CN221206852U - Heterogeneous azeotropic distillation combines anhydrous ethanol production system of heat pump - Google Patents
Heterogeneous azeotropic distillation combines anhydrous ethanol production system of heat pump Download PDFInfo
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- CN221206852U CN221206852U CN202323094568.8U CN202323094568U CN221206852U CN 221206852 U CN221206852 U CN 221206852U CN 202323094568 U CN202323094568 U CN 202323094568U CN 221206852 U CN221206852 U CN 221206852U
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 533
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 37
- 238000010533 azeotropic distillation Methods 0.000 title claims abstract description 25
- 235000019441 ethanol Nutrition 0.000 claims abstract description 173
- 230000018044 dehydration Effects 0.000 claims abstract description 160
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 160
- 238000011084 recovery Methods 0.000 claims abstract description 141
- 239000002904 solvent Substances 0.000 claims abstract description 137
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 39
- 238000010992 reflux Methods 0.000 claims description 46
- 239000002351 wastewater Substances 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 4
- 239000002994 raw material Substances 0.000 claims description 4
- 238000005265 energy consumption Methods 0.000 abstract description 28
- 238000005516 engineering process Methods 0.000 abstract description 14
- 239000000203 mixture Substances 0.000 abstract description 3
- 238000003912 environmental pollution Methods 0.000 abstract description 2
- 239000012071 phase Substances 0.000 description 52
- 239000000463 material Substances 0.000 description 27
- 238000000034 method Methods 0.000 description 16
- 238000000926 separation method Methods 0.000 description 15
- 230000008569 process Effects 0.000 description 10
- 239000012808 vapor phase Substances 0.000 description 8
- UHOVQNZJYSORNB-UHFFFAOYSA-N Benzene Chemical compound C1=CC=CC=C1 UHOVQNZJYSORNB-UHFFFAOYSA-N 0.000 description 6
- 239000000498 cooling water Substances 0.000 description 4
- 230000007613 environmental effect Effects 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 239000012528 membrane Substances 0.000 description 4
- 238000004064 recycling Methods 0.000 description 4
- 230000009286 beneficial effect Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000003960 organic solvent Substances 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- XDTMQSROBMDMFD-UHFFFAOYSA-N Cyclohexane Chemical compound C1CCCCC1 XDTMQSROBMDMFD-UHFFFAOYSA-N 0.000 description 2
- 238000013459 approach Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 230000005611 electricity Effects 0.000 description 2
- 230000006872 improvement Effects 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000002808 molecular sieve Substances 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000004065 wastewater treatment Methods 0.000 description 2
- 230000004075 alteration Effects 0.000 description 1
- 238000002485 combustion reaction Methods 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- IDGUHHHQCWSQLU-UHFFFAOYSA-N ethanol;hydrate Chemical compound O.CCO IDGUHHHQCWSQLU-UHFFFAOYSA-N 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 238000000895 extractive distillation Methods 0.000 description 1
- 239000004519 grease Substances 0.000 description 1
- 238000009776 industrial production Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000003607 modifier Substances 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
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- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model relates to a heterogeneous azeotropic distillation combined heat pump absolute ethyl alcohol production system, which comprises an ethyl alcohol dehydration tower and a solvent recovery tower which are sequentially communicated, and also comprises an ethyl alcohol dehydration tower heat pump compressor which is connected with the ethyl alcohol dehydration tower and is used for recovering heat of a light component azeotrope at the top of the ethyl alcohol dehydration tower, and a solvent recovery tower heat pump compressor which is connected with the solvent recovery tower and is used for recovering heat of a light component at the top of the solvent recovery tower. The utility model provides an absolute ethyl alcohol production system combining heterogeneous azeotropic distillation with a heat pump, which adopts a heterogeneous azeotropic distillation technology to remove water in an alcohol-water mixture so as to obtain high-purity absolute ethyl alcohol. Meanwhile, by combining with the heat pump energy-saving technology, the liquefied latent heat of the gas phase at the top of the rectifying tower can be recycled, so that the steam consumption for heat supply is greatly reduced, and the production energy consumption is reduced. The system has higher production efficiency and product quality, and has lower energy consumption and environmental pollution.
Description
Technical Field
The utility model relates to the field of absolute ethyl alcohol production, in particular to an absolute ethyl alcohol production system combining heterogeneous azeotropic rectification with a heat pump.
Background
Ethanol is a common organic solvent and is widely used in various fields including medicine, paint, sanitary products, cosmetics, grease, etc. Ethanol can be classified into three grades of industrial ethanol, edible ethanol and absolute ethanol according to different uses. The absolute ethanol refers to ethanol with the volume concentration of more than 99.5 percent, and the absolute ethanol can be used as renewable resources to partially replace fossil energy sources such as non-renewable petroleum and the like, so the production technology of the absolute ethanol is receiving wide attention. In recent years, absolute ethyl alcohol is widely used as a gasoline modifier, can improve the antiknock property of gasoline, eliminate lead pollution, improve combustion and reduce tail gas emission, and plays an increasingly important role in protecting environment.
In industrial production, the azeotrope contains about 95.8wt% of ethanol and 4.2wt% of water due to the azeotropic phenomenon of ethanol and water under normal pressure, and the water in the ethanol is difficult to remove by using a conventional separation means. The existing production method for preparing absolute ethyl alcohol by ethanol dehydration mainly comprises membrane separation, extractive distillation, molecular sieve adsorption, azeotropic distillation and the like. However, these methods all have some drawbacks. Wherein, the membrane separation needs to use a steam permeable membrane with larger area, and the higher the water content of the raw material is, the higher the water content of absolute ethyl alcohol after passing through the permeable membrane is, so that the ideal separation effect is difficult to achieve. The method combining extraction and rectification with molecular sieve adsorption has high energy consumption, and the extractant is easy to lose to cause waste. And compared with other methods, azeotropic distillation has the problems of huge energy consumption and the like.
Disclosure of utility model
In view of the above, the present utility model provides an anhydrous ethanol production system combining heterogeneous azeotropic distillation with a heat pump, which adopts a heterogeneous azeotropic distillation technology to remove water in an ethanol-water mixture and obtain ethanol with high concentration. Meanwhile, by combining with the heat pump energy-saving technology, the liquefied latent heat of the gas phase at the top of the azeotropic distillation tower can be recycled, so that the steam consumption for heat supply is greatly reduced, and the production energy consumption is reduced. The system has higher production efficiency and product quality, and has lower energy consumption and environmental pollution.
The aim of the utility model is achieved by the following technical scheme:
The heterogeneous azