Heat pump type rectification Rubik's cube system

Abstract

The utility model discloses a heat pump type rectification magic cube system which comprises a tower body, a heat pump device is arranged on one side of the tower body, the heat pump device comprises a main condenser, a gas separation tank, a compressor, an oil separation tank, a reboiler, an expansion valve and an oil cooling cooler, the main condenser is communicated with the gas separation tank through a pipeline, the gas separation tank is communicated with the compressor through a pipeline, and the oil cooling cooler is communicated with the compressor through a pipeline. The compressor is communicated with the oil separation tank through a pipeline, the compressor is communicated with the oil cooler through a pipeline, the oil separation tank is communicated with the reboiler through a pipeline, the reboiler is communicated with the expansion valve through a pipeline, and the expansion valve is communicated with the main condenser through a pipeline; the main condenser is connected with a preheater and a heat balance condenser, and the preheater is communicated with the tower body through a pipeline; the heat balance condenser is connected with a buffer tank and a vacuum system, the buffer tank is connected with a finished product cooler, and the finished product cooler is connected with a qualified product storage tank. The technical scheme is reasonable in structural design, compact in structure, low in height, high in heat and mass transfer efficiency, low in operation cost and good in practicability.

Description

Technical Field

[0001] This utility model relates to the field of distillation equipment technology, specifically to a heat pump type distillation cube system. Background Technology

[0002] Existing distillation equipment generally uses traditional distillation columns. A search reveals that, for example, Chinese utility model patent CN202421311861.7 discloses "a distillation device for hydrogen cyanide, including a column body, a tray structure disposed within the column body, and a spray structure disposed at the top of the column, and also includes a liquid separation structure disposed at the bottom of the column body, wherein the liquid separation structure includes a connecting ring platform fixed to the inner wall of the column body and several first dividing plates fixed within the connecting ring platform, the bottom surface of the first dividing plates not contacting the bottom surface of the column body." Such distillation columns are generally over 20 meters long and have a dispersed layout, requiring high-level construction. Furthermore, existing distillation columns use steam as a heat source and cooling circulating water as a cold source, resulting in high energy consumption costs.

[0003] Traditional distillation columns, due to their considerable height, are highly susceptible to problems even with slight tilting. This can lead to uneven liquid distribution, wall flow, and reduced heat and mass exchange efficiency. Furthermore, equipment maintenance is difficult, time-consuming, and costly, often requiring the deployment of lifting equipment for repairs.

[0004] Traditional distillation columns require a long time to heat up and undergo total reflux before operation, which wastes both steam and time. In addition, the large heat dissipation area of ​​the traditional distillation column body results in unnecessary steam waste. Summary of the Invention

[0005] In view of the shortcomings of the existing technology, the purpose of this utility model is to provide a heat pump type distillation cube system with reasonable structural design, compact structure, low height, high heat and mass exchange efficiency, low operating cost and good practicality.

[0006] To achieve the above objectives, this utility model provides the following technical solution: a heat pump type distillation cube system, including a column body, a heat pump device is provided on one side of the column body, the heat pump device includes a main condenser, a gas separator, a compressor, an oil separator, a reboiler, an expansion valve and an oil cooler, the main condenser is connected to the gas separator via a pipeline, the gas separator is connected to the compressor via a pipeline, the compressor is connected to the oil separator via a pipeline and the compressor is connected to the oil cooler via a pipeline, the oil separator is connected to the reboiler via a pipeline, the reboiler is connected to the expansion valve via a pipeline, and the expansion valve is connected to the main condenser via a pipeline;

[0007] The main condenser is connected to a preheater and a heat balance condenser. The main condenser and the preheater are connected by a pipeline. The preheater is connected to a material tank and to the tower body via a pipeline. The heat balance condenser is connected to a buffer tank and a vacuum system. The buffer tank is connected to a finished product cooler and a qualified product storage tank. The main condenser and the buffer tank are connected by a pipeline, and the buffer tank is connected to the tower body via a pipeline.

[0008] This invention is further configured as follows: the low-temperature, low-pressure liquid working fluid in the main condenser absorbs the energy released by the condensation of materials and vaporizes into a low-temperature, low-pressure gaseous working fluid, which then enters the gas separator tank through a pipeline. The liquid refrigerant, carried by the airflow into the gas separator tank, is separated within the gas separator tank and then flows back to the main condenser through a pipeline. The low-temperature, low-pressure gaseous working fluid in the gas separator tank enters the compressor through a pipeline. The compressor discharges the high-temperature, high-pressure gaseous working fluid through a pipeline into the oil separator tank, and the high-pressure end of the compressor discharges refrigerant oil through a pipeline to the oil cooler. After being cooled by the oil cooler, the oil enters the low-pressure end of the compressor through pipelines. The oil separator separates a small amount of refrigeration oil and pressurizes it back to the low-pressure end of the compressor through pipelines. The high-temperature and high-pressure gaseous working fluid separated by the oil separator enters the reboiler through pipelines. In the reboiler, the high-temperature and high-pressure gaseous working fluid transfers energy to the material and becomes a high-temperature and high-pressure liquid working fluid. After entering the expansion valve through pipelines, the high-temperature and high-pressure liquid working fluid is depressurized through the expansion valve. Part of the working fluid self-vaporizes and absorbs heat. The working fluid becomes a low-temperature and low-pressure liquid phase and a small amount of gas phase, which enter the main condenser for circulation.

