Crude heliotropin treatment device

Abstract

According to the heliotropin crude product treatment device, the heat exchanger is arranged to preheat a crude heliotropin solution stored in the crude product storage tank and then input the heliotropin solution into the rectifying tower to be rectified, the vacuum unit is arranged to vacuumize the rectifying tower so as to reduce the boiling point of rectified materials, and meanwhile the receiving tank group is arranged to receive fractions at different temperatures; according to the device, the rectifying tower is arranged, the synthesized heliotropin crude product is rectified and purified through the rectifying tower and then is fed into the crystallization kettle to be crystallized, the purity of the obtained heliotropin product can be effectively improved, the grade of the product is improved, and the yield of the heliotropin product is improved. The defect that after heliotropin is synthesized in an existing chemical mode, a high-purity heliotropin product is difficult to obtain through direct crystallization is overcome.

Description

Technical Field

[0001] The present application relates to the technical field of material purification, and in particular to a device for processing crude piperonal. Background Art

[0002] Piperonal is a kind of flavor aldehyde. Piperonal is widely used in perfumes, spices, cherry and vanilla flavoring agents (such as preparing vanilla and cherry essences), and can also be used in the synthesis of organic matter. Natural piperonal exists in small amounts in flower oils such as bilberry, melon, sweet pepper, sherry, and acacia, as well as vanilla beans. Due to the large demand for piperonal, the traditional method of extracting it from plants has been difficult to meet the demand, so the existing methods mostly use organic synthesis to prepare the corresponding flavor aldehydes.

[0003] The synthesis of piperonal is mainly to use 3,4-methylenedioxymandelic acid as the starting material and then undergo a nitric acid oxidation reaction to prepare piperonal. The melting point of piperonal is relatively low, at 37°C, and due to the influence of by-products in the reaction solution, it is difficult to obtain a product of high purity by direct crystallization. Therefore, it is necessary to purify piperonal before its crystallization operation. Utility Model Content

[0004] The present application provides a crude piperonal processing device, which is used to solve the problem that it is difficult to obtain a high-purity piperonal product by directly crystallizing piperonal after chemical synthesis.

[0005] The present application provides a piperonal crude product processing device, comprising a crude product storage tank, a heat exchanger, a distillation tower, a receiving tank group and a crystallization kettle connected in series in sequence;

[0006] The distillation tower and the receiving tank group are also connected to the vacuum unit respectively;

[0007] The receiving tank group includes a front fraction receiving tank and a main fraction receiving tank connected in parallel, the front fraction receiving tank and the main fraction receiving tank are respectively connected to the vacuum unit through valves; the front fraction receiving tank and the main fraction receiving tank are also respectively connected to the distillation tower through valves;

[0008] The main fraction receiving tank is also connected to the crystallization kettle;

[0009] The distillation tower is also connected to the still residue receiving tank and the steam pipeline.

[0010] Optionally, the distillation tower comprises an upper condenser and a lower tower kettle, the condenser and the tower kettle are connected through a distillation tower body; an empty high tower section is also arranged between the condenser and the distillation tower body; and multiple layers of tower plates are staggered from top to bottom in the distillation tower body;

[0011] The material output end of the heat exchanger is connected to the material input end of the distillation tower body;

[0012] The top of the condenser is connected to the vacuum unit;

[0013] A jacket is provided outside the tower kettle, and the heat exchange medium inlet of the jacket is connected to the steam pipeline, and the heat exchange medium outlet of the jacket is connected to the heat exchange medium inlet of the heat exchanger;

[0014] A liquid collecting tank is arranged on the upper part of the inner wall of the distillation tower body, and the liquid collecting tank is located between the empty high tower section and the distillation tower body, and the liquid collecting tank is respectively connected to the front fraction receiving tank and the main fraction receiving tank through valves;

[0015] The liquid collecting tank is arranged in a ring shape on the inner wall of the empty high tower section.

[0016] Optionally, a guide plate is also provided in the empty high tower section.

[0017] Optionally, the guide plate includes a guide surface and a plurality of guide grooves;

[0018] The guide surface is in the shape of a porous conical surface, the guide groove array is arranged on the bottom circumference of the guide surface, and the guide surface is connected to the inner wall of the distillation tower through the guide groove;

[0019] A circle of cofferdam is arranged on the upper surface of the guide surface near the bottom circumference, and the cofferdam is connected with the guide groove;

[0020] The guide trough is set at an angle.

[0021] Optionally, the upper surface of the guide surface is provided with guide ribs, the guide ribs are provided in one-to-one correspondence with the guide grooves, one end of the guide ribs is close to the apex of the guide surface, and the other end is close to the guide groove.

[0022] Optionally, a deep cooler is also provided at the vacuum end of the vacuum unit;

[0023] The cryogenic cooler is connected to the distillation tower and the receiving tank group respectively.

[0024] Optionally, the exhaust end of the vacuum unit is also connected to an exhaust gas treatment device;

[0025] The waste gas treatment device is an activated carbon adsorption tower or an incinerator.

[0026] The present application provides a crude piperonal processing device, which preheats a crude piperonal solution stored in a crude product storage tank by setting a heat exchanger and then inputs it into a distillation tower for distillation, and sets a vacuum unit to evacuate the distillation tower to reduce the boiling point of the material being distilled, and sets a receiving tank group to receive fractions at different temperatures, and inputs the received main fraction, i.e., piperonal, into a crystallization kettle for crystallization. The device of the present application sets a distillation tower, and after the synthesized crude piperonal is distilled and purified by the distillation tower, it is sent into a crystallization kettle for crystallization, which can effectively improve the purity of the obtained piperonal product and improve the grade of the product, thereby overcoming the disadvantage that it is difficult to obtain a high-purity piperonal product by direct crystallization after piperonal is synthesized by chemical means. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] In order to more clearly illustrate the embodiments of the present application or the technical solutions in the prior art, a brief introduction will be given below to the drawings required for use in the embodiments or the description of the prior art. Obviously, the drawings described below are some embodiments of the present application. For ordinary technicians in this field, other drawings can be obtained based on these drawings without paying any creative work.

[0028] Figure 1 A schematic diagram of a crude piperonal processing device provided in one embodiment of the present application;

[0029] Figure 2 A schematic diagram of the structure of a distillation tower provided in one embodiment of the present application;

[0030] Figure 3 A schematic diagram of the structure of a liquid collecting tank provided in an embodiment of the present application;

[0031] Figure 4 A schematic diagram of the front view of a guide plate provided in one embodiment of the present application;

[0032] Figure 5 A schematic diagram of a top view of a guide plate provided in another embodiment of the present application;

[0033] Figure 6 A schematic diagram of a crude piperonal processing device provided in another embodiment of the present application.

[0034] Description of reference numerals:

[0035] 1. Crude product storage tank; 2. Heat exchanger; 3. Distillation tower; 4. Receiving tank group; 5. Crystallization kettle; 6. Vacuum unit; 7. Steam pipeline; 30. Residue receiving tank; 31. Condenser; 32. Tower kettle; 33. Distillation tower body; 34. Empty high tower section; 35. Guide plate; 41. Fore fraction receiving tank; 42. Main fraction receiving tank; 61. Cryogenic cooler; 62. Waste gas treatment device; 341. Liquid collecting tank; 351. Guide surface; 352. Guide trough; 353. Cofferdam; 354. Guide rib. DETAILED DESCRIPTION

[0036] In order to make the purpose, technical scheme and advantages of the embodiments of the present application clearer, the technical scheme in the embodiments of the present application is clearly and completely described below. Obviously, the described embodiments are part of the embodiments of the present application, not all of the embodiments. Based on the embodiments in the present application, all other embodiments obtained by ordinary technicians in this field without creative work also fall within the scope of protection of the present application.

