CN219848208U

CN219848208U - High-efficiency energy-saving high-boiling-point lifting system concentration device

Info

Publication number: CN219848208U
Application number: CN202320167394.4U
Authority: CN
Inventors: 李丽; 张建勇
Original assignee: Shanghai Changliuyuan Chemical Technology Co ltd
Current assignee: Shanghai Changliuyuan Chemical Technology Co ltd
Priority date: 2023-01-29
Filing date: 2023-01-29
Publication date: 2023-10-20
Anticipated expiration: 2033-01-29

Abstract

The utility model belongs to the technical field of separation and purification of chemical substances, and particularly relates to an efficient and energy-saving device for concentrating a high-boiling-point lifting system. The utility model provides a high-efficiency energy-saving high-boiling-point lifting system concentrating device aiming at the problems of low concentrating efficiency, large entrainment and high energy consumption in the prior art, which comprises a rectifying system and a reboiling system connected to the rectifying system, wherein a feed inlet is communicated with the rectifying system, the device also comprises a secondary preheater, two ends of the secondary preheater are respectively communicated with a cooler and a secondary condensate pump, one end of the cooler, which is far away from the secondary preheater, is connected with the top of the rectifying system, and one end of the secondary condensate pump, which is far away from the secondary preheater, is communicated with the bottom of the rectifying system through the secondary condensate water tank. The utility model realizes the concentration of a high boiling point lifting system in a mode of using an MVR rectifying system or combining MVR evaporation and MVR rectification, and flexibly matches with a process route, thereby achieving the purposes of reducing the running power consumption, reducing the loss rate and improving the concentration efficiency, and further reducing the cost of products.

Description

High-efficiency energy-saving high-boiling-point lifting system concentration device

Technical Field

The utility model belongs to the technical field of separation and purification of chemical substances, and particularly relates to an efficient and energy-saving device for concentrating a high-boiling-point lifting system.

Background

After dissolution of a part of the inorganic salts or organics into water, the newly formed solution will have a boiling point higher than the boiling point of water, i.e. higher than 100 ℃. For example, the boiling temperature of saturated sodium chloride brine is 108 ℃, and the difference between these 8 ℃ is the boiling point rise at normal pressure of saturated sodium chloride aqueous solution. The utility model aims to provide a concentration device aiming at a high-boiling-point ascending system. Caprolactam is taken as an example, and is an important organic chemical raw material, mainly used for producing PA6 slices, and 95% of caprolactam in 2022 is used for producing PA6 slices, and can be further processed to produce nylon 6 resin, engineering plastics, medical intermediates and the like, so that the caprolactam has wide application in the fields of electronic industry, automobile processing, ships, industrial machinery, aerospace and the like.

At present, the caprolactam concentration process is mainly applied to the following two processes:

1. cyclohexanone ammoximation process: the finished caprolactam is obtained through the procedures of extraction, back extraction, ion exchange, hydrogenation, evaporation concentration, distillation and the like. It is usually concentrated from a 30% caprolactame-containing aqueous solution to 90% caprolactam-containing.

2. The caprolactam recovery process after polyester: and (3) after granulating the slices, carrying out hot water countercurrent extraction on the slices until the oligomer content in the slices meets the spinning requirement, and evaporating after obtaining an extract liquid to obtain caprolactam concentrate. Typically from a 10% aqueous solution containing caprolactam to 70% caprolactam.

The concentration of caprolactam obtained in the two processes is low, so that concentration is an unavoidable process, and concentration efficiency, loss rate and operation energy consumption become key to influence the cost of caprolactam products.

The current common treatment method is as follows:

CN106039749A, a device and a process for concentrating and recycling caprolactam water solution: the process is to remove the water in the material by evaporating and absorbing MVR (Mechanical vapor recompression) in the caprolactam concentration process. The vapor compressor is operated by electric energy to heat the vaporized gas and return the vaporized gas to the heater housing of the evaporator as a heat source. The process can effectively reduce steam consumption.

However, any one gas-liquid separation in the evaporation concentration process is actually a flash evaporation process, and the gas-liquid phase equilibrium data of caprolactam show that the caprolactam concentration in the gas phase is very low under the same pressure condition when the caprolactam concentration is low; however, as the concentration proceeds, the concentration of caprolactam in the gas phase is high when the concentration of caprolactam is high. Caprolactam entering the gas phase also enters the condensate along with the condensation of water vapor, resulting in loss of caprolactam product. Although in this process, a multi-layer tray type separator is used for spray absorption, these devices have low absorption efficiency and have very limited effect of reducing the entrainment of caprolactam in the gas phase.