[0009] This utility model is further configured such that: the tower body includes a primary tower, a secondary tower, a tertiary tower, a quaternary tower, and a quintuplet tower; the primary tower, secondary tower, tertiary tower, quaternary tower, and quintuplet tower are respectively connected to the preheater via pipelines; the primary tower is connected to the secondary tower via a pipeline; the secondary tower is connected to the tertiary tower via a pipeline; the tertiary tower is connected to the quaternary tower via a pipeline; the quaternary tower is connected to the quintuplet tower via a pipeline; the quintuplet tower is connected to the buffer tank via a pipeline; a primary pump is installed at the lower end of the primary tower; a secondary pump is installed at the lower end of the secondary tower; a tertiary pump is installed at the lower end of the tertiary tower; a quaternary pump is installed at the lower end of the quaternary tower; and a quintuplet tower is installed at the lower end of the quintuplet tower; all the primary tower, secondary tower, tertiary tower, quaternary tower, and quintuplet tower are square structures and are arranged side by side.

[0010] This invention is further configured such that: automatic valves are respectively installed on the pipelines between the first-stage, second-stage, third-stage, fourth-stage, and fifth-stage towers and the preheater. After the liquid phase material is heated, the automatic valves control the material to enter one of the first-stage, second-stage, third-stage, or fourth-stage towers according to different concentrations. The liquid in the first-stage tower and the liquid in the reboiler are combined and then enter the reboiler through a first-stage pump, where heat exchange occurs through the tubes and refrigerant, generating rising steam. The liquid in the second-stage tower enters the first-stage tower through a second-stage pump and exchanges heat and mass with the rising hot steam in the first-stage tower within the packing. The liquid in the third-stage tower enters the second-stage tower through a third-stage pump and exchanges heat and mass with the rising hot steam in the second-stage tower within the packing. The liquid in the fourth-stage tower enters the third-stage tower through a fourth-stage pump and exchanges heat and mass with the rising hot steam in the third-stage tower within the packing. The liquid in the fifth-stage tower enters the fourth-stage tower through a fifth-stage pump and exchanges heat and mass with the rising hot steam in the fourth-stage tower within the packing. The steam from the top of the fifth-stage tower is introduced into the preheater for heat exchange with the raw material.

[0011] This utility model is further configured as follows: steam and a small amount of liquid phase material are introduced into the main condenser through a preheater via a pipeline; the main condenser introduces a small amount of steam into the heat balance condenser through a ventilation pipeline; the heat balance condenser allows the liquid phase material to flow by gravity into the buffer tank through a pipeline; the liquid in the buffer tank flows back to the finished product cooler through a pipeline; the finished product cooler is connected to the qualified product storage tank through a pipeline; and the qualified liquid phase product at room temperature is introduced into the qualified product storage tank through a pipeline.

[0012] This invention is further configured such that: each of the first-stage, second-stage, third-stage, fourth-stage, and fifth-stage towers is equipped with a distribution plate and packing. The distribution plate is located at the top of each stage of the tower. The reflux liquid enters the distribution plate from the top of each stage of the tower, is evenly distributed, and then enters the packing. The liquid phase material that falls after heat and mass exchange at the bottom of each stage of the tower is pumped to the previous stage of the tower as reflux liquid for redistribution, thereby forming components of different concentrations in each stage of the tower, with the lowest concentration in the first stage of the tower.

[0013] The beneficial effects of this utility model are as follows: Compared with the prior art, this utility model has a reasonable structural design. Each tower section presents a regular matrix, allowing for side-by-side arrangement. Each tower section has a certain volume at its bottom, which is pumped to the top of the next stage tower. A distribution plate is installed at the top of the tower to ensure the liquid is evenly distributed within the packing. This change not only fully realizes all the functions of previous single-stage high-rise towers but also avoids the various drawbacks that occurred during the design, manufacture, and installation of single-stage high-rise towers. It features a compact structure, low height, high heat and mass exchange efficiency, low operating costs, and good practicality.

