Low-energy-consumption high-concentration organic matter aqueous solution dehydration system

Abstract

The invention discloses a low-energy-consumption high-concentration organic matter water solution dehydration system, and relates to the technical field of organic matter dehydration. Comprising a liquid phase adsorption system, a first gas phase adsorption drying system, a first regeneration liquid system, a second gas phase adsorption drying system and a second regeneration liquid system, a product of the first gas-phase adsorption drying system is introduced into the heat exchanger to serve as a heat source to heat a product ethanol of the liquid-phase adsorption tower group, and a product of the second gas-phase adsorption drying system is used as a heat source to preheat a regenerated liquid of the first gas-phase adsorption drying system; a product from the liquid phase adsorption tower group is used as a heat source to preheat regeneration liquid of the first gas phase adsorption drying system and raw materials of the second gas phase adsorption drying system; according to the invention, latent heat of an intermediate product and a final product ethanol can be fully utilized, heat is fully coupled and recovered, energy consumption is reduced, deep dehydration can be realized, and product quality is improved.

Description

Technical Field

[0001] The invention relates to the technical field of organic dehydration, and in particular to a low-energy-consumption and high-concentration organic aqueous solution dehydration system. Background Art

[0002] The high-concentration organic dehydration system in the prior art has the defects of numerous equipment configurations, large equipment size, large layout site, and high one-time investment. Before entering the adsorption dryer, the raw liquid needs to be gasified and superheated, and its product needs to be liquefied. In order to make full use of the latent heat of liquefaction of organic gas, a differential pressure staggered method is usually adopted to recover heat as much as possible. However, there are still problems such as low heat utilization efficiency, high energy consumption, and high overall operating costs. In addition, the dehydration depth is not enough, the water content quality of the product is unstable, and the drying load is limited. Based on this, a low-energy consumption and high-concentration organic aqueous solution dehydration system is provided. Summary of the invention

[0003] The present invention aims to solve the technical problems of low heat utilization efficiency, high energy consumption, insufficient dehydration depth, etc. in the existing high-concentration organic aqueous solution dehydration system, and aims to provide a low-energy consumption high-concentration organic aqueous solution dehydration system, which can fully utilize the latent heat of high and low pressure gas phase adsorption products and the latent heat of the final product ethanol, not only fully couples and recovers the heat, reduces the steam consumption, reduces the energy consumption, but also can achieve deep dehydration and improve the product quality.

[0004] The present invention is achieved through the following technical solutions:

[0005] A low-energy consumption high-concentration organic aqueous solution dehydration system, comprising a liquid phase adsorption system, a first gas phase adsorption drying system, a first regeneration liquid system, a second gas phase adsorption drying system and a second regeneration liquid system;

[0006] The liquid phase adsorption system comprises a liquid phase adsorption tower group, and the product outlet of the liquid phase adsorption tower group is connected to a heat exchanger;

[0007] The first gas phase adsorption drying system comprises a first raw material preheater, a first superheater and a first adsorption drying tower group which are connected in sequence, the liquid phase outlet of the first adsorption drying tower group is connected to the first regeneration liquid system, the product outlet of the first adsorption drying tower group is connected to the heat exchanger and serves as a heat source for the heat exchanger, and the product is cooled and introduced into the liquid phase adsorption tower group as part of its raw material;

[0008] The second gas phase adsorption drying system comprises a second raw material preheater, a second superheater, a second adsorption drying tower group and a second regeneration liquid system which are connected in sequence, the liquid phase outlet of the second adsorption drying tower group is connected to the second regeneration liquid system, the product outlet of the second adsorption drying tower group is connected to the first regeneration liquid system as a heat source to preheat the first regeneration liquid, and the product is cooled and introduced into the liquid phase adsorption tower group as another part of the raw material;

[0009] Among them, the product of the liquid phase adsorption tower group is divided into two paths after being gasified by the heat exchanger. The first path is connected to the first raw material preheater, the first regeneration liquid system, and the second regeneration liquid system in sequence as its heat source, and an organic anhydrous product is obtained after cooling. The second path is used as the heat source of the second raw material preheater, and an organic anhydrous product is obtained after cooling.

[0010] Furthermore, it also includes a drainage system, which includes a drainage tower and a reboiler arranged at the bottom of the drainage tower, and the drainage tower is connected between the first raw material preheater and the first superheater.

