Production process of high-purity dimer acid

Abstract

The invention relates to the field of dimer acid production, in particular to a high-purity dimer acid production process, an extraction device is used, the extraction device comprises a mounting base used for supporting the whole device, and supporting legs are fixedly connected to the four corners of the bottom of the mounting base; the condensation reaction kettle is mounted at the top of the mounting seat, and an oleic acid dispersion kettle is arranged at the input end of the condensation reaction kettle; the nitrogen replacement assembly is arranged on the side of the condensation reaction kettle, is communicated with the condensation reaction kettle and is used for carrying out nitrogen replacement on the interior of the condensation reaction kettle, and a protection device is arranged in the nitrogen replacement assembly. Through the arrangement of the nitrogen replacement assembly, high-pressure impact can be reduced, and the purity can be further improved through multiple evaporation extraction, so that the problems that in the prior art, the purification effect cannot meet the requirements of the market for high-quality and high-purity dimer acid, and the valve is prone to damage due to large impact are solved.

Description

Technical Field

[0001] The invention relates to the field of dimer acid production, and in particular to a production process of high-purity dimer acid. Background Art

[0002] The polymer synthesized from dimer acid, an extended product of oleic acid, has excellent softness, sealing, water resistance and rust resistance. It is widely used in many industries such as machinery, automobiles, electronics, aerospace, shipping, textiles, daily chemicals, coatings, etc. Moreover, its application areas are constantly expanding and it has become an indispensable and important raw material for modern industry.

[0003] In the actual production process, most of the purification is done through molecular evaporation. The purification effect cannot meet the market's requirements for high-quality and high-purity dimer acid. In addition, when nitrogen replacement is performed, the air needs to be evacuated first to make it a vacuum setting, and then nitrogen is injected. When nitrogen is injected, the valve is easily damaged due to the large impact it receives.

[0004] Therefore, it is necessary to invent a production process of high-purity dimer acid to solve the above problems. Summary of the invention

[0005] The purpose of the present invention is to provide a production process for high-purity dimer acid. By setting a nitrogen replacement component, high-pressure shock can be reduced, and the purity can be further improved through multiple evaporation extraction, so as to solve the problem that the purification effect in the prior art cannot meet the market requirements for high-quality and high-purity dimer acid, and the valve is easily damaged due to the large impact it receives.

[0006] In order to achieve the above object, the present invention provides the following technical solution: a production process of high-purity dimer acid, using an extraction device, the extraction device comprising

[0007] A mounting base, used to support the entire device, with supporting legs fixedly connected to the four corners of the bottom of the mounting base;

[0008] A condensation reaction kettle is installed on the top of the mounting seat, and an oleic acid dispersion kettle is provided at the input end of the condensation reaction kettle;

[0009] A nitrogen replacement component is arranged at the side of the condensation reactor and is interconnected with the condensation reactor, and is used to replace the interior of the condensation reactor with nitrogen, and a protective device is arranged inside the nitrogen replacement;

[0010] A fine treatment component is arranged at the output end of the condensation reactor and is used to wash the output material of the condensation reactor;

[0011] A conduit, used for connecting the fine processing component with the purification processing component;

[0012] The purification processing component is used to evaporate and purify the processed raw materials.

[0013] As a preferred embodiment of the present invention, the interior of the condensation reactor is provided with an explosion-proof layer and a high-temperature resistant layer, and the interior of the condensation reactor is provided with an inner liner, the inner wall of the inner liner is provided with a corrosion-resistant layer, the top outer ring of the inner liner is fixedly connected to a mounting ring, the top of the mounting ring is detachably connected to a top cover, and a sealing gasket is provided between the top cover and the mounting ring.

[0014] As a preferred embodiment of the present invention, a feed pipe connected to the oleic acid dispersion kettle is provided on the top of the top cover, and a motor is also installed in the center of the top of the top cover. The output end of the motor passes through the top cover and is fixedly connected to a connecting rod. A plurality of staggered stirring rods are fixedly connected to the outer side of the connecting rod, and the plurality of stirring rods are all in contact with the inner wall of the inner tank.

