel operating structure similar to that of the parallel crystallizer group 6. The concentrated liquid produced by the vacuum scraper thin-film evaporator 8 enters the dispersion vessel diversion pipe through the parallel dispersion vessel group inlet 91, and is then divided into two streams, entering the first dispersion vessel and the second dispersion vessel respectively. Inside the dispersion vessel, methanol introduced through the solvent inlet is thoroughly mixed with the concentrated liquid and dispersed. This parallel design allows the dispersion vessels to operate simultaneously to process materials, or one of the dispersion vessels can be selectively operated individually according to process requirements.

[0082] After thorough dispersion, the material flows out of the outlets of its respective dispersion reactors, merges into the confluence pipe of the dispersion reactors, and is finally discharged through outlet 93. When one dispersion reactor needs to be shut down for maintenance, the other dispersion reactor can continue to operate, ensuring the continuous operation of the glufosinate technical purification process and guaranteeing the stability of the production process.

[0083] Specifically, such as Figure 1 As shown, the separation vessel 3 is equipped with a stirring device, which is suitable for stirring the mother liquor in the separation vessel 3.

[0084] In this embodiment, as Figure 1 As shown, the stirring device inside the separation vessel 3 is a key component of the continuous purification unit for glufosinate technical. When the mother liquor enters the separation vessel 3 through the inlet 31, the stirring device begins operation, continuously agitating the mother liquor within the vessel. This agitation process promotes the separation of gaseous substances from the mother liquor.

[0085] The specific embodiments described above further illustrate the technical problems, technical solutions, and beneficial effects of this utility model. It should be understood that the above descriptions are merely specific embodiments of this utility model and are not intended to limit this utility model. Any modifications, equivalent substitutions, improvements, etc., made within the spirit and principles of this utility model should be included within the protection scope of this utility model.

Claims

1. A continuous purification device for glufosinate technical grade, characterized in that, include: Mother liquor buffer tank (1), the mother liquor buffer tank (1) is provided with a first inlet (11), a second inlet (12) and a first outlet (13), the first inlet (11) is suitable for introducing glufosinate hydrolysate; Mother liquor transfer pump (2), the inlet of which is connected to the first outlet (13) of the mother liquor buffer tank (1); Separation vessel (3), the separation vessel (3) is provided with a separation vessel inlet (31), a gas phase outlet (32) and a liquid phase outlet (33), the separation vessel inlet (31) is connected to the outlet of the mother liquor transfer pump (2), the separation vessel (3) is suitable for stirring the mother liquor and separating the gas phase and the liquid phase; Heater (14), the heater (14) is disposed between the outlet of the mother liquor transfer pump (2) and the separation vessel inlet (31) of the separation vessel (3), the heater (14) is adapted to heat the mother liquor output from the mother liquor buffer tank (1); Separation vessel transfer pump (4), the inlet of which is connected to the liquid phase outlet (33) of the separation vessel (3); The suspension separator (5) is provided with a suspension separator inlet (51), an upper liquid phase outlet (52) and a lower solid phase outlet (53). The suspension separator inlet (51) is connected to the outlet of the separation vessel transfer pump (4), and the upper liquid phase outlet (52) is connected to the second inlet (12) of the mother liquor buffer tank (1). A parallel crystallizer group (6) is provided with a parallel crystallizer group inlet (61), an ammonia water inlet and a mother liquor outlet (62). The parallel crystallizer group inlet (61) is connected to the lower solid phase outlet (53) of the suspension separator (5). The ammonia water inlet is suitable for introducing ammonia water to adjust the pH value of the mother liquor in the parallel crystallizer group (6). Evaporator feed pump (7), the inlet of which is connected to the mother liquor outlet (62) of the parallel crystallizer group (6); Vacuum scraped film evaporator (8), the vacuum scraped film evaporator (8) is provided with a vacuum scraped film evaporator inlet (81), a gas phase outlet (82) and a concentrate outlet (83), the vacuum scraped film evaporator inlet (81) is connected to the outlet of the evaporator feed pump (7); A parallel dispersion vessel group (9) is provided with a parallel dispersion vessel group inlet (91), a solvent inlet and an outlet (93). The parallel dispersion vessel group inlet (91) is connected to the concentrate outlet (83) of the vacuum scraped film evaporator (8). The solvent inlet is suitable for introducing methanol. The parallel dispersion vessel group (9) is suitable for mixing the concentrate output from the vacuum scraped film evaporator (8) with methanol and dispersing it to output glufosinate methanol solution.

2. The continuous purification apparatus for glufosinate technical grade according to claim 1, characterized in that, Also includes: A condenser (100) is connected to the gas phase outlet (32) of the separation vessel (3); A dilute acid storage tank (110) is provided, the inlet of which is connected to the outlet of the condenser (100).

3. The continuous purification apparatus for glufosinate technical grade according to claim 1, characterized in that, Also includes: The second condenser (120) has its inlet connected to the gas phase outlet (82) of the vacuum scraped film evaporator (8). The second condenser (120) is adapted to condense the gas phase output from the vacuum scraped film evaporator (8) into dilute ammonia water. A dilute ammonia water storage tank (130) is provided, the inlet of which is connected to the outlet of the second condenser (120).

4. The continuous purification apparatus for glufosinate technical grade according to claim 1, characterized in that, It also includes a control valve assembly, which comprises: A first control valve (15) is provided between the first outlet (13) of the mother liquor buffer tank (1) and the inlet of the mother liquor transfer pump (2); The second control valve (16) is located between the liquid phase outlet (33) of the separation vessel (3) and the inlet of the separation vessel transfer pump (4); The third control valve (17) is located between the lower solid phase outlet (53) of the suspension separator (5) and the parallel crystallizer group inlet (61) of the parallel crystallizer group (6). The fourth control valve (18) is located between the mother liquor outlet (62) of the parallel crystallizer group (6) and the inlet of the evaporator feed pump (7); The fifth control valve (19) is located between the concentrate outlet (83) of the vacuum scraper thin film evaporator (8) and the parallel dispersion vessel inlet (91) of the parallel dispersion vessel group (9).

5. The continuous purification apparatus for glufosinate technical grade according to claim 1, characterized in that, The parallel crystallizer group (6) includes: A first crystallizer and a second crystallizer are connected in parallel. The diversion pipe has an inlet end connected to the feed inlet (61) of the parallel crystallizer group, and an outlet end connected to the inlet of the first crystallizer and the second crystallizer respectively. The confluence pipe has its inlet end connected to the outlets of the first crystallizer and the second crystallizer, respectively, and its outlet end connected to the mother liquor outlet (62).

6. The continuous purification apparatus for glufosinate technical grade according to claim 1, characterized in that, The parallel dispersion reactor group (9) includes: The first dispersion vessel and the second dispersion vessel are arranged in parallel; The dispersing vessel diversion pipe has an inlet end connected to the feed inlet (91) of the parallel dispersing vessel group, and an outlet end connected to the inlets of the first dispersing vessel and the second dispersing vessel respectively. The inlet end of the dispersion vessel confluence pipe is connected to the outlet of the first dispersion vessel and the outlet end of the second dispersion vessel, respectively, and the outlet end of the dispersion vessel confluence pipe is connected to the discharge port (93).

7. The continuous purification apparatus for glufosinate technical grade according to claim 1, characterized in that, The separation vessel (3) is equipped with a stirring device, which is suitable for stirring the mother liquor in the separation vessel (3).

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