[0011] Furthermore, the first raw material preheater includes a first raw material preheater 1 and a first raw material preheater 2 which are connected in sequence, the first raw material preheater 1 is connected to a heat exchanger, and a portion of the product of the liquid phase adsorption tower group after vaporization by the heat exchanger is passed into the first raw material preheater 1 to preheat the raw material, and the first raw material preheater 2 uses steam as a heat source.

[0012] Furthermore, the first adsorption drying tower group is also connected to a first regeneration liquid condenser group and a first regeneration vacuum system, and the regeneration liquid obtained after passing through the first regeneration liquid condenser group and the first regeneration vacuum system is introduced into the first regeneration liquid system.

[0013] Furthermore, the first regeneration liquid system includes a first regeneration liquid delivery pump and a first regeneration liquid preheater which are connected in sequence, the first regeneration liquid preheater is connected to a drainage tower, the first regeneration liquid delivery pump pumps the regeneration liquid of the first adsorption drying tower group and the first regeneration vacuum system into the first regeneration liquid preheater, and the preheated regeneration liquid is passed into the drainage tower for drainage.

[0014] Furthermore, the first regeneration liquid preheater comprises a first regeneration liquid preheater 1, a first regeneration liquid preheater 2 and a first regeneration liquid preheater 3 connected in series, the heat source end inlet of the first regeneration liquid preheater 1 is connected to the heat source end outlet of the first raw material preheater, the heat source end inlet of the first regeneration liquid preheater 2 is connected to the product outlet of the second adsorption drying tower group, and the heat source end inlet of the first regeneration liquid preheater 3 is connected to the heat source end outlet of the first superheater.

[0015] Furthermore, the second raw material preheater includes a second raw material preheater 1, a second raw material preheater 2 and a second superheater which are connected in sequence, the heat source inlet of the second raw material preheater 1 is connected to the heat exchanger, and the product of another part of the liquid phase adsorption tower group after gasification by the heat exchanger is introduced into the second raw material preheater 1 to preheat the raw material, and the second raw material preheater 2 and the second superheater use steam as the heat source.

[0016] Furthermore, the second adsorption drying tower group is also connected to a second regeneration liquid condenser group and a second regeneration vacuum system, and the regeneration liquid obtained after passing through the second regeneration liquid condenser group and the second regeneration vacuum system is introduced into the second regeneration liquid system.

[0017] Furthermore, the second regeneration liquid system includes a second regeneration liquid delivery pump and a second regeneration liquid preheater connected in sequence, the second regeneration liquid preheater is connected to the drainage tower, the second regeneration liquid delivery pump pumps the regeneration liquid of the second adsorption drying tower group and the second regeneration vacuum system into the second regeneration liquid preheater, and the preheated regeneration liquid is passed into the drainage tower for drainage.

[0018] Furthermore, the second regeneration liquid preheater includes a second regeneration liquid preheater 1 and a second regeneration liquid preheater 2 connected in series.

[0019] Compared with the prior art, the present invention has the following advantages and beneficial effects:

[0020] The system of the present invention makes full use of the latent heat of the low-pressure gas phase adsorption product by passing the low-pressure gas phase adsorption product into the heat exchanger as a heat source to heat the product ethanol of the liquid phase adsorption tower group to gasify it; makes full use of the latent heat of the high-pressure gas phase adsorption product by using the high-pressure gas phase adsorption product as a heat source to preheat the regeneration liquid of the low-pressure gas phase adsorption; makes full use of the latent heat of the product ethanol by using the product from the liquid phase adsorption tower group as a heat source to preheat the regeneration liquid of the low-pressure gas phase adsorption and the raw material of the high-pressure gas phase adsorption. Therefore, the present invention can make full use of the latent heat of the high and low pressure gas phase adsorption products and the latent heat of the final product ethanol, not only fully couples and recovers the heat, reduces the steam usage, reduces the energy consumption, but also can achieve deep dehydration and improve the product quality. BRIEF DESCRIPTION OF THE DRAWINGS

[0021] In order to more clearly illustrate the technical solutions of the exemplary embodiments of the present invention, the following briefly introduces the drawings required for use in the embodiments. It should be understood that the following drawings only illustrate certain embodiments of the present invention and should not be regarded as limiting the scope. For those of ordinary skill in the art, other relevant drawings can be obtained based on these drawings without creative work. In the drawings:

[0022] Figure 1It is a structural schematic diagram of the system of the present invention;