[0015] As a preferred solution of the present invention, an air pressure sensor and a temperature sensor are also installed inside the top cover, and a hot oil pipe and a cold oil pipe are arranged inside the inner tank.

[0016] As a preferred embodiment of the present invention, the nitrogen replacement assembly includes an inlet valve and an outlet valve installed on the side wall of the condensation reactor, the inlet valve and the outlet valve are both provided with solenoid valves and are connected to the inner tank, the output end of the inlet valve is provided with a nitrogen converter, the output end of the nitrogen converter is provided with a nitrogen storage tank, the output end of the nitrogen storage tank is connected to a pressure reducing tank, and the output end of the pressure reducing tank is connected to the outlet valve.

[0017] As a preferred solution of the present invention, a mounting plate fixedly connected to a nitrogen replacement assembly is fixedly connected to the side of the pressure reducing tank, and two electric push rods are fixedly installed on the side of the mounting plate, and the output ends of the two electric push rods are fixedly connected to telescopic rods, and the ends of the two telescopic rods are respectively fixedly connected to a first push plate and a second push plate, and the inner side of the first push plate is fixedly connected to a second baffle and a first baffle, and the inner side of the second push plate is fixedly connected to a third baffle and a fourth baffle, and the first baffle, the second baffle, the third baffle and the fourth baffle are all slidably plugged and matched with the pressure reducing tank, wherein the third baffle is close to the input end of the pressure reducing tank, and the distance between the third baffle and the second baffle is smaller than the distance between the second baffle and the fourth baffle, which is smaller than the distance between the fourth baffle and the first baffle.

[0018] As a preferred solution of the present invention, a filter press is arranged inside the fine processing component, a filtrate temporary storage tank is arranged at the output end of the filter press, a disc centrifuge is arranged at the output end of the filtrate temporary storage tank, and a condensed acid temporary storage tank is arranged at the output end of the disc centrifuge.

[0019] As a preferred embodiment of the present invention, the purification processing component includes a long-path evaporator, a 1# short-path evaporator, a 2# short-path evaporator and a 3# short-path evaporator, the output end of the long-path evaporator is provided with a first outlet, the output end of the 1# short-path evaporator is provided with a second outlet, the output end of the 2# short-path evaporator is provided with a third outlet, and the output end of the 3# short-path evaporator is provided with a fourth outlet.

[0020] As a preferred embodiment of the present invention, the specific processing steps are as follows:

[0021] (1) Oleic acid catalytic polymerization unit: Oleic acid undergoes condensation reaction under catalyst pressure to generate monoacid, dimer acid, polymer acid, dimer acid lithium and carbon dioxide;

[0022] (2) Acidification unit: phosphoric acid is added to the polymer product to precipitate the metal cations bound to the dimer acid in the form of phosphate precipitation;

[0023] (3) Filtration and water washing separation unit: The acidified polymer is filtered and washed with water and centrifuged to remove impurities such as white clay to obtain crude dimer acid;

[0024] (4) Molecular distillation unit: After the crude dimer acid is distilled and dehydrated, it is subjected to molecular distillation No. 1 to obtain 99.5% monoacid and 80% dimer acid. After molecular distillation No. 2, the light component is separated. After molecular distillation No. 3, the heavy component 65% polyacid is separated to obtain a product of 98% high-purity dimer acid.