The absorbent is condensed water with caprolactam concentration of about 0-1% by mass, although the absorbent is sourced from an evaporation system, the absorbent with low concentration is added into a multi-layer tray type separator, after the absorption process, the concentration of the absorbent is increased, and the material flows into an evaporation unit to be concentrated together with the material; the introduction of the extra absorbent brings extra load to the evaporation unit, namely when the original evaporation capacity is 100t/h, the evaporation capacity is more than 100t/h due to the circulation of the absorbent, and the steam capacity entering the compressor is also increased; the additional absorbent forces the area of the evaporator to be correspondingly increased, the work of the compressor to be increased, and the equipment investment and the energy consumption are increased.

In addition, in the MVR evaporation concentration process, caprolactam carried in the gas phase is compressed by a compressor after passing through an absorption unit with low absorption efficiency and enters a heater shell, and in the water vapor condensation process, caprolactam with higher concentration in the gas phase can be accumulated in a local area outside a tube array to form a gas dense area which is relatively difficult to condense; this phenomenon can seriously affect the heat transfer coefficient of the heat exchanger, thereby affecting the concentration efficiency; even if the operating conditions are adjusted, caprolactam with higher concentration in the gas phase is condensed, the bubble dew point temperature difference formed by the component is higher, and the effective heat transfer temperature difference of evaporation is correspondingly reduced.

Therefore, how to solve the problems of low concentration efficiency, large entrainment and high energy consumption in the prior art is a technical problem that needs to be solved by those skilled in the art.

Disclosure of Invention

The utility model aims to solve the problems and provide an efficient and energy-saving device for concentrating a high-boiling-point rising system.

In order to achieve the above purpose, the present utility model adopts the following technical scheme:

the utility model provides a concentrated device of high boiling point system that energy-efficient rises, includes rectification system and the reboiling system of connection on rectification system, and the feed inlet is linked together with rectification system, still includes the second grade pre-heater that is used for taking place heat exchange that sets up between feed inlet and rectification system, the both ends of second grade pre-heater are linked together with cooler and second grade condensate pump respectively, the one end that the second grade pre-heater was kept away from to the cooler links to each other with rectification system top, the one end that the second grade condensate pump was kept away from to the second grade pre-heater links to each other with rectification system's reboiler through second grade condensate water tank. Preferably, the condensate reflux ratio of the rectification system is 0-50.

Only heat exchange occurs between the raw material and the condensed water in the secondary preheater, and the raw material and the condensed water are not mutually contacted or mixed in the secondary preheater. In the primary preheater described below, only heat exchange also occurs between the raw material and the condensed water.

In the device for concentrating the high-boiling-point lifting system with high efficiency and energy conservation, the rectification system comprises a rectification tower and compressors connected to the top of the rectification tower and used for compressing steam, the coolers are communicated with the top of the rectification tower, one ends of the compressors, far away from the rectification tower, are communicated with the reboiling system, and the compressors are arranged in one-to-one correspondence with the reboiling system.

In the device for concentrating the high-boiling point rising system with high efficiency and energy saving, at least one reboiling system is arranged, and the reboiling system comprises a reboiler and a tower bottom circulating pump which are communicated with each other.

In the device for concentrating the high-boiling point rising system with high efficiency and energy conservation, at least one reboiling system is arranged, one end of the reboiler is communicated with the middle part or the lower section of the rectification system, and the tower bottom circulating pump is communicated with the middle part or the bottom of the rectification system.

In the high-efficiency energy-saving high-boiling point lifting system concentrating device, the rectifying tower is one or a combination of a plurality of plate towers and fillers; the reboiler is one or a combination of more of a kettle type reboiler, a siphon type reboiler and a falling film type reboiler.

In the high-efficiency energy-saving high-boiling point system concentration device, at least one evaporation system can be additionally arranged between the feed inlet and the secondary preheater, the evaporation system is communicated with the secondary preheater through a transfer pump, and the feed inlet is communicated with the evaporation system through the primary preheater. The evaporation system can be one or a combination of a falling film evaporation effect body, a rising film evaporation effect body and a forced circulation evaporation effect body.