[0014] (1) By using the principle of heat pump, low-grade energy is recovered and converted into high-grade energy for reuse. Compared with traditional steam distillation towers, the operating cost is significantly reduced.

[0015] (2) The total height of the device of this utility model is within 6m, which can meet the indoor installation without crossing floors, and can also be installed outdoors without steel frame or building support. The installation cost is greatly reduced. Only cable laying and small steam pipe and circulating water are needed, which can greatly reduce the construction cost of public system.

[0016] (3) This utility model can be made into a skid-mounted structure, which is compact and reasonable, with high space utilization. It is qualified for commissioning and operation before leaving the factory. Compared with traditional distillation towers, it can significantly shorten the on-site installation and commissioning time.

[0017] (4) Each tower section of this utility model is independently positioned, which can effectively ensure the verticality of each tower section. Each tower section has a distribution plate to collect and redistribute liquid, thereby improving the packing efficiency.

[0018] (5) Each tower section of this utility model can be repaired independently without the need for lifting equipment.

[0019] (6) Each tower section of this utility model has an independent liquid storage function. When the machine is stopped, the concentration difference between each tower section is still maintained, saving energy consumption costs for the next cycle. At the same time, it reduces the hot tower and total reflux time when the machine is started.

[0020] (7) Each tower section of this utility model is compact, which reduces the external heat dissipation area and reduces energy waste.

[0021] The present invention will be further described below with reference to the accompanying drawings and specific embodiments. Attached Figure Description

[0022] Figure 1 This is a schematic diagram of the structure of an embodiment of the present utility model. Figure 1 ;

[0023] Figure 2 This is a schematic diagram of the structure of an embodiment of the present utility model. Figure 2 ;

[0024] Figure 3 This is a top view schematic diagram of an embodiment of the present utility model;

[0025] Figure 4 This is a front view schematic diagram of an embodiment of the present utility model;

[0026] Figure 5 This is a schematic diagram of the heat pump device according to an embodiment of the present invention;

[0027] Figure 6 This is a schematic diagram illustrating the material distillation principle of an embodiment of this utility model. Detailed Implementation

[0028] In the description of this embodiment, it should be noted that the terms "center," "upper," "lower," "left," "right," "vertical," "horizontal," "inner," "outer," "front," and "rear," etc., indicate the orientation or positional relationship based on the orientation or positional relationship shown in the accompanying drawings. They are used only for the convenience of describing this utility model and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this utility model. Furthermore, the terms "first," "second," and "third" are used for descriptive purposes only and should not be construed as indicating or implying relative importance.

[0029] See Figures 1 to 6 This utility model discloses a heat pump type distillation cube system, including a column body. A heat pump device is provided on one side of the column body. The heat pump device includes a main condenser 1, a gas separator 2, a compressor 3, an oil separator 4, a reboiler 5, an expansion valve 6, and an oil cooler 7. The main condenser 1 is connected to the gas separator 2 through a pipeline. The gas separator 2 is connected to the compressor 3 through a pipeline. The compressor 3 is connected to the oil separator 4 through a pipeline, and the compressor 3 is connected to the oil cooler 7 through a pipeline. The oil separator 4 is connected to the reboiler 5 through a pipeline. The reboiler 5 is connected to the expansion valve 6 through a pipeline. The expansion valve 6 is connected to the main condenser 1 through a pipeline.

[0030] The main condenser 1 is connected to a preheater 8 and a heat balance condenser 9. The main condenser 1 and the preheater 8 are connected by a pipeline. The preheater 8 is connected to a material tank and is also connected to the tower body by a pipeline. The heat balance condenser 9 is connected to a buffer tank 10 and a vacuum system 11. The buffer tank 10 is connected to a finished product cooler 12 and a qualified product storage tank. The main condenser 1 and the buffer tank 10 are connected by a pipeline, and the buffer tank 10 is connected to the tower body by a pipeline.

[0031] Preferably, the oil cooler 7 is an oil-cooled plate cooler; the finished product cooler 12 is a plate cooler; the vacuum system 11 includes a vacuum pump and a water tank.

[0032] The main condenser 1 is an evaporator for the refrigerant, and the reboiler 5 is a condenser for the refrigerant.