[0025] In the above technical solution, compared with the prior art, the technical effects and advantages provided by the present invention are as follows:

[0026] 1. When performing nitrogen replacement, the user can start the electric push rod, which drives the telescopic rod to move, wherein the first push plate and the second push plate move alternately, and the second push plate drives the third baffle and the fourth baffle to open, so that the nitrogen inside the nitrogen storage tank enters the pressure reduction tank on the side of the second baffle, and at the same time, the second baffle is connected to the first baffle to mix the gas pressure entering, and then the second push plate is closed, and the second baffle and the first baffle are driven to open by the first push plate, so that the other parts between the third baffle and the fourth baffle are merged, and the nitrogen on the side of the fourth baffle is released to the inside of the condensation reactor through the outlet valve, which is convenient for step-by-step pressure reduction, reduces the damage to the valve caused by pressure shock, and is conducive to reducing noise;

[0027] 2. Through multiple evaporation settings, the material can be further purified, which is beneficial to improve processing efficiency and further improve purity, and can meet the market requirements for high-quality and high-purity dimer acid. BRIEF DESCRIPTION OF THE DRAWINGS

[0028] In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, the drawings required for use in the embodiments will be briefly introduced below. Obviously, the drawings described below are only some embodiments recorded in the present invention. For ordinary technicians in this field, other drawings can also be obtained based on these drawings.

[0029] Figure 1 It is a schematic diagram of the overall structure of the present invention;

[0030] Figure 2 It is a schematic diagram of the exploded structure of the condensation reaction kettle of the present invention;

[0031] Figure 3 It is a schematic diagram of the internal structure of the nitrogen replacement component of the present invention;

[0032] Figure 4 It is a schematic diagram of the internal structure of the pressure reducing tank of the present invention;

[0033] Figure 5 It is a system processing block diagram of the present invention;

[0034] Figure 6 It is the pre-processing and detailed processing flow chart of the present invention;

[0035] Figure 7 It is the extraction process flow chart of the present invention.

[0036] Description of reference numerals:

[0037] 001, mounting base; 002, condensation reactor; 003, nitrogen replacement component; 004, fine processing component; 006, conduit; 007, purification processing component;

[0038] 101. Support leg;

[0039] 201, liner; 202, mounting ring; 203, top cover; 204, feed pipe; 205, discharge pipe; 206, oil pump mounting assembly; 207, motor; 208, connecting rod; 209, stirring rod; 210, air pressure sensor; 211, temperature sensor;

[0040] 301, inlet valve; 302, nitrogen converter; 303, nitrogen storage tank; 304, pressure reducing tank; 305, outlet valve; 310, mounting plate; 311, electric push rod; 312, telescopic rod; 313, first push plate; 314, first baffle; 315, second baffle; 316, second push plate; 317, third baffle; 318, fourth baffle;

[0041] 701, long-path evaporator; 702, first outlet; 703, 1# short-path evaporator; 704, second outlet; 705, 2# short-path evaporator; 706, third outlet; 707, 3# short-path evaporator; 708, fourth outlet. DETAILED DESCRIPTION

[0042] In order to enable those skilled in the art to better understand the technical solution of the present invention, the present invention will be further described in detail below with reference to the accompanying drawings.

[0043] The present invention provides Figure 1-7 A production process of high-purity dimer acid shown in FIG. 1 uses an extraction device, which includes

[0044] The mounting base 001 is used to support the entire device, and the four corners of the bottom of the mounting base 001 are fixedly connected with support legs 101;

[0045] The condensation reaction kettle 002 is installed on the top of the mounting seat 001, and an oleic acid dispersion kettle is provided at the input end of the condensation reaction kettle 002;

[0046] The nitrogen replacement component 003 is arranged at the side of the condensation reactor 002 and is interconnected with the condensation reactor 002, and is used to replace the interior of the condensation reactor 002 with nitrogen, and a protective device is arranged inside the nitrogen replacement;

[0047] The fine treatment component 004 is arranged at the output end of the condensation reaction kettle 002 and is used to wash the material output from the condensation reaction kettle 002;

[0048] The conduit 006 is used to connect the fine processing component 004 with the purification processing component 007;

[0049] The purification processing component 007 is used to evaporate and purify the processed raw materials.

[0050] The interior of the condensation reactor 002 is provided with an explosion-proof layer and a high-temperature resistant layer, and the interior of the condensation reactor 002 is provided with an inner liner 201, and the inner wall of the inner liner 201 is provided with a corrosion-resistant layer to extend the service life. The top outer ring of the inner liner 201 is fixedly connected with a mounting ring 202, and the top of the mounting ring 202 is detachably connected with a top cover 203, and a sealing gasket is provided between the top cover 203 and the mounting ring 202 to facilitate sealing and disassembly of the device.