[0037] like Figure 1As shown, the present application provides a piperonal crude product processing device, comprising a crude product storage tank 1, a heat exchanger 2, a distillation tower 3, a receiving tank group 4 and a crystallization kettle 5 connected in series in sequence;

[0038] The distillation tower 3 and the receiving tank group 4 are also connected to the vacuum unit 6 respectively;

[0039] The receiving tank group 4 includes a front fraction receiving tank 41 and a main fraction receiving tank 42 connected in parallel, and the front fraction receiving tank 41 and the main fraction receiving tank 42 are respectively connected to the vacuum unit 6 through valves; the front fraction receiving tank 41 and the main fraction receiving tank 42 are also respectively connected to the distillation tower 3 through valves;

[0040] The main fraction receiving tank 42 is also connected to the crystallization kettle 5;

[0041] The distillation tower 3 is also connected to a still residue receiving tank 30 and a steam pipeline 7 .

[0042] When in use, the piperonal crude product solution stored in the crude product storage tank 1 is passed into the tube side of the heat exchanger 2, and is heated to a preset temperature (for example, 50-60°C) by heat exchange with the heat exchange medium in the shell side, and then enters the distillation tower 3. At this time, the valve between the front fraction receiving tank 41 and the vacuum unit 6 and the distillation tower 3 is opened, and the valve between the main fraction receiving tank 42 and the vacuum unit 6 and the distillation tower 3 is closed.

[0043] The vacuum unit 6 is used to evacuate the distillation tower 3 from the top of the tower (for example, to -80 kPa), which can reduce the boiling point of the material, making the material in the tower easier to be evaporated, and can effectively reduce the amount of heating medium used. At this time, the steam supplied by the steam pipeline 7 is used to heat the material in the tower to a preset first temperature (for example, 80-110° C.), and the material with a boiling point lower than that of piperonal, such as piperonyl ring, in the material is evaporated. When the material with a lower boiling point in the material is evaporated in a gaseous state, a gas-liquid exchange distillation process occurs on the tower plate of the distillation tower 3. The gaseous material rising to the top of the tower is condensed by the condensing device at the top of the tower, and then extracted from the corresponding extraction port, and the fore fraction with a lower boiling point is collected by the fore fraction receiving tank 41. When the temperature of the front fraction is maintained in the tower and no more fraction is distilled out, the temperature is raised to a second preset temperature (for example, 120° C.) to keep the pressure in the tower stable and unchanged. During this process, the front fraction is continuously received. When no more fraction is distilled out, the suction power of the vacuum unit 6 is adjusted (for example, several vacuum pumps are additionally turned on) to pump the pressure in the tower to a pressure (for example, -85 kPa) at which the main fraction, i.e., piperonal, can be distilled out. At the same time, the valves between the front fraction receiving tank 41 and the vacuum unit 6 and the distillation tower 3 are closed, and the valves between the main fraction receiving tank 42 and the vacuum unit 6 and the distillation tower 3 are opened. At this time, the main fraction is received by the main fraction receiving tank 42. The distillation process of the main fraction in the distillation tower 3 is the same as the distillation process of the front fraction, which will not be described in detail here.

[0044] What is received in the main fraction receiving tank 42 is high-purity piperonal (at this time, the temperature is high and the piperonal is in liquid state). The liquid piperonal in the main fraction receiving tank 42 is then transferred to the crystallization kettle 5 for crystallization. The crystallized piperonal can be subsequently separated, dried, packaged, and other operations.

[0045] After the distillation is completed, the high boiling point still residue in the distillation tower 3 is input into the still residue receiving tank 30 for collection and centralized treatment.