[0023] Marks and corresponding parts names in the attached drawings:

[0024] 1-liquid phase adsorption tower group, 2-feed pump, 3-heat exchanger, 4-first raw material preheater 1, 5-first raw material preheater 2, 6-drainage tower, 7-reboiler, 8-first superheater, 9-first adsorption drying tower group, 10-first regeneration liquid condenser group, 11-first regeneration vacuum system, 12-first regeneration liquid delivery pump, 13-first regeneration liquid preheater 1, 14-first regeneration liquid preheater 2, 15-first regeneration liquid preheater 3, 16-second raw material preheater 1, 17-second raw material preheater 2, 18-second superheater, 19-second adsorption drying tower group, 20-second regeneration liquid condenser group, 21-second regeneration vacuum system, 22-second regeneration liquid delivery pump, 23-second regeneration liquid preheater 1, 24-second regeneration liquid preheater 2, 25-first product cooler, 26-second product cooler, 27-product delivery pump, 28-wastewater cooler, 29-first raw material cooler, 30-second raw material cooler. DETAILED DESCRIPTION

[0025] In order to make the objectives, technical solutions and advantages of the present invention more clearly understood, the technical solutions in the embodiments of the present invention are clearly and completely described below in combination with the embodiments and drawings. Obviously, the schematic implementation modes of the present invention and their description are only used to explain the present invention and are not intended to limit the present invention.

[0026] The following is a detailed description of an embodiment of a low-energy consumption high-concentration organic aqueous solution dehydration system of the present invention with appropriate reference to the accompanying drawings. However, there may be cases where unnecessary detailed descriptions are omitted. For example, there may be cases where detailed descriptions and repeated descriptions of well-known matters are omitted. This is to avoid the following description from becoming unnecessarily lengthy and to facilitate the understanding of those skilled in the art.

[0027] Unless otherwise specified, all embodiments and optional embodiments of the present application can be combined with each other to form a new technical solution.

[0028] Unless otherwise specified, all technical features and optional technical features of this application can be combined with each other to form a new technical solution.

[0029] If there is no special description, the "include" and "comprising" mentioned in this application represent open-ended or closed-ended. If there is no special description, all steps of this application can be performed sequentially or randomly, preferably sequentially. The technical solution of the present invention is further described in detail below in conjunction with the embodiments.

[0030] Example 1

[0031] A low energy consumption high concentration organic aqueous solution dehydration system, such as Figure 1 As shown, it includes a liquid phase adsorption system, a first gas phase adsorption drying system, a first regeneration liquid system, a second gas phase adsorption drying system and a second regeneration liquid system;

[0032] The liquid phase adsorption system comprises a liquid phase adsorption tower group 1, and the product outlet of the liquid phase adsorption tower group 1 is connected to a heat exchanger 3;

[0033] The first gas phase adsorption drying system comprises a first raw material preheater, a first superheater 8 and a first adsorption drying tower group 9 which are connected in sequence, the liquid phase outlet of the first adsorption drying tower group 9 is connected to the first regeneration liquid system, the product outlet of the first adsorption drying tower group 9 is connected to the heat exchanger 3 and serves as a heat source for the heat exchanger 3, and the product is cooled and introduced into the liquid phase adsorption tower group 1 as part of its raw material;

[0034] The second gas phase adsorption drying system comprises a second raw material preheater, a second superheater 18, a second adsorption drying tower group 19 and a second regeneration liquid system which are connected in sequence. The liquid phase outlet of the second adsorption drying tower group 19 is connected to the second regeneration liquid system. The product outlet of the second adsorption drying tower group 19 is connected to the first regeneration liquid system as a heat source to preheat the first regeneration liquid. After the product is cooled, it is introduced into the liquid phase adsorption tower group 1 as another part of its raw material.

[0035] Among them, the product of the liquid phase adsorption tower group 1 is divided into two paths after being gasified by the heat exchanger 3. The first path is connected to the first raw material preheater, the first regeneration liquid system, and the second regeneration liquid system in sequence as its heat source, and an organic anhydrous product is obtained after cooling. The second path is used as the heat source of the second raw material preheater, and an organic anhydrous product is obtained after cooling.