[0033] To make the structural design of this utility model more reasonable, as a preferred embodiment, the low-temperature, low-pressure liquid working fluid in the main condenser 1 absorbs the energy released by the condensation of materials and vaporizes into a low-temperature, low-pressure gaseous working fluid, which then enters the gas separator 2 through a pipeline. The liquid refrigerant carried into the gas separator 2 by the airflow is separated in the gas separator 2 and then flows back to the main condenser 1 through a pipeline. The low-temperature, low-pressure gaseous working fluid in the gas separator 2 enters the compressor 3 through a pipeline. The compressor 3 discharges the high-temperature, high-pressure gaseous working fluid into the oil separator 4 through a pipeline, and the high-pressure end of the compressor 3 discharges refrigeration oil to the oil cooler through a pipeline. Cooler 7: After being cooled by the oil cooler 7, the refrigeration oil enters the low-pressure end of the compressor 3 through a pipeline; oil separator 4 separates a small amount of refrigeration oil and pressurizes it back to the low-pressure end of the compressor 3 through a pipeline. The high-temperature and high-pressure gaseous working fluid separated by the oil separator 4 enters the reboiler 5 through a pipeline. In the reboiler 5, the high-temperature and high-pressure gaseous working fluid transfers energy and heat to the material, becoming a high-temperature and high-pressure liquid working fluid, which then enters the expansion valve 6 through a pipeline. After the high-temperature and high-pressure liquid working fluid is depressurized by the expansion valve 6, part of the working fluid self-vaporizes and absorbs heat, becoming a low-temperature and low-pressure liquid phase and a small amount of gas phase, which then enter the main condenser 1 for cyclic operation.

[0034] The tower body includes a primary tower 13, a secondary tower 14, a tertiary tower 15, a quaternary tower 16, and a quinary tower 17. Each of these towers is connected to the preheater 8 via a pipe. The primary tower 13 is connected to the secondary tower 14 via a pipe, the secondary tower 14 to the tertiary tower 15 via a pipe, the tertiary tower 15 to the quaternary tower 16 via a pipe, and the quaternary tower 16 to the quinary tower 17 via a pipe. The primary tower 13 is connected to the reboiler 5 via a pipe, and the quinary tower 17 is connected to the preheater 8 via a pipe. The five-stage tower 17 is connected to the buffer tank 10 via a pipeline. A first-stage pump 131 is installed at the lower end of the first-stage tower 13, a second-stage pump 141 is installed at the lower end of the second-stage tower 14, a third-stage pump 151 is installed at the lower end of the third-stage tower 15, a fourth-stage pump 161 is installed at the lower end of the fourth-stage tower 16, and a fifth-stage pump 171 is installed at the lower end of the fifth-stage pump 17. The first-stage tower 13, second-stage tower 14, third-stage tower 15, fourth-stage tower 16, and fifth-stage tower 17 are all square structures and are arranged side by side.

[0035] Preferably, the primary tower 13, secondary tower 14, tertiary tower 15, quaternary tower 16, and quinary tower 17 are assembled side-by-side as a single unit, and the primary pump 131, secondary pump 141, tertiary pump 151, quaternary pump 161, and quinary pump 171 are all water pumps. Each of the primary tower 13, secondary tower 14, tertiary tower 15, quaternary tower 16, and quinary tower 17 is equipped with an independent liquid storage structure. Due to its independent liquid storage function, the concentration difference between each tower section is maintained when the unit is shut down, saving energy costs for the next cycle and reducing the time required for hot towers and total reflux during startup.

[0036] Automatic valves are installed on the pipelines between the primary tower 13, secondary tower 14, tertiary tower 15, quaternary tower 16, and quinary tower 17 and the preheater 8. After the liquid material is heated, the automatic valves control the flow of the material into one of the primary tower 13, secondary tower 14, tertiary tower 15, or quaternary tower 16 according to different concentrations. The liquid in the primary tower 13 and the liquid in the reboiler 5 are combined and then enter the reboiler 5 through the primary pump 131. Heat exchange is conducted through the tubes and refrigerant to generate rising steam. The liquid in the secondary tower 14 enters the primary tower 13 through the secondary pump 141 and combines with the liquid in the primary tower 13. The rising hot steam in the first stage undergoes heat and mass exchange within the packing. The liquid in the third-stage tower 15 enters the second-stage tower 14 through the third-stage pump 151, and exchanges heat and mass with the rising hot steam in the second-stage tower 14 within the packing. The liquid in the fourth-stage tower 16 enters the third-stage tower 15 through the fourth-stage pump 161, and exchanges heat and mass with the rising hot steam in the third-stage tower 15 within the packing. The liquid in the fifth-stage tower 17 enters the fourth-stage tower 16 through the fifth-stage pump 171, and exchanges heat and mass with the rising hot steam in the fourth-stage tower 16 within the packing. The steam from the top of the fifth-stage tower 17 is introduced into the preheater 8 for heat exchange with the raw material.

[0037] Steam and a small amount of liquid material are introduced into the main condenser 1 through the preheater 8 via a pipeline. The main condenser 1 then introduces a small amount of steam into the heat balance condenser 9 through a ventilation pipeline. The heat balance condenser 9 then allows the liquid material to flow by gravity into the buffer tank 10 through a pipeline. The liquid in the buffer tank 10 flows back to the finished product cooler 12 through a pipeline. The finished product cooler 12 is connected to the qualified product storage tank through a pipeline. The qualified liquid product at room temperature is introduced into the qualified product storage tank through a pipeline.