[0046] The present application provides a crude piperonal processing device, which includes a heat exchanger 2, a crude piperonal solution stored in a crude product storage tank 1 is preheated and then input into a distillation tower 3 for distillation, a vacuum unit 6 is provided to evacuate the distillation tower 3 to reduce the boiling point of the material being distilled, and a receiving tank group 4 is provided to receive fractions at different temperatures, and the received main fraction, i.e., piperonal, is input into a crystallization kettle 5 for crystallization. The device of the present application is provided with a distillation tower 3, and the synthesized crude piperonal is distilled and purified by the distillation tower 3, and then sent to the crystallization kettle 5 for crystallization, which can effectively improve the purity of the obtained piperonal product and improve the grade of the product, thereby overcoming the disadvantage that it is difficult to obtain a high-purity piperonal product by direct crystallization after piperonal is synthesized by chemical means.

[0047] like Figure 2 and Figure 3 As shown, optionally, the distillation tower 3 includes an upper condenser 31 and a lower tower kettle 32, and the condenser 31 and the tower kettle 32 are connected through a distillation tower body 33; an empty high tower section 34 is also arranged between the condenser 31 and the distillation tower body 33; and multiple layers of tower plates are staggered from top to bottom in the distillation tower body 33;

[0048] The material output end of the heat exchanger 2 is connected to the material input end of the distillation tower body 33;

[0049] The top of the condenser 31 is connected to the vacuum unit 6;

[0050] A jacket is provided outside the tower kettle 32, and the heat exchange medium inlet of the jacket is connected to the steam pipeline 7, and the heat exchange medium outlet of the jacket is connected to the heat exchange medium inlet of the heat exchanger 2;

[0051] A liquid collecting tank 341 is provided on the upper part of the inner wall of the distillation tower body 33. The liquid collecting tank 341 is located between the empty height tower section 34 and the distillation tower body 33. The liquid collecting tank 341 is connected to the front fraction receiving tank 41 and the main fraction receiving tank 42 through valves.

[0052] The liquid collecting tank 341 is annularly arranged on the inner wall of the hollow tower section 34 .

[0053] In the present application, when in use, the vacuum unit 6 is used to evacuate the inside of the distillation tower 3 from the condenser 31 arranged at the top of the tower (for example, to -80 kPa), which can reduce the boiling point of the material, so that the material in the tower bottom 32 is easier to be evaporated, and the amount of steam used can be effectively reduced. At the same time, circulating water is introduced into the top condenser 31, and steam is introduced into the jacket arranged outside the tower bottom 32, and the material in the tower bottom 32 is heated to a preset first temperature, for example, (80-110° C.), and the material with a boiling point lower than that of piperonal in the material is evaporated. For example, when the pepper rings are evaporated and the materials with lower boiling points in the materials are evaporated in gaseous state, a distillation process of gas-liquid exchange occurs on the tower plates of the distillation tower body 33, and the gaseous materials rising to the top of the tower go up into the tube side of the condenser 31, and the circulating water in the shell side of the condenser 31 condenses the gaseous materials into droplets that fall down. The droplets falling in the tube bundle near the outer periphery of the condenser 31 will contact the tower wall under the disturbance of the rising airflow and flow down, and enter the liquid collecting tank 341 and be discharged to the front fraction receiving tank 41 or the main fraction receiving tank 42.

[0054] like Figure 2 As shown, optionally, a guide plate 35 is further provided in the empty high tower section 34 .

[0055] In the present application, a guide plate 35 is provided to facilitate the collection and diversion of droplets dripping from the tube bundle in the central part of the condenser 31 on the guide plate 35, so that these droplets can flow into the liquid collecting tank 341 along the tower wall.

[0056] like Figure 4 As shown, optionally, the guide plate 35 includes a guide surface 351 and a plurality of guide grooves 352;

[0057] The guide surface 351 is in the shape of a porous conical surface, and the guide grooves 352 are arranged in an array on the bottom circumference of the guide surface 351, and the guide surface 351 is connected to the inner wall of the distillation tower 3 through the guide grooves 352;

[0058] A circle of cofferdam 353 is provided on the upper surface of the guide surface 351 near the bottom circumference, and the cofferdam 353 is connected to the guide groove 352;

[0059] The guide groove 352 is arranged obliquely.