In the high-efficiency and energy-saving device for concentrating the high-boiling-point ascending system, the evaporation system comprises a heater and a separator which are communicated with each other, a liquid outlet of the separator is communicated with the material transferring pump, a gas outlet of the separator is communicated with the heater through a rectifying tower and a compressor in sequence, and the primary preheater is communicated with the top of the heater. The scheme that the gas outlet of the separator is communicated with the heater through the rectifying tower and the secondary compressor sequentially is that the evaporating system and the rectifying system share one compressor.

In the high-efficiency and energy-saving device for concentrating the high-boiling-point ascending system, one end of the primary preheater is communicated with the top of the heater, the other end of the primary preheater is communicated with the primary condensate pump, and one end of the primary condensate pump, which is far away from the primary preheater, is connected with the heater through the primary condensate water tank.

In the high-efficiency energy-saving high-boiling point system concentration device, the heater is a tubular heater and/or a plate heater.

In the high-efficiency energy-saving high-boiling point system concentration device, at least one evaporation system is arranged, and at least one evaporation system is connected in series or in parallel. For example, two adjacent evaporation systems may be arranged, wherein the material output port of the next evaporation system is connected with the raw material input port of the previous evaporation system, the steam input port of the next evaporation system is connected with the steam output port of the previous evaporation system, or the steam output ports of more than two evaporation systems are combined into a total steam output port connected to the inlet of the compressor.

Compared with the prior art, the utility model has the advantages that:

1. the utility model realizes the concentration and purification process of caprolactam with relatively higher feeding concentration in a MVR rectification mode. The water quantity to be separated in the process is smaller, the caprolactam entrainment quantity in the gas phase balanced with the liquid phase is increased rapidly along with the increase of the concentration of the liquid phase, at the moment, the higher-separation-precision rectification process is adopted, so that caprolactam entrainment in the water vapor at the top of the tower is less than 0.05% (wt%), the non-condensable gas quantity generated after the water vapor enters the reboiler is less, the influence of the non-condensable gas on the heat transfer coefficient is reduced, the heat transfer efficiency of the reboiler is not influenced, and the later concentration of the caprolactam is more ensured; and no additional absorption liquid is needed to be introduced, and no additional load is added to the evaporation process at the front end.

2. According to the utility model, an MVR evaporation system can be additionally arranged before MVR rectification, and the MVR evaporation system is utilized to initially concentrate raw materials, namely, the working condition of low feeding concentration is adopted. The evaporation water quantity is large in the stage, the MVR evaporation concentration process is adopted, the boiling point of the material in the low concentration stage is low, the temperature rise of the used compressor is small, and the running electricity consumption is low; meanwhile, caprolactam carried in the water vapor is less than 0.01% (wt%) and the water vapor has less non-condensable gas generated after entering the evaporation system, has less influence on heat transfer coefficient and ensures the heat transfer efficiency of evaporation.

3. According to the utility model, the MVR evaporation system and the MVR rectification system are organically combined, so that the compressor can be utilized to the greatest extent to apply work, the low-pressure water vapor is compressed and the pressure and temperature are increased to be higher-pressure water vapor which can be used as a heat source, namely, the low-grade vapor is increased to be high-grade vapor, a small amount of electricity is used for recycling a large amount of secondary vapor, and compared with the situation that fresh vapor is fully or partially used as the heat source, the steam consumption is saved; meanwhile, the condenser of the evaporator and cooling water used for the top condenser of the rectifying tower are omitted. The MVR evaporation system and the MVR rectification system are organically combined to exert respective advantages, so that the concentration efficiency of caprolactam is ensured and the loss rate of caprolactam is reduced compared with a multi-effect evaporation process or MVR evaporation+multi-effect evaporation process or MVR evaporation process adopted in the prior art; as the concentration process is carried out step by step, the running power consumption is reduced, and the cost of caprolactam is reduced.

Drawings

Fig. 1 is a schematic structural view of embodiment 1;

fig. 2 is a schematic structural view of embodiment 2;

FIG. 3 is a schematic structural view of embodiment 3;

in the figure: the device comprises a primary preheater 1, a primary condensate water tank 2, a heater 3, a separator 4, a secondary preheater 6, a cooler 7, a secondary condensate water tank 8, a rectifying tower 9, a compressor 10, a reboiler 11, a primary condensate water pump 12, a circulating pump 13, a material transferring pump 14, a secondary condensate water pump 15, a tower bottom circulating pump 16, a rectifying system 17, a reboiling system 18, a feed inlet 19 and an evaporating system 20.

Detailed Description

The utility model will be described in further detail with reference to the drawings and the detailed description.