[0038] In this embodiment, each of the first-stage tower 13, second-stage tower 14, third-stage tower 15, fourth-stage tower 16, and fifth-stage tower 17 is equipped with a distribution plate and packing. The distribution plate is located at the top of each stage of the tower. The reflux liquid enters the distribution plate from the top of each stage of the tower and is evenly distributed before entering the packing. The liquid phase material that falls after heat and mass exchange at the bottom of each stage of the tower is pumped to the previous stage of the tower as reflux liquid for redistribution, thereby forming components of different concentrations in each stage of the tower, with the lowest concentration in the first stage of the tower.

[0039] The two ends of each of the above-mentioned pipes are fixed by flange connection, welding, or threaded connection.

[0040] In practical applications, the materials can be organic solvents such as dilute ethanol, dilute methanol, dilute acetone, and dilute ethyl acetate. For ease of understanding, dilute ethanol will be used as an example below.

[0041] A dilute ethanol solution at room temperature enters the preheater by gravity or pump. After heating, the liquid dilute ethanol, depending on its concentration, is controlled by an automatic valve to enter one of the first-stage, second-stage, third-stage, or fourth-stage columns. The liquid in the first-stage column and the liquid in the reboiler are combined and then pumped into the reboiler via a first-stage pump. Heat exchange occurs through the tubes and refrigerant, generating rising steam. The liquid in the second-stage column is pumped back into the first-stage column for distribution, where it exchanges heat and mass with the rising steam within the packing. The liquid in the third-stage column is pumped back into the second-stage column for distribution, where it exchanges heat and mass with the rising steam within the packing. The liquid in the fourth-stage column is pumped back into the third-stage column for distribution, where it exchanges heat and mass with the rising steam within the packing. The liquid in the fifth-stage column is pumped back into the fourth-stage column for distribution, where it exchanges heat and mass with the rising steam within the packing. Wastewater reaching the discharge concentration in the reboiler is discharged via a wastewater discharge pump.

[0042] Preheater working principle: High-concentration ethanol vapor from the top of the tower exchanges heat with the raw material through a shell-and-tube heat exchanger, allowing for energy reuse. Ethanol vapor and a small portion of liquid ethanol are introduced into the main condenser. In the main condenser, the high-concentration ethanol vapor exchanges heat with the low-temperature, low-pressure liquid working fluid. The high-concentration ethanol vapor condenses into liquid high-concentration ethanol and enters the buffer tank. The low-temperature, low-pressure liquid working fluid evaporates into a gas phase and enters the gas separator. A small amount of ethanol vapor is introduced into the heat balance condenser. Through a shell-and-tube or plate heat exchanger, the high-concentration ethanol vapor that was not liquefied by the main condenser exchanges heat with the refrigerant (cooling circulating water), improving the ethanol recovery rate. Non-condensable gas is passed through... The vacuum pump of the vacuum system discharges the ethanol outside the system; the liquid ethanol flows by gravity to the buffer tank, which collects the high-concentration ethanol liquefied in the main condenser and the heat balance condenser through gravity, so that the condensation rate and the flow rate of the reflux / finished product pump are dynamically stable, and a certain liquid level is maintained as a buffer. The liquid in the buffer tank is branched off by the reflux / finished product pump and goes to the finished product cooler. The finished product cooler exchanges heat between the refrigerant (cooling circulating water) and the finished product ethanol between the plates, so as to achieve a cooling effect, so that the finished product ethanol is cooled before it reaches the qualified product storage tank, reducing evaporation. The room temperature liquid-phase concentrated ethanol enters the qualified product storage tank after exiting the finished product cooler.

[0043] The liquid in the buffer tank is diverted through a reflux / finished product pump to a branch line for distillation reflux back to the top of the five-stage column. The working principle of the entire column is as follows:

[0044] From level 1 to multiple levels (five levels in total is just an example; the number of levels may not be specified).

[0045] The reflux liquid is the most concentrated liquid ethanol in the entire system. It enters the distribution plate from the top of the column, where it is evenly distributed into the packing material, where it exchanges heat and mass with the lower-concentration ethanol vapor rising from the bottom layer.

[0046] The concept of heat and mass transfer: Steam rises through the trays or packing and comes into contact with the upper cold liquid. The heavy components in the gas phase condense and release heat, while the light components in the liquid phase absorb heat and vaporize, resulting in more volatile components entering the gas phase and less volatile components remaining in the liquid phase.