[0051] The top of the top cover 203 is provided with a feed pipe 204 connected to the oleic acid dispersion kettle, the bottom of the condensation reactor 002 is provided with a discharge pipe 205 and an oil pump mounting assembly 206, and a motor 207 is also installed in the top center of the top cover 203. The output end of the motor 207 passes through the top cover 203 and is fixedly connected to a connecting rod 208. The outer side of the connecting rod 208 is fixedly connected with a plurality of staggered stirring rods 209, and the plurality of stirring rods 209 are all in contact with the inner wall of the inner tank 201, so as to facilitate uniform stirring of the raw materials inside and accelerate the reaction time.

[0052] An air pressure sensor 210 and a temperature sensor 211 are also installed inside the top cover 203, and a hot oil pipe and a cold oil pipe are arranged inside the inner tank 201;

[0053] The reactor is heated to a specified temperature with hot oil. Because the reaction is an exothermic reaction, the temperature will rise to about after the reaction starts. The regulating valve automatically controls to close the hot oil and appropriately opens the cold oil. When the reaction temperature rises to about the specified temperature, the cooling oil pipe in the reactor is used to adjust and maintain the temperature in the reactor. The air pressure sensor 210 and the temperature sensor 211 can detect the internal pressure and temperature.

[0054] The nitrogen replacement assembly 003 includes an inlet valve 301 and an outlet valve 305 installed on the side wall of the condensation reactor 002. The inlet valve 301 and the outlet valve 305 are both provided with solenoid valves and are both connected to the inner tank 201. The output end of the inlet valve 301 is provided with a nitrogen converter 302, and the output end of the nitrogen converter 302 is provided with a nitrogen storage tank 303. The output end of the nitrogen storage tank 303 is connected to a pressure reducing tank 304, and the output end of the pressure reducing tank 304 is connected to the outlet valve 305.

[0055] The gas inside the condensation reactor 002 is pumped into the nitrogen converter 302 for conversion by an air pump, and the converted gas is stored in the nitrogen storage tank 303, and returned to the condensation reactor 002 through the pressure reducing tank 304 to complete the nitrogen replacement.

[0056] The side of the pressure reducing tank 304 is fixedly connected with a mounting plate 310 fixedly connected to the nitrogen replacement assembly 003, and two electric push rods 311 are fixedly installed on the side of the mounting plate 310. The output ends of the two electric push rods 311 are fixedly connected with telescopic rods 312. The ends of the two telescopic rods 312 are respectively fixedly connected with a first push plate 313 and a second push plate 316. The inner side of the first push plate 313 is fixedly connected with a second baffle 315 and a first baffle 314. The inner side of the second push plate 316 is fixedly connected with a second baffle 316. The third baffle 317 and the fourth baffle 318 are fixedly connected to the side, and the first baffle 314, the second baffle 315, the third baffle 317 and the fourth baffle 318 are all slidably plugged and matched with the depressurization tank 304, wherein the third baffle 317 is close to the input end of the depressurization tank 304, and the distance between the third baffle 317 and the second baffle 315 is smaller than the distance between the second baffle 315 and the fourth baffle 318, which is smaller than the distance between the fourth baffle 318 and the first baffle 314;

[0057] When performing nitrogen replacement, the user can start the electric push rod 311, and the electric push rod 311 drives the telescopic rod 312 to move, wherein the first push plate 313 and the second push plate 316 move alternately, and the second push plate 316 drives the third baffle 317 and the fourth baffle 318 to open, so that the nitrogen inside the nitrogen storage tank 303 enters the inside of the pressure reduction tank 304 on the side of the second baffle 315, and at the same time, the second baffle 315 is connected to the first baffle 314 to mix the entering gas pressure, and then the second push plate 316 is closed, and then the first push plate 313 drives the second baffle 315 and the first baffle 314 to open, so that the other parts between the third baffle 317 and the fourth baffle 318 are merged, and the nitrogen on the side of the fourth baffle 318 is released to the inside of the condensation reactor 002 through the outlet valve 305, which is convenient for step-by-step pressure reduction, reduces the damage to the valve caused by pressure shock, and is conducive to reducing noise.