Example 1

The embodiment provides a high-efficiency energy-saving device for concentrating a high-boiling-point lifting system. In this embodiment, the concentration process of caprolactam is taken as an example, and besides caprolactam, various organic aqueous solutions can be concentrated by using the device, for example, DMF aqueous solution, DMA aqueous solution, DMAC aqueous solution, DMSO aqueous solution, etc. As shown in fig. 1, this embodiment includes an evaporation system 20 and a rectification system 17. Specifically, an evaporation system 20 with a compressor connected thereto; the evaporation system 20 is an evaporation device comprising a heater 3 and a separator 4; the rectification system 17 comprises a rectification tower 9, a reboiler 11 and a compressor 10, wherein the compressor connected with the evaporation system 20 is the compressor 10 in the rectification system 17, i.e. the evaporation system 20 and the rectification system 17 share one compressor.

The evaporation system 20 is further provided with a raw material input port, a material output port, a steam input port, a steam output port, a condensed water output port and other communication ports for conveying materials, steam and condensed water, and arrows shown in fig. 1 indicate the flow direction of the materials, steam or condensed water.

The raw material input port, i.e. the feed port 19, is connected to the primary preheater 1.

The heater 3 may be a tube heater, a plate heater or other heaters commonly used in the art, but in this embodiment it is preferred that the heater 3 is a tube heater.

The primary preheater 1 extracts condensed water output by the evaporation system 20 from a corresponding condensed water output port through the primary condensed water pump 12, exchanges heat between the condensed water and caprolactam solution to be input into the evaporation system 20, and preheats the caprolactam solution.

The steam outlet is connected to the compressor 10, and pressurizes the steam and inputs the steam into the steam inlet.

The intermediate material output port is connected with the secondary preheater 6 through a pipeline provided with a material transfer pump 14, and intermediate materials are conveyed into a rectification system 17 through the material transfer pump 14.

The rectification system 17 is also provided with a middle material input port, a concentrated material output port, a condensed water output port and other communication ports for conveying materials, steam and condensed water.

The intermediate material inlet is connected with the secondary preheater 6.

The top vapor of the rectifying column 9 included in the rectifying system 17 enters the compressor 10, pressurizes the vapor, and is fed to the reboiler 11.

The rectifying system 17 may include a rectifying column 9 which may be a tray column, a packed column or other rectifying columns commonly used in the art, but in this embodiment, it is preferable that the rectifying column 9 is a tray column.

The secondary preheater 6 extracts condensed water output by the rectification system 17 from a corresponding condensed water output port through the secondary condensed water pump 15, exchanges heat between the condensed water and intermediate materials to be input into the rectification system 17, and preheats the intermediate materials; the condensate water is cooled by the mol reflux ratio of 2 to the cooler 7 and then is sent to the top of the rectifying tower 9 to be used as top reflux liquid.

In practical application, intermediate materials input into the rectifying system 17 enter from the middle part of the rectifying tower 9 and flow downwards from top to bottom; meanwhile, the gas phase generated by the reboiler 11 enters the bottom of the rectifying tower 9 and flows from bottom to top to generate mass transfer and heat transfer with the intermediate material on a tower plate of the rectifying tower 9, so that moisture in the intermediate material is taken away, and the intermediate material is separated from the moisture.

In practical application, the bottom of the rectifying tower 9 is provided with a bottom circulating pump 16.

The condensed water output port of the evaporation system 20 is connected with the primary condensed water tank 2; the condensate water outlet of the rectifying system 17 is connected with the secondary condensate water tank 8; the primary condensate water tank 2 is connected with the primary preheater 1 through a primary condensate water pump 12; the secondary condensate water tank 8 is connected with the secondary preheater 6 through a secondary condensate water pump 15.

Example 2

The embodiment provides a high-efficiency energy-saving device for concentrating a high-boiling-point lifting system. In this embodiment, the concentration process of caprolactam is taken as an example, and besides caprolactam, various organic aqueous solutions can be concentrated by using the device, for example, DMF aqueous solution, DMA aqueous solution, DMAC aqueous solution, DMSO aqueous solution, etc. As shown in fig. 2, this embodiment includes two evaporation systems 20 and one rectification system 17. Specifically, there are two evaporation systems 20, both connected to the compressor; each evaporation system 20 comprises a heater 3, a separator 4, a circulation pump 13; the rectification system 17 comprises a rectification tower 9, a reboiler 11 and a compressor 10, wherein the compressor connected with the evaporation system 20 is the compressor 10 in the rectification system 17, i.e. the evaporation system 20 and the rectification system 17 share one compressor.