[0047] At the bottom of each stage of the tower, the liquid phase that falls after heat and mass exchange is pumped to the previous stage as reflux liquid for redistribution, so that each stage of the tower forms components of different concentrations, while the first stage tower has the lowest concentration and meets the emission standards.

[0048] The concentration of the raw material determines its entry point into the tower.

[0049] The working principle of the heat pump device in this embodiment is as follows:

[0050] The low-temperature, low-pressure liquid working fluid absorbs the energy released by the condensation of materials in the main condenser (which is the evaporator for refrigerant), vaporizing into a low-temperature, low-pressure gaseous working fluid, which then enters the gas separator. The liquid refrigerant, carried by the airflow into the gas separator, is separated and then flows back to the main condenser. The low-temperature, low-pressure gaseous working fluid enters the compressor. The high-temperature, high-pressure gaseous working fluid discharged from the compressor enters the oil separator. The refrigeration oil exits from the high-pressure end of the compressor, passes through an oil-cooled plate heat exchanger, and enters the low-pressure end of the compressor, thus providing cooling. The function of oil separation: A small amount of refrigeration oil is carried into the oil separator, separated, and then compressed back to the low-pressure end of the compressor; the high-temperature and high-pressure gaseous working fluid separated by the oil separator enters the reboiler (which is the condenser for refrigerant); the high-temperature and high-pressure gaseous working fluid transfers energy and heat to the material in the reboiler, becoming a high-temperature and high-pressure liquid working fluid that enters the expansion valve; after the high-temperature and high-pressure liquid working fluid is depressurized through the expansion valve, part of the working fluid self-vaporizes, absorbs heat, and the working fluid becomes a low-temperature and low-pressure liquid phase and a small amount of gas phase, which then enter the main condenser for circulation.

[0051] The working principles of each component of the heat pump unit are as follows:

[0052] Main condenser working principle:

[0053] High-concentration ethanol vapor exchanges heat with a low-temperature, low-pressure liquid working medium in the main condenser. The high-concentration ethanol vapor condenses into liquid high-concentration ethanol and enters the buffer tank. The low-temperature, low-pressure liquid working medium evaporates into a gas phase and enters the gas separator.

[0054] Working principle of gas separator:

[0055] When the low-temperature, low-pressure gaseous working fluid enters the gas separator, a small amount of liquid phase will inevitably be carried in. Through separation in the gas separator, the small amount of liquid working fluid will re-enter the main condenser due to the height difference, while the gaseous working fluid will be drawn into the compressor.

[0056] Compressor working principle:

[0057] The compressor has a screw structure inside, using refrigerant oil for lubrication and gap filling. Its function is to transform a low-temperature, low-pressure gaseous working fluid into a high-temperature, high-pressure gaseous working fluid through the extrusion of the screw.

[0058] Working principle of oil-cooled plate cooler:

[0059] The refrigerant (which can be cooling water or other methods) exchanges heat with the refrigeration oil discharged from the high-pressure side of the compressor to cool it down, and then the refrigeration oil re-enters the low-pressure side of the compressor. This cycle is repeated.

[0060] Working principle of oil separator:

[0061] When the high-temperature, high-pressure gaseous working fluid exits the compressor, it inevitably carries a small amount of refrigeration oil into the oil separator. The oil separator works by increasing its volume, causing the refrigeration oil particles to settle, and using internal packing materials to intercept the oil droplets, thus achieving separation.

[0062] Reboiler working principle:

[0063] A high-temperature, high-pressure gaseous working fluid exchanges heat with a low-concentration liquid ethanol solution (generally <1%) in a reboiler. The high-temperature, high-pressure gaseous working fluid condenses into a high-temperature, high-pressure liquid working fluid, while the low-concentration ethanol solution vaporizes into low-concentration ethanol vapor upon heating.

[0064] Expansion valve working principle:

[0065] The expansion valve is actually a pressure relief valve, and its function is to control the pressure on the working fluid side inside the main condenser. When the high-temperature, high-pressure liquid working fluid enters the main condenser, the flow rate is regulated by the expansion valve. Due to the decrease in pressure, a small portion of the working fluid vaporizes and absorbs heat, causing the temperature of the liquid working fluid to drop, forming a low-temperature, low-pressure liquid working fluid with a small amount of gaseous working fluid entrained.

[0066] This invention allows each tower section to be arranged in a regular matrix, enabling side-by-side placement. Each section has a specific volume at its bottom, through which liquid is pumped to the top of the next stage. A distribution plate at the top ensures even distribution of the liquid within the packing. This design not only fully realizes all the functions of previous single-stage high-rise towers but also avoids the various drawbacks associated with their design, fabrication, and installation. The structure is rationally designed, compact, low in height, highly efficient in heat and mass exchange, low in operating costs, and highly practical.