[0060] When in use, the gaseous material rising to the top of the tower passes through the guide plate 35 and enters the tube side of the condenser 31. The circulating water in the shell side of the condenser 31 condenses the gaseous material into droplets and falls. The droplets falling in the tube bundle near the outer periphery of the condenser 31 will partially contact the tower wall under the disturbance of the rising airflow and flow down and then enter the collecting tank 341. The droplets near the central part of the condenser 31 will gather when they contact the conical guide surface 351 when falling. The liquid flow flows down along the guide surface 351 and is blocked and gathered by the cofferdam 353, and then flows into the guide tank 352 from the connection between the cofferdam 353 and the guide tank 352. The fractions flowing into the guide tank 352 flow out from the other end of the guide tank 352, flow down along the tower wall, and finally fall into the collecting tank 341, and then are discharged through the collecting tank 341.

[0061] One end of the guide groove 352 is connected to the lower edge of the guide surface 351, and the other end is connected to the tower wall. The guide groove 352 is inclined to facilitate guiding the converged liquid flow to flow down along the inner wall of the tower.

[0062] like Figure 5 As shown, optionally, the upper surface of the guide surface 351 is provided with guide ribs 354 , and the guide ribs 354 are provided in one-to-one correspondence with the guide grooves 352 , and one end of the guide rib 354 is close to the vertex of the guide surface 351 , and the other end is close to the guide groove 352 .

[0063] In the present application, part of the liquid condensed on the guide surface 351 flows into the guide groove 352 along the guide ribs 354 on the guide surface 351, which is convenient for collecting the liquid. The guide ribs 354 and the guide grooves 352 are arranged one by one, which is convenient for the guided liquid to flow into the guide grooves 352.

[0064] like Figure 6 As shown, optionally, a deep cooler 61 is also provided at the vacuum end of the vacuum unit 6;

[0065] The cryogenic cooler 61 is connected to the distillation tower 3 and the receiving tank group 4 respectively.

[0066] In the working process of the vacuum unit 6, it is inevitable that a small amount of gaseous materials (piperonyl ring, piperonal molecules, etc.) will be extracted from the distillation tower 3. If these gaseous materials are not processed, they will enter the vacuum equipment of the vacuum unit 6, which is easy to cause damage to the equipment. Moreover, the vacuum equipment will discharge these materials when exhausting, which will also cause environmental pollution. Therefore, a deep freezer 61 is set at the exhaust end of the vacuum unit 6, and the deep freezer 61 (using low-temperature frozen brine as a cooling medium, the temperature is -5 to -20 ° C) can be used to condense the extracted gaseous materials, and the condensed materials can be collected and recycled.

[0067] like Figure 6 As shown, optionally, the exhaust end of the vacuum unit 6 is also connected to the exhaust gas treatment device 62;

[0068] The waste gas treatment device 62 is an activated carbon adsorption tower or an incinerator.

[0069] The non-condensable gas that cannot be condensed in the gas sucked by the vacuum unit 6 is discharged by the vacuum unit 6 to the exhaust gas treatment device 62 for harmless treatment such as incineration or absorption.

[0070] A piperonal crude product processing device, the working process of which is as follows:

[0071] When in use, the piperonal crude product solution stored in the crude product storage tank 1 is passed into the tube side of the heat exchanger 2, and heat is exchanged with the heat exchange medium of the shell side (the heat exchange medium comes from the steam output from the jacket of the tower kettle 32) to raise the temperature to a preset temperature (for example, 50-60°C). The preheated solution enters the distillation tower 3 from the material inlet in the middle of the distillation tower body 33 and falls into the tower kettle 32. At this time, the valve between the front fraction receiving tank 41 and the vacuum unit 6 and the distillation tower 3 is opened, and the valve between the main fraction receiving tank 42 and the vacuum unit 6 and the distillation tower 3 is closed.