[0058] A filter press is provided inside the fine processing component 004, a filtrate temporary storage tank is provided at the output end of the filter press, a disc centrifuge is provided at the output end of the filtrate temporary storage tank, and a condensed acid temporary storage tank is provided at the output end of the disc centrifuge;

[0059] The reaction suspension is cooled to 100-110°C in the reactor and then pumped into the filter press. The separated dimer acid is temporarily stored in the filtrate storage tank. The filter cake containing phosphate and clay after filtration is outsourced for treatment.

[0060] The dimer acid filtrate is added with 30% to 40% water and washed and separated using a disc centrifuge to obtain a crude dimer acid which enters a condensation acid temporary storage tank for standby use.

[0061] The purification processing component 007 includes a long-path evaporator 701, a 1# short-path evaporator 703, a 2# short-path evaporator 705 and a 3# short-path evaporator 707. The output end of the long-path evaporator 701 is provided with a first outlet 702, the output end of the 1# short-path evaporator 703 is provided with a second outlet 704, the output end of the 2# short-path evaporator 705 is provided with a third outlet 706, and the output end of the 3# short-path evaporator 707 is provided with a fourth outlet 708, so as to facilitate multiple purification settings of the raw materials.

[0062] Oleic acid undergoes polymerization reaction under the action of catalyst kaolin and co-catalyst lithium carbonate to obtain a mixture of monoacid, dimer acid, polymeric acid and kaolin. After acidification and physical separation to remove kaolin and some impurities from the mixture, crude dimer acid containing only three components, dimer acid, monoacid and polymeric acid, is obtained. The crude dimer acid is then separated into several different products through three-stage molecular distillation. The production process of dimer acid mainly includes the following chemical units:

[0063] (1) Oleic acid catalytic polymerization unit: Oleic acid undergoes condensation reaction under catalyst pressure to generate monoacid, dimer acid, polymer acid, dimer acid lithium and carbon dioxide;

[0064] (2) Acidification unit: phosphoric acid is added to the polymer product to precipitate the metal cations bound to the dimer acid in the form of phosphate precipitation;

[0065] (3) Filtration and water washing separation unit: The acidified polymer is filtered and washed with water and centrifuged to remove impurities such as white clay to obtain crude dimer acid;

[0066] (4) Molecular distillation unit: After the crude dimer acid is distilled and dehydrated, it is subjected to molecular distillation No. 1 to obtain 99.5% monoacid and 80% dimer acid. After molecular distillation No. 2, the light component is separated. After molecular distillation No. 3, the heavy component 65% polyacid is separated to obtain a product of 98% high-purity dimer acid.

[0067] Oleic acid is pumped into the oleic acid dispersion kettle from the tank area. After adding kaolin and lithium carbonate into the oleic acid dispersion kettle through the metering tank and fully mixed, the materials are discharged into the condensation reactor. After the discharge is completed, the materials in the dispersion kettle and the discharge pipe are purged into the condensation reactor with nitrogen.

[0068] Start stirring the reactor, add process water into the reactor through the metering tank, and replace the reactor with nitrogen before the reaction.

[0069] The reactor is heated to 180-200°C with hot oil. Because the reaction is exothermic, the temperature will rise to about 230°C after the reaction starts. The regulating valve automatically controls to close the hot oil and appropriately open the cold oil. When the reaction temperature rises to about 250°C, the cooling oil pipe in the reactor is used to adjust to maintain the temperature in the reactor at 245-250°C.