[0067] The specific beneficial effects are as follows:

[0068] (1) By using the heat pump principle, low-grade energy is recovered and converted into high-grade energy for reuse. Compared with traditional steam-type distillation towers, the operating cost is significantly reduced. Based on a steam price of 250 yuan / ton, an electricity cost of 0.8 yuan / kWh, and a water cost of 5 yuan / ton, the operating cost can be reduced by about 67%.

[0069] (2) The total height of the device of this utility model is within 6m, which can meet the indoor installation without crossing floors, and can also be installed outdoors without steel frame or building support. The installation cost is greatly reduced. Only cable laying and small steam pipe and circulating water are needed, which can greatly reduce the construction cost of public system.

[0070] (3) This utility model can be made into a skid-mounted structure, which is compact and reasonable, with high space utilization, and has passed the commissioning and operation test before leaving the factory. Compared with traditional distillation columns, it can significantly shorten the on-site installation and commissioning time.

[0071] (4) Each tower section of this utility model is independently positioned, which can effectively ensure the verticality of each tower section. Each tower section has a distribution plate to collect and redistribute liquid, thereby improving the packing efficiency.

[0072] (5) Each tower section of this utility model can be repaired independently without the need for lifting equipment.

[0073] (6) Each tower section of this utility model has an independent liquid storage function. When the machine is stopped, the concentration difference of each tower section is still maintained, saving energy consumption costs in the next cycle, while reducing the hot tower and total reflux time when the machine is started.

[0074] (7) Each tower section of this utility model is compact, which reduces the external heat dissipation area and reduces energy waste.

[0075] In addition, improvements can be made to the technical solution of this embodiment: for example, the structures of the first-level tower 13, the second-level tower 14, the third-level tower 15, the fourth-level tower 16 and the fifth-level tower 17 can all be set as cylindrical.

[0076] The above description of the specific embodiments of this utility model is only used to further illustrate this utility model and should not be construed as limiting the scope of protection of this utility model. Any non-essential improvements and adjustments made to this utility model by technical engineers based on the above description of the utility model shall fall within the scope of protection of this utility model.

Claims

1. A heat pump type distillation cube system, comprising a column body, characterized in that: A heat pump device is provided on one side of the tower body. The heat pump device includes a main condenser (1), a gas separator (2), a compressor (3), an oil separator (4), a reboiler (5), an expansion valve (6), and an oil cooler (7). The main condenser (1) is connected to the gas separator (2) through a pipeline. The gas separator (2) is connected to the compressor (3) through a pipeline. The compressor (3) is connected to the oil separator (4) through a pipeline. The compressor (3) is connected to the oil cooler (7) through a pipeline. The oil separator (4) is connected to the reboiler (5) through a pipeline. The reboiler (5) is connected to the expansion valve (6) through a pipeline. The expansion valve (6) is connected to the main condenser (1) through a pipeline. The main condenser (1) is connected to a preheater (8) and a heat balance condenser (9). The main condenser (1) and the preheater (8) are connected by a pipeline. The preheater (8) is connected to a material tank and is also connected to the tower body by a pipeline. The heat balance condenser (9) is connected to a buffer tank (10) and a vacuum system (11). The buffer tank (10) is connected to a finished product cooler (12), and the finished product cooler (12) is connected to a qualified product storage tank. The main condenser (1) and the buffer tank (10) are connected by a pipeline, and the buffer tank (10) is also connected to the tower body by a pipeline.

2. The heat pump type distillation cube system according to claim 1, characterized in that: The low-temperature, low-pressure liquid working fluid in the main condenser (1) absorbs the energy released by the condensation of materials and vaporizes into a low-temperature, low-pressure gaseous working fluid, which then enters the gas separator (2) through a pipeline. The liquid refrigerant carried into the gas separator (2) by the airflow is separated in the gas separator (2) and then flows back to the main condenser (1) through a pipeline. The low-temperature, low-pressure gaseous working fluid in the gas separator (2) enters the compressor (3) through a pipeline. The compressor (3) discharges the high-temperature, high-pressure gaseous working fluid into the oil separator (4) through a pipeline. The high-pressure end of the compressor (3) discharges refrigeration oil to the oil cooler (7) through a pipeline. The refrigeration oil is cooled by the oil cooler. After being cooled by the cooler (7), the oil enters the low-pressure end of the compressor (3) through the pipeline; the oil separator (4) separates a small amount of refrigeration oil and then presses it back to the low-pressure end of the compressor (3) through the pipeline. The high-temperature and high-pressure gaseous working medium separated by the oil separator (4) enters the reboiler (5) through the pipeline. The high-temperature and high-pressure gaseous working medium transfers energy to the material in the reboiler (5) and becomes a high-temperature and high-pressure liquid working medium. After entering the expansion valve (6) through the pipeline, the high-temperature and high-pressure liquid working medium is depressurized through the expansion valve (6). After the high-temperature and high-pressure liquid working medium is depressurized through the expansion valve (6), part of the working medium self-vaporizes and absorbs heat. The working medium becomes a low-temperature and low-pressure liquid phase and a small amount of gas phase and enters the main condenser (1) for cyclic operation.