[0072] The vacuum unit 6 is used to evacuate the inside of the distillation tower 3 from the condenser 31 arranged at the top of the tower (for example, to -80 kPa), which can reduce the boiling point of the material, so that the material in the tower bottom 32 is easier to be evaporated, which can effectively reduce the use of steam. At the same time, circulating water is introduced into the top condenser 31, and steam is introduced into the jacket arranged outside the tower bottom 32 to heat the material in the tower bottom 32 to a preset first temperature, for example, (80-110° C.), and the material with a boiling point lower than that of piperonal, such as piperonyl ring, is evaporated. When the material with a lower boiling point in the material is evaporated in a gaseous state, in the distillation tower A distillation process of gas-liquid exchange occurs on the tower plate of the main body 33. The gaseous material rising to the top of the tower passes through the guide plate 35 and enters the tube side of the condenser 31. The circulating water in the shell side of the condenser 31 condenses the gaseous material into droplets and falls down. The droplets falling in the tube bundle near the outer periphery of the condenser 31 will partially contact the tower wall under the disturbance of the rising airflow and flow down and enter the liquid collecting tank 341. The droplets near the central part of the condenser 31 will gather when they contact the conical guide surface 351 when falling, and part of the liquid flow will flow into the guide groove 352 along the guide ribs 354 on the guide surface 351. Part of the liquid flow flows down along the guide surface 351 and is blocked and gathered by the cofferdam 353, and then flows into the guide groove 352 from the connection between the cofferdam 353 and the guide groove 352. The fraction flowing into the guide groove 352 flows out from the other end of the guide groove 352, flows down along the tower wall, and finally falls into the collecting groove 341, and is output from the collecting groove 341 into the front fraction receiving tank 41 to collect the front fraction with a lower boiling point. When the temperature of the tower bottom 32 for distilling the front fraction is maintained and no more fraction is distilled out, the temperature of the tower bottom 32 is increased to a second preset temperature (for example, 120° C.) to keep the pressure in the tower stable and unchanged. During this process, the front fraction is continuously received. When no more fraction is distilled out, the suction power of the vacuum unit 6 is adjusted (for example, several vacuum pumps are additionally turned on) to pump the pressure in the tower to a pressure (for example, -85 kPa) at which the main fraction, i.e., piperonal, can be distilled out. At the same time, the valve between the front fraction receiving tank 41 and the vacuum unit 6 and the distillation tower 3 is closed, and the valve between the main fraction receiving tank 42 and the vacuum unit 6 and the distillation tower 3 is opened. At this time, the main fraction is received by the main fraction receiving tank 42. The distillation process of the main fraction in the distillation tower 3 is the same as the distillation process of the front fraction, which will not be described in detail here.

[0073] What is received in the main fraction receiving tank 42 is high-purity piperonal (at this time, the temperature is high and the piperonal is in liquid state). The liquid piperonal in the main fraction receiving tank 42 is then transferred to the crystallization kettle 5 for crystallization. The crystallized piperonal can be subsequently separated, dried, packaged, and other operations.

[0074] After the distillation is completed, the high boiling point still residue in the distillation tower 3 is input into the still residue receiving tank 30 for collection and centralized treatment.

[0075] During the operation of the vacuum unit 6, a small amount of gaseous materials will inevitably be extracted from the distillation tower 3. If these gaseous materials are not processed, they will enter the vacuum equipment of the vacuum unit 6, which may easily cause damage to the equipment. In addition, the vacuum equipment will discharge these materials when exhausting, which will also cause environmental pollution. Therefore, a cryogenic refrigerator 61 is set at the exhaust end of the vacuum unit 6. The cryogenic refrigerator 61 (using low-temperature frozen brine as a cooling medium, the temperature is -5 to -20°C) can be used to condense the extracted gaseous materials. The condensed materials can be collected and recycled, and the non-condensable gases that cannot be condensed in this process are discharged by the vacuum unit 6 to the waste gas treatment device 62 for harmless treatment such as incineration or absorption.