[0070] A small amount of water produced during the reaction will turn into steam, which will increase the pressure of the reactor. The pneumatic regulating valve will be interlocked with the reactor pressure to release a certain amount of pressure, and the reactor pressure will be automatically controlled to maintain at about 0.45MPa. The temperature will be kept for 3 hours to complete the condensation reaction. The pressure will then be released to the tail gas system and the temperature will be reduced to 180-190℃.

[0071] The prepared 85% phosphoric acid was pumped into the reactor by a metering pump for acidification reaction. The reactor continued to cool down and was kept at about 140° C. for 30 minutes.

[0072] The gaseous part is discharged to the tail gas treatment system through the condenser, and the condensable liquid enters the sewage grease trap.

[0073] The reaction suspension is cooled to 100-110°C in the reactor and then pumped into the filter press. The separated dimer acid is temporarily stored in the filtrate storage tank. The filter cake containing phosphate and clay after filtration is outsourced for treatment.

[0074] The dimer acid filtrate is added with 30% to 40% water and washed and separated using a disc centrifuge to obtain a crude dimer acid which enters a condensation acid temporary storage tank for standby use.

[0075] The crude dimer acid in the condensation acid temporary storage tank is pumped into a long-range thin film evaporator (jacket heat transfer oil temperature 170-180°C) after flash dehydration. The crude dimer acid after distilling out water and low-boiling point substances is pumped into a 1# short-range thin film evaporator (jacket heat transfer oil temperature 240-250°C) to separate monoacid (99.5%) and common dimer acid (80%). Part of the common dimer acid (80%) is sent to a 2# short-range thin film evaporator (jacket heat transfer oil temperature 260-270°C), and the light component (mixture of dimer acid and monoacid) is separated and returned to the condensation acid temporary storage tank through a light component receiving tank. The heavy fraction is continuously pumped into the 3# short-path thin film evaporator (jacket heat transfer oil temperature 280-290°C) to separate high-purity dimer acid (98%) and heavy fractions, of which the high-purity dimer acid (98%) enters the high-purity dimer acid storage tank, and the heavy fraction is the polymer acid, which is sent to the polymer acid storage tank.

[0076] The multiple evaporation settings can further purify the material, which is beneficial to improving processing efficiency and further improving purity, and can meet the market requirements for high-quality and high-purity dimer acid.

[0077] The above description is only by way of illustration of certain exemplary embodiments of the present invention. It is undoubted that those skilled in the art can modify the described embodiments in various ways without departing from the spirit and scope of the present invention. Therefore, the above drawings and descriptions are illustrative in nature and should not be construed as limiting the scope of protection of the claims of the present invention.

Claims

1. A production process of high-purity dimer acid, using an extraction device, characterized in that: The extraction device comprises A mounting seat (001) is used to support the entire device, and the four corners of the bottom of the mounting seat (001) are fixedly connected to support legs (101); A condensation reaction kettle (002) is installed on the top of the mounting seat (001), and an oleic acid dispersion kettle is provided at the input end of the condensation reaction kettle (002); A nitrogen replacement component (003) is arranged on the side of the condensation reaction kettle (002) and is interconnected with the condensation reaction kettle (002) for performing nitrogen replacement on the interior of the condensation reaction kettle (002), and a protective device is arranged inside the nitrogen replacement; A fine treatment component (004) is arranged at the output end of the condensation reaction kettle (002) and is used to wash the material output from the condensation reaction kettle (002); A conduit (006) for connecting the fine processing component (004) and the purification processing component (007); The purification processing component (007) is used to evaporate and purify the processed raw materials.

2. The production process of high-purity dimer acid according to claim 1, characterized in that: The interior of the condensation reaction kettle (002) is provided with an explosion-proof layer and a high-temperature resistant layer, and the interior of the condensation reaction kettle (002) is provided with an inner liner (201), the inner wall of the inner liner (201) is provided with a corrosion-resistant layer, the top outer ring of the inner liner (201) is fixedly connected to a mounting ring (202), the top of the mounting ring (202) is detachably connected to a top cover (203), and a sealing gasket is provided between the top cover (203) and the mounting ring (202).