3. A heat pump type distillation cube system according to claim 1 or 2, characterized in that: The tower body includes a primary tower (13), a secondary tower (14), a tertiary tower (15), a quaternary tower (16), and a quinary tower (17). The primary tower (13), secondary tower (14), tertiary tower (15), quaternary tower (16), and quinary tower (17) are connected to the preheater (8) via pipes. The primary tower (13) is connected to the secondary tower (14) via a pipe, the secondary tower (14) is connected to the tertiary tower (15) via a pipe, the tertiary tower (15) is connected to the quaternary tower (16) via a pipe, the quaternary tower (16) is connected to the quinary tower (17) via a pipe, the primary tower (13) is connected to the reboiler (5) via a pipe, and the quinary tower (17) is connected to the preheater (8) via a pipe. The five-stage tower (17) and the buffer tank (10) are connected by a pipeline. A first-stage pump (131) is installed at the lower end of the first-stage tower (13), a second-stage pump (141) is installed at the lower end of the second-stage tower (14), a third-stage pump (151) is installed at the lower end of the third-stage tower (15), a fourth-stage pump (161) is installed at the lower end of the fourth-stage tower (16), and a fifth-stage pump (171) is installed at the lower end of the fifth-stage tower (17). The first-stage tower (13), second-stage tower (14), third-stage tower (15), fourth-stage tower (16), and fifth-stage tower (17) are all square structures, and the first-stage tower (13), second-stage tower (14), third-stage tower (15), fourth-stage tower (16), and fifth-stage tower (17) are arranged side by side.

4. The heat pump type distillation cube system according to claim 3, characterized in that: Automatic valves are installed on the pipelines between the first-stage tower (13), second-stage tower (14), third-stage tower (15), fourth-stage tower (16), and fifth-stage tower (17) and the preheater (8). After the liquid material is heated, the automatic valves control the flow of the material into one of the first-stage tower (13), second-stage tower (14), third-stage tower (15), or fourth-stage tower (16) according to the different concentrations. The liquid in the first-stage tower (13) and the liquid in the reboiler (5) are combined and then enter the reboiler (5) through the first-stage pump (131). Through heat exchange with the refrigerant in the tubes, rising steam is generated. The liquid in the second-stage tower (14) enters the first-stage tower (13) through the second-stage pump (141) and merges with the liquid in the first-stage tower. The rising hot steam in (13) undergoes heat and mass exchange within the packing; the liquid in the third-stage tower (15) enters the second-stage tower (14) through the third-stage pump (151) and undergoes heat and mass exchange with the rising hot steam in the second-stage tower (14) within the packing; the liquid in the fourth-stage tower (16) enters the third-stage tower (15) through the fourth-stage pump (161) and undergoes heat and mass exchange with the rising hot steam in the third-stage tower (15) within the packing; the liquid in the fifth-stage tower (17) enters the fourth-stage tower (16) through the fifth-stage pump (171) and undergoes heat and mass exchange with the rising hot steam in the fourth-stage tower (16) within the packing; the steam from the top of the fifth-stage tower (17) is introduced into the preheater (8) for heat exchange with the raw material.

5. The heat pump type distillation cube system according to claim 1, characterized in that: Steam and a small amount of liquid material are introduced into the main condenser (1) through the preheater (8) via a pipeline. The main condenser (1) introduces a small amount of steam into the heat balance condenser (9) through a ventilation pipeline. The heat balance condenser (9) allows the liquid material to flow by gravity into the buffer tank (10) through a pipeline. The liquid in the buffer tank (10) flows back to the finished product cooler (12) through a pipeline. The finished product cooler (12) is connected to the qualified product storage tank through a pipeline. The qualified liquid product at room temperature is introduced into the qualified product storage tank through a pipeline.

6. The heat pump type distillation cube system according to claim 3, characterized in that: Each of the first-stage tower (13), second-stage tower (14), third-stage tower (15), fourth-stage tower (16), and fifth-stage tower (17) is equipped with a distribution plate and packing. The distribution plate is located at the top of each stage of the tower. The reflux liquid enters the distribution plate from the top of each stage of the tower and is evenly distributed before entering the packing. The liquid phase material that falls after heat and mass exchange at the bottom of each stage of the tower is pumped to the previous stage of the tower as reflux liquid for redistribution, so that each stage of the tower forms components of different concentrations, with the lowest concentration in the first stage of the tower.

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