[0036] It should be noted that the first adsorption drying tower group 9 / the second adsorption drying tower group 19 is composed of two groups, each group of 2 or more adsorption towers and program-controlled valves with regulating functions, and its working process is automatically carried out in accordance with the set steps. Qualified ethanol vapor enters the adsorption tower through the program-controlled valve at the entrance of the adsorption tower for dehydration (only one tower is adsorbing in each period). The liquid phase adsorption tower group 1 is composed of multiple adsorption towers and program-controlled valves with regulating functions, and its working process is automatically carried out in accordance with the set steps. Qualified ethanol enters the adsorption tower through the program-controlled valve at the entrance of the adsorption tower for dehydration (there is a tower adsorbing in each period, and the tower is being regenerated). The dehydrated product (water content ≤ 0.007%) is sent out of the boundary area to downstream users.

[0037] In the dehydration system of the present invention, ethanol deep dehydration is used as an example to explain in detail. The ethanol liquid with an ethanol content of 95% (w / w) from the main pipe is divided into two paths:

[0038] One path is that the raw liquid is mixed with the dilute phase light wine of the downstream liquid phase adsorption tower group 1, and then vaporized by the second raw material preheater. After being overheated by the second superheater 18, the water-containing ethanol vapor first enters the second adsorption drying tower group 19 (high-pressure gas phase adsorption) for dehydration. The product of the high-pressure gas phase adsorption is used as a heat source to preheat the dilute phase light wine of the first regeneration liquid system, and then cooled to room temperature liquid phase intermediate product ethanol by the second raw material cooler 30, as part of the raw material of the downstream liquid phase adsorption tower group 1, and the intermediate product ethanol is sent to the liquid phase adsorption tower group 1 through the feed pump 2.

[0039] Another path is that the raw material liquid is preheated by the first raw material preheater, and then enters the first adsorption drying tower group 9 (low-pressure gas phase adsorption) after being overheated by the first superheater 8. The product is passed into the heat exchanger 3 as a heat source to heat the product ethanol of the liquid phase adsorption tower group 1 to vaporize it. The product from the low-pressure gas phase adsorption is cooled and then cooled to room temperature liquid phase intermediate product ethanol by the first raw material cooler 29. As another part of the raw material of the downstream liquid phase adsorption tower group 1, the intermediate product ethanol is sent to the liquid phase adsorption tower group 1 through the feed pump 2.

[0040] The product ethanol from the liquid phase adsorption tower group 1 is also divided into two paths after being vaporized by the heat exchanger 3. The heat source for vaporization of the heat exchanger 3 comes from the product of the first adsorption drying tower group 9.

[0041] One path is that the product coming out of the liquid phase adsorption tower group 1 is used as a heat source for low-pressure gas phase dehydration after being vaporized, specifically as a heat source for the first raw material preheater. After heating part of the raw material liquid, it is used as a heat source to preheat the dilute phase light wine in the first regeneration liquid system, and then as a heat source to preheat the dilute phase light wine in the second regeneration liquid system. Finally, after being cooled by the first product cooler 25, it is sent to the final product tank for temporary storage through the product delivery pump 27.

[0042] Another path is that the product from the liquid phase adsorption tower group 1 is used as the heat source of the second raw material preheater after being vaporized, and then cooled by the second product cooler 26, and then sent to the final product tank for temporary storage through the product delivery pump 27.

[0043] The water content of the ethanol product after dehydration by the system of the present invention is 50 ppm, and the steam consumption is reduced to 0.44 tons / ton of product.

[0044] It can be seen that the system of the present invention makes full use of the latent heat of the low-pressure gas phase adsorption product by passing the low-pressure gas phase adsorption product into the heat exchanger 3 as a heat source to heat the product ethanol of the liquid phase adsorption tower group 1 to vaporize it; the high-pressure gas phase adsorption product is used as a heat source to preheat the regeneration liquid of the low-pressure gas phase adsorption, thereby fully utilizing the latent heat of the high-pressure gas phase adsorption product; the product coming out of the liquid phase adsorption tower group 1 is used as a heat source to preheat the regeneration liquid of the low-pressure gas phase adsorption and the raw material of the high-pressure gas phase adsorption, so that the latent heat of the product ethanol can be fully utilized. Therefore, the present invention can fully utilize the latent heat of the high and low pressure gas phase adsorption products and the latent heat of the final product ethanol, not only fully couples and recovers the heat, reduces the steam usage, reduces the energy consumption, but also can achieve deep dehydration and improve the product quality.