Each evaporation system 20 includes a raw material input port, a material output port, a steam input port, a steam output port, and a condensate output port, forming an evaporation system including a raw material total input port, an intermediate material total output port, a steam total input port, a steam total output port, and a condensate total output port.

The raw material main input port is connected with the primary preheater 1.

Each evaporation body comprises a heater 3, and the heater 3 may be a tube heater, a plate heater or other heaters commonly used in the art, but in this embodiment, it is preferable that the heater 3 is a tube heater.

The primary preheater 1 extracts condensed water output by each evaporation system 20 from a corresponding condensed water output port through a primary condensed water pump 12, exchanges heat between the condensed water and caprolactam solution to be input into the evaporation system 20, and preheats the caprolactam solution.

The steam main output port is connected to the compressor 10, pressurizes steam, and inputs the steam into the steam main input port.

The total output port of the intermediate material is connected with the secondary preheater 6 through a pipeline provided with a material transfer pump 14, and the intermediate material is conveyed into a rectification system 17 through the material transfer pump 14.

The rectification system 17 comprises an intermediate material input port, a concentrated material output port, a condensed water output port and other communication ports for conveying materials, steam and condensed water.

The intermediate material inlet is connected with the secondary preheater 6.

The secondary preheater 6 extracts condensed water output by the rectification system 17 from a corresponding condensed water output port through the secondary condensed water pump 15, exchanges heat between the condensed water and intermediate materials to be input into the rectification system 17, and preheats the intermediate materials; the condensate water is sent to the top of the rectifying tower 9 as tower top reflux liquid after being cooled by the mol reflux ratio of 5 to the cooler 7.

In practical application, two evaporation effect bodies are connected in parallel, namely, in two adjacent evaporation effect bodies, the material output port of the latter evaporation effect body is connected with the raw material input port of the former evaporation effect body, and the vapor output ports of the two evaporation effect bodies are summarized as a vapor total output port and are connected to the inlet of the compressor 10.

In practical application, a raw material input port of each evaporation system 20 is provided with a feed pump; a material outlet of each evaporation system 20 is provided with a discharge pump; between two adjacent evaporation systems 20, the discharge pump of the material output port of the latter evaporation system 20 and the feed pump of the material input port of the former evaporation system 20 are the same pump, namely the transfer pump 14.

By combining rectification and evaporation, the method not only greatly improves the removal amount of caprolactam in the secondary steam and ensures the evaporation heat transfer efficiency, but also saves the use of steam and circulating water, does not add an absorbent additionally, has obvious reduction of the operation energy consumption and reduces the production cost of products.

Example 3

The embodiment provides a high-efficiency and energy-saving device for concentrating a high-boiling-point ascending system, which has a specific structure similar to that of embodiment 1, and is different from the embodiment 1 only in the number of evaporation systems 20, and particularly as shown in fig. 3, in the embodiment, one rectification system 17 is separately arranged, and no evaporation system 20 is arranged.

Application example 1

For the 140t/h flow of caprolactam aqueous solution, the working condition that the caprolactam concentration is 30% and the caprolactam concentration after concentration is 90% is compared with the working condition that the concentration device described in the example 1 is adopted for concentration, the three-effect evaporation in the prior art is adopted, the MVR evaporation+the two-effect evaporation in the prior art is adopted, the MVR evaporation+the three-effect evaporation in the prior art is adopted, and the MVR evaporation (the final heat source is steam) in the prior art is adopted. Assume that the energy prices are respectively: steam price 200 yuan/t, electricity price 0.8 yuan/kwh, circulating water price 0.2 yuan/t, annual operation 8000h, the comparison result is shown in the following table:

from the table above, the device and the corresponding process used in the utility model can save about 60% of energy by three-effect evaporation, about 55% of energy by MVR+two-effect evaporation, about 45% of energy by MVR+three-effect evaporation, and about 40% of energy by MVR evaporation (the last effect heat source is steam); the process used in the utility model does not need to additionally introduce an absorbent, the flow rate of the absorbent accounts for about 10% of the total evaporation capacity, the absorbent needs to be generated in the evaporator, the evaporation capacity is increased by 10% relatively, namely the area of a heater of the evaporator is increased by 10%, the flow rate of a compressor is increased by 10% by the absorbent, and therefore, the increase of part of operation energy consumption is not calculated in the comparison table; the utility model adopts MVR rectification and MVR evaporation mode to separate caprolactam and water, and the reflux liquid at the top of the rectification column is condensed water with lower concentration of caprolactam, which has higher efficiency than the absorption tower adopted in the conventional process. Thus, the present utility model achieves the intended aim.