[0076] Finally, it should be noted that the above embodiments are only used to illustrate the technical solutions of the present application, rather than to limit it. Although the present application has been described in detail with reference to the aforementioned embodiments, ordinary technicians in the field should understand that they can still modify the technical solutions recorded in the aforementioned embodiments, or replace some or all of the technical features therein with equivalents. However, these modifications or replacements do not cause the essence of the corresponding technical solutions to deviate from the scope of the technical solutions of the embodiments of the present application.

Claims

1. A piperonal crude product processing device, characterized in that: It comprises a crude product storage tank (1), a heat exchanger (2), a distillation tower (3), a receiving tank group (4) and a crystallization kettle (5) which are sequentially connected in series; The distillation tower (3) and the receiving tank group (4) are also respectively connected to a vacuum unit (6); The receiving tank group (4) comprises a front fraction receiving tank (41) and a main fraction receiving tank (42) connected in parallel, wherein the front fraction receiving tank (41) and the main fraction receiving tank (42) are respectively connected to a vacuum unit (6) via valves; the front fraction receiving tank (41) and the main fraction receiving tank (42) are also respectively connected to a distillation tower (3) via valves; The main fraction receiving tank (42) is also connected to the crystallization kettle (5); The distillation tower (3) is also connected to a still residue receiving tank (30) and a steam pipeline (7).

2. The crude piperonal processing device according to claim 1, characterized in that: The distillation tower (3) comprises an upper condenser (31) and a lower tower kettle (32), wherein the condenser (31) and the tower kettle (32) are connected via a distillation tower body (33); an empty tower section (34) is further arranged between the condenser (31) and the distillation tower body (33); and multiple layers of tower plates are arranged alternately from top to bottom in the distillation tower body (33); The material output end of the heat exchanger (2) is connected to the material input end of the distillation tower body (33); The top of the condenser (31) is connected to the vacuum unit (6); The tower kettle (32) is provided with a jacket outside, and the heat exchange medium inlet of the jacket is connected to the steam pipeline (7), and the heat exchange medium outlet of the jacket is connected to the heat exchange medium inlet of the heat exchanger (2); A liquid collecting tank (341) is provided at the upper part of the inner wall of the distillation tower body (33), and the liquid collecting tank (341) is located between the empty height tower section (34) and the distillation tower body (33). The liquid collecting tank (341) is connected to the front fraction receiving tank (41) and the main fraction receiving tank (42) through valves respectively; The liquid collecting tank (341) is arranged in an annular shape on the inner wall of the empty high tower section (34).

3. The piperonal crude product processing device according to claim 2, characterized in that: A guide plate (35) is also arranged inside the empty high tower section (34).

4. The crude piperonal processing device according to claim 3, characterized in that: The guide plate (35) comprises a guide surface (351) and a plurality of guide grooves (352); The guide surface (351) is in the shape of a porous conical surface, the guide grooves (352) are arranged in an array on the bottom circumference of the guide surface (351), and the guide surface (351) is connected to the inner wall of the distillation tower (3) through the guide grooves (352); A circle of cofferdams (353) is provided on the upper surface of the guide surface (351) near the bottom circumference, and the cofferdams (353) are connected to the guide groove (352); The guide groove (352) is arranged obliquely.

5. The crude piperonal processing device according to claim 4, characterized in that: The upper surface of the guide surface (351) is provided with a guide rib (354), and the guide rib (354) is arranged in a one-to-one correspondence with the guide groove (352), and one end of the guide rib (354) is close to the vertex of the guide surface (351), and the other end is close to the guide groove (352).

6. The crude piperonal processing device according to claim 1, characterized in that: The vacuum unit (6) is also provided with a cryogenic cooler (61) at the air extraction end; The cryogenic cooler (61) is respectively connected to the distillation tower (3) and the receiving tank group (4).

7. The crude piperonal processing device according to any one of claims 1 to 6, characterized in that: The exhaust end of the vacuum unit (6) is also connected to an exhaust gas treatment device (62); The waste gas treatment device (62) is an activated carbon adsorption tower or an incinerator.

Images