[0045] In one or more specific embodiments of the present invention, a drainage system is also included, the drainage system includes a drainage tower 6 and a reboiler 7 arranged at the bottom of the drainage tower 6, and the drainage tower 6 is connected between the first raw material preheater and the first superheater 8. A portion of the raw material liquid enters the top of the drainage tower 6 after being preheated by the first raw material preheater as a reflux liquid, and the dilute phase light wine of the first adsorption drying tower group 9 and the second adsorption drying tower group 19 also enters the drainage tower 6 after being preheated. The drainage tower 6 discharges the water that needs to be discharged from the high and low pressure gas phase dehydrated light wine liquid, and is cooled by the wastewater cooler 28 and then discharged from the entire system. The gas phase ethanol discharged from the top of the drainage tower 6 enters the first superheater 8 for superheating and then passes into the first adsorption drying tower group 9.

[0046] In one or more specific embodiments of the present invention, the first raw material preheater includes a first raw material preheater 4 and a first raw material preheater 2 5 which are connected in sequence, the first raw material preheater 4 is connected to the heat exchanger 3, and a portion of the product of the liquid phase adsorption tower group 1 after vaporization by the heat exchanger 3 is passed into the first raw material preheater 4 to preheat the raw material, and the first raw material preheater 2 5 uses steam as a heat source to preheat the raw material.

[0047] The first adsorption drying tower group 9 is also connected to a first regeneration liquid condenser group 10 and a first regeneration vacuum system 11, and the regeneration liquid obtained after passing through the first regeneration liquid condenser group 10 and the first regeneration vacuum system 11 is introduced into the first regeneration liquid system.

[0048] The first regeneration liquid system includes a first regeneration liquid delivery pump 12 and a first regeneration liquid preheater connected in sequence. The first regeneration liquid preheater is connected to the drainage tower 6. The first regeneration liquid delivery pump 12 pumps the regeneration liquid from the first adsorption drying tower group 9 and the first regeneration vacuum system 11 into the first regeneration liquid preheater, and the preheated regeneration liquid enters the drainage tower 6 for drainage.

[0049] The first regeneration liquid preheater comprises a first regeneration liquid preheater 13, a first regeneration liquid preheater 14 and a first regeneration liquid preheater 15 connected in series.

[0050] Specifically, the heat source end inlet of the first regeneration liquid preheater 13 is connected to the heat source end outlet of the first raw material preheater, specifically, the heat source end inlet of the first regeneration liquid preheater 13 is connected to the heat source end outlet of the first raw material preheater 4, and the heat source end outlet of the first regeneration liquid preheater 13 is connected to the heat source end inlet of the second regeneration liquid preheater 23, that is, the product ethanol of the liquid phase adsorption tower group 1 is used as the heat source of the first raw material preheater 4, and then as the heat source of the first regeneration liquid preheater 13, and then as the heat source of the second regeneration liquid preheater 23, which fully utilizes the latent heat of the product ethanol, fully recovers the heat, and at the same time realizes the cooling of the product ethanol, reducing the use of cooling devices and cold sources.

[0051] The heat source inlet of the first regeneration liquid preheater 14 is connected to the product outlet of the second adsorption drying tower group 19. It should be noted that before the product of the second adsorption drying tower group 19 is used as the heat source of the reboiler 7 at the bottom of the drainage tower 6, it can fully recover the latent heat of the high-pressure gas-phase adsorption product, thereby cooling the high-pressure gas-phase adsorption product and reducing the load of the subsequent second raw material cooler 30.

[0052] The heat source inlet of the first regeneration liquid preheater three 15 is connected to the heat source outlet of the first superheater 8, that is, the heat source entering the first regeneration liquid preheater three 15 is the steam that has been used by the first superheater 8, and the waste heat of the steam is fully utilized.

[0053] Therefore, in the dehydration system of the present invention, the heat sources of the first regeneration liquid preheater 13, the first regeneration liquid preheater 2 14 and the first regeneration liquid preheater 3 15 all come from the heat sources that have been used by other equipment, and the residual heat of the heat sources is fully recovered and utilized, and no new steam is used as the heat source, thereby reducing the use of steam and greatly reducing energy consumption.