The specific embodiments described herein are offered by way of example only to illustrate the spirit of the utility model. Those skilled in the art may make various modifications or additions to the described embodiments or substitutions thereof without departing from the spirit of the utility model or exceeding the scope of the utility model as defined in the accompanying claims.

Although terms such as the primary preheater 1, the primary condensate tank 2, the heater 3, the separator 4, the secondary preheater 6, the cooler 7, the secondary condensate tank 8, the rectifying column 9, the compressor 10, the reboiler 11, the primary condensate pump 12, the circulation pump 13, the transfer pump 14, the secondary condensate pump 15, the bottom circulation pump 16, the rectifying system 17, the reboiling system 18, the feed inlet 19, the evaporation system 20, etc. are used more herein, the possibility of using other terms is not excluded. These terms are used merely for convenience in describing and explaining the nature of the utility model; they are to be interpreted as any additional limitation that is not inconsistent with the spirit of the present utility model.

Claims

1. The utility model provides a concentrated device of high boiling point system that energy-efficient rises, includes rectification system (17) and connects reboiling system (18) on rectification system (17), feed inlet (19) are linked together with rectification system (17), its characterized in that: the device comprises a rectification system (17), a feed inlet (19) and a secondary preheater (6) which are arranged between the feed inlet (19) and the rectification system (17) and are used for generating heat exchange, wherein two ends of the secondary preheater (6) are respectively communicated with a cooler (7) and a secondary condensate pump (15), one end, far away from the secondary preheater (6), of the cooler (7) is connected with the top of the rectification system (17), and one end, far away from the secondary preheater (6), of the secondary condensate pump (15) is connected with a reboiler (11) of the rectification system (17) through a secondary condensate water tank (8);

the rectification system (17) comprises a rectification tower (9) and at least one compressor (10) connected to the top of the rectification tower (9) and used for compressing steam, the cooler (7) is communicated with the top of the rectification tower (9), one end of the compressor (10) away from the rectification tower (9) is communicated with the reboiling system (18), and the compressors (10) are arranged in one-to-one correspondence with the reboiling system (18);

at least one evaporation system (20) can be additionally arranged between the feed inlet (19) and the secondary preheater (6), the evaporation system (20) is communicated with the secondary preheater (6) through a transfer pump (14), and the feed inlet (19) is communicated with the evaporation system (20) through the primary preheater (1);

the evaporation system (20) comprises a heater (3) and a separator (4) which are communicated with each other, a liquid outlet of the separator (4) is communicated with a material transferring pump (14), a gas outlet of the separator (4) is communicated with the heater (3) through a rectifying tower (9) and a compressor (10) in sequence, and the primary preheater (1) is communicated with the top of the heater (3).

2. The energy efficient high boiling point lift system concentrating apparatus of claim 1 wherein: the reboiling system (18) is provided with at least one, and the reboiling system (18) comprises a reboiler (11) and a tower bottom circulating pump (16) which are communicated with each other.

3. The energy efficient high boiling point system concentrating apparatus according to claim 2 wherein: the reboiling system (18) is provided with at least one, one end of the reboiler (11) is communicated with the middle part or the lower section of the rectifying system (17), and the tower bottom circulating pump (16) is communicated with the middle part or the bottom of the rectifying system (17).

4. The energy efficient high boiling point system concentrating apparatus according to claim 2 wherein: the rectifying tower (9) is one or a combination of a plurality of plate towers and fillers; the reboiler (11) is one or more of a kettle type reboiler, a siphon type reboiler and a falling film type reboiler.

5. The energy efficient high boiling point lift system concentrating apparatus of claim 1 wherein: one end of the primary preheater (1) is communicated with the top of the heater (3), the other end of the primary preheater is communicated with the primary condensate pump (12), and one end of the primary condensate pump (12), which is far away from the primary preheater (1), is connected with the heater (3) through the primary condensate water tank (2).

6. The energy efficient high boiling point lift system concentrating apparatus of claim 1 wherein: the heater (3) is a tubular heater and/or a plate heater.

7. The energy efficient high boiling point lift system concentrating apparatus of claim 1 wherein: the evaporation system (20) is provided with at least one, and the at least one evaporation system (20) is connected in series or in parallel.