3. The production process of a high-purity dimer acid according to claim 2, characterized in that: The top of the top cover (203) is provided with a feed pipe (204) connected to the oleic acid dispersion kettle, and a motor (207) is also installed in the center of the top of the top cover (203). The output end of the motor (207) passes through the top cover (203) and is fixedly connected to a connecting rod (208). The outer side of the connecting rod (208) is fixedly connected to a plurality of staggered stirring rods (209), and the plurality of stirring rods (209) are all in contact with the inner wall of the inner container (201).

4. The production process of a high-purity dimer acid according to claim 2, characterized in that: An air pressure sensor (210) and a temperature sensor (211) are also installed inside the top cover (203), and a hot oil pipe and a cold oil pipe are arranged inside the inner tank (201).

5. The production process of a high-purity dimer acid according to claim 2, characterized in that: The nitrogen replacement component (003) comprises an inlet valve (301) and an outlet valve (305) installed on the side wall of the condensation reaction kettle (002); the inlet valve (301) and the outlet valve (305) are both provided with solenoid valves inside and are both connected to the inner tank (201); the output end of the inlet valve (301) is provided with a nitrogen converter (302); the output end of the nitrogen converter (302) is provided with a nitrogen storage tank (303); the output end of the nitrogen storage tank (303) is connected to a pressure reducing tank (304); the output end of the pressure reducing tank (304) is connected to the outlet valve (305).

6. The production process of high-purity dimer acid according to claim 5, characterized in that: The side of the pressure reducing tank (304) is fixedly connected to a mounting plate (310) fixedly connected to the nitrogen replacement assembly (003); two electric push rods (311) are fixedly installed on the side of the mounting plate (310); the output ends of the two electric push rods (311) are fixedly connected to telescopic rods (312); the ends of the two telescopic rods (312) are respectively fixedly connected to a first push plate (313) and a second push plate (316); the inner side of the first push plate (313) is fixedly connected to a second baffle plate (315) and a first baffle plate (314); the second push plate (31 6), the inner side of which is fixedly connected with a third baffle (317) and a fourth baffle (318), wherein the first baffle (314), the second baffle (315), the third baffle (317) and the fourth baffle (318) are all slidably plugged and matched with the pressure reducing tank (304), wherein the third baffle (317) is close to the input end of the pressure reducing tank (304), and the distance between the third baffle (317) and the second baffle (315) is smaller than the distance between the second baffle (315) and the fourth baffle (318), and the distance between the fourth baffle (318) and the first baffle (314).

7. The production process of high-purity dimer acid according to claim 1, characterized in that: A filter press is arranged inside the fine processing component (004), a filtrate temporary storage tank is arranged at the output end of the filter press, a disc centrifuge is arranged at the output end of the filtrate temporary storage tank, and a condensed acid temporary storage tank is arranged at the output end of the disc centrifuge.

8. The production process of high-purity dimer acid according to claim 1, characterized in that: The purification treatment component (007) includes a long-path evaporator (701), a 1# short-path evaporator (703), a 2# short-path evaporator (705) and a 3# short-path evaporator (707).

9. The production process of a high-purity dimer acid according to claim 1, characterized in that: The specific processing steps are as follows: (1) Oleic acid catalytic polymerization unit: Oleic acid undergoes condensation reaction under catalyst pressure to generate monoacid, dimer acid, polymer acid, dimer acid lithium and carbon dioxide; (2) Acidification unit: phosphoric acid is added to the polymer product to precipitate the metal cations bound to the dimer acid in the form of phosphate precipitation; (3) Filtration and water washing separation unit: The acidified polymer is filtered and washed with water and centrifuged to remove impurities such as white clay to obtain crude dimer acid; (4) Molecular distillation unit: After the crude dimer acid is distilled and dehydrated, it is subjected to molecular distillation No. 1 to obtain 99.5% monoacid and 80% dimer acid. After molecular distillation No. 2, the light component is separated. After molecular distillation No. 3, the heavy component 65% polyacid is separated to obtain a product of 98% high-purity dimer acid.

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