[0054] In one or more specific embodiments of the present invention, the second raw material preheater includes a second raw material preheater 16, a second raw material preheater 17 and a second superheater 18 which are connected in sequence, and the heat source inlet of the second raw material preheater 16 is connected to the heat exchanger 3, and another part of the product of the liquid phase adsorption tower group 1 after being vaporized by the heat exchanger 3 (a part of it is passed into the first raw material preheater 4 to preheat the raw material) is passed into the second raw material preheater 16 to preheat the raw material, and the second raw material preheater 17 and the second superheater 18 use steam as a heat source.

[0055] The preheating of the raw materials uses the product ethanol of the liquid phase adsorption tower group 1 as the heat source, which fully utilizes the latent heat of the product ethanol. In this way, the amount of steam required for preheating the raw materials is significantly reduced, effectively reducing energy consumption.

[0056] The second adsorption drying tower group 19 is also connected to a second regeneration liquid condenser group 20 and a second regeneration vacuum system 21, and the regeneration liquid obtained after passing through the second regeneration liquid condenser group 20 and the second regeneration vacuum system 21 is introduced into the second regeneration liquid system.

[0057] The second regeneration liquid system includes a second regeneration liquid delivery pump 22 and a second regeneration liquid preheater connected in sequence. The second regeneration liquid preheater is connected to the drainage tower 6. The second regeneration liquid delivery pump 22 pumps the regeneration liquid of the second adsorption drying tower group 19 and the second regeneration vacuum system 21 into the second regeneration liquid preheater. The preheated regeneration liquid is passed into the drainage tower 6 for drainage.

[0058] The second regeneration liquid preheater includes a second regeneration liquid preheater 1 23 and a second regeneration liquid preheater 2 24 connected in series. Specifically, the heat source inlet of the second regeneration liquid preheater 1 23 is connected to the heat source outlet of the first regeneration liquid preheater 1 13, so that the heat source of the second regeneration liquid preheater 1 23 comes from the heat source after the first regeneration liquid preheater 1 13 is used, and the residual heat of the heat source can be fully utilized; the heat source inlet of the second regeneration liquid preheater 2 24 is connected to the heat source outlet of the second raw material preheater 2 17, so that the heat source of the second regeneration liquid preheater 2 24 comes from the steam after the second raw material preheater 2 17 is used, and the residual heat of the steam source can be fully utilized.

[0059] Finally, it should be noted that the above specific embodiments are only used to explain in detail the purpose, technical solutions and beneficial effects of the present invention. It should be understood that the above description is only a specific implementation method of the present invention and is not used to limit the protection scope of the present invention. Although the present invention is described in detail with reference to the above specific embodiments, ordinary technicians in this field should understand that it is still possible to modify the technical solutions recorded in the above embodiments, or to replace or improve some or all of the technical features therein. These modifications, equivalent replacements and improvements do not make the essence of the corresponding technical solutions deviate from the scope of the technical solutions of the embodiments of the present invention, and they should all be included in the scope of the claims and description of the present invention.

Claims

1. A low energy consumption and high concentration organic aqueous solution dehydration system, characterized in that: It includes a liquid phase adsorption system, a first gas phase adsorption drying system, a first regeneration liquid system, a second gas phase adsorption drying system and a second regeneration liquid system; The liquid phase adsorption system comprises a liquid phase adsorption tower group (1), and a product outlet of the liquid phase adsorption tower group (1) is connected to a heat exchanger (3); The first gas phase adsorption drying system comprises a first raw material preheater, a first superheater (8) and a first adsorption drying tower group (9) which are connected in sequence, the liquid phase outlet of the first adsorption drying tower group (9) is connected to the first regeneration liquid system, the product outlet of the first adsorption drying tower group (9) is connected to the heat exchanger (3) and serves as a heat source for the heat exchanger (3), and the product is cooled and introduced into the liquid phase adsorption tower group (1) as part of its raw material; The second gas phase adsorption drying system comprises a second raw material preheater, a second superheater (18), a second adsorption drying tower group (19) and a second regeneration liquid system which are connected in sequence, the liquid phase outlet of the second adsorption drying tower group (19) is connected to the second regeneration liquid system, the product outlet of the second adsorption drying tower group (19) is connected to the first regeneration liquid system as a heat source to preheat the first regeneration liquid, and the product is introduced into the liquid phase adsorption tower group (1) as another part of the raw material after cooling down; The product of the liquid phase adsorption tower group (1) is divided into two paths after being gasified by the heat exchanger (3). The first path is connected to the first raw material preheater, the first regeneration liquid system, and the second regeneration liquid system in sequence as its heat source, and an organic anhydrous product is obtained after cooling. The second path is used as the heat source of the second raw material preheater, and an organic anhydrous product is obtained after cooling.

2. A low-energy consumption, high-concentration organic aqueous solution dehydration system according to claim 1, characterized in that: It also includes a drainage system, which includes a drainage tower (6) and a reboiler (7) arranged at the bottom of the drainage tower (6), and the drainage tower (6) is connected between the first raw material preheater and the first superheater (8).

3. A low-energy consumption, high-concentration organic aqueous solution dehydration system according to claim 1, characterized in that: The first raw material preheater comprises a first raw material preheater 1 (4) and a first raw material preheater 2 (5) which are connected in sequence. The first raw material preheater 1 (4) is connected to the heat exchanger (3). A portion of the product of the liquid phase adsorption tower group (1) which has been vaporized by the heat exchanger (3) is introduced into the first raw material preheater 1 (4) to preheat the raw material. The first raw material preheater 2 (5) uses steam as a heat source.

4. A low-energy consumption high-concentration organic aqueous solution dehydration system according to claim 1, characterized in that: The first adsorption drying tower group (9) is also connected to a first regeneration liquid condenser group (10) and a first regeneration vacuum system (11), and the regeneration liquid obtained after passing through the first regeneration liquid condenser group (10) and the first regeneration vacuum system (11) is introduced into the first regeneration liquid system.

5. A low-energy consumption high-concentration organic aqueous solution dehydration system according to claim 1, characterized in that: The first regeneration liquid system comprises a first regeneration liquid delivery pump (12) and a first regeneration liquid preheater which are connected in sequence. The first regeneration liquid preheater is connected to a drainage tower (6). The first regeneration liquid delivery pump (12) pumps the regeneration liquid of the first adsorption drying tower group (9) and the first regeneration vacuum system (11) into the first regeneration liquid preheater. The preheated regeneration liquid is passed into the drainage tower (6) for drainage.

6. A low-energy consumption high-concentration organic aqueous solution dehydration system according to claim 5, characterized in that: The first regeneration liquid preheater comprises a first regeneration liquid preheater one (13), a first regeneration liquid preheater two (14) and a first regeneration liquid preheater three (15) connected in series, the heat source end inlet of the first regeneration liquid preheater one (13) is connected to the heat source end outlet of the first raw material preheater, the heat source end inlet of the first regeneration liquid preheater two (14) is connected to the product outlet of the second adsorption drying tower group (19), and the heat source end inlet of the first regeneration liquid preheater three (15) is connected to the heat source end outlet of the first superheater (8).

7. A low-energy consumption, high-concentration organic aqueous solution dehydration system according to claim 1, characterized in that: The second raw material preheater comprises a second raw material preheater 1 (16), a second raw material preheater 2 (17) and a second superheater (18) which are connected in sequence. The heat source inlet of the second raw material preheater 1 (16) is connected to the heat exchanger (3). Another part of the product of the liquid phase adsorption tower group (1) after being vaporized by the heat exchanger (3) is introduced into the second raw material preheater 1 (16) to preheat the raw material. The second raw material preheater 2 (17) and the second superheater (18) use steam as a heat source.

8. A low-energy consumption high-concentration organic aqueous solution dehydration system according to claim 1, characterized in that: The second adsorption drying tower group (19) is also connected to a second regeneration liquid condenser group (20) and a second regeneration vacuum system (21), and the regeneration liquid obtained after passing through the second regeneration liquid condenser group (20) and the second regeneration vacuum system (21) is introduced into the second regeneration liquid system.

9. A low-energy consumption, high-concentration organic aqueous solution dehydration system according to claim 1, characterized in that: The second regeneration liquid system comprises a second regeneration liquid delivery pump (22) and a second regeneration liquid preheater which are connected in sequence. The second regeneration liquid preheater is connected to a drainage tower (6). The second regeneration liquid delivery pump (22) pumps the regeneration liquid of the second adsorption drying tower group (19) and the second regeneration vacuum system (21) into the second regeneration liquid preheater. The preheated regeneration liquid is passed into the drainage tower (6) for drainage.

10. A low-energy consumption, high-concentration organic aqueous solution dehydration system according to claim 9, characterized in that: The second regeneration liquid preheater comprises a second regeneration liquid preheater one (23) and a second regeneration liquid preheater two (24) connected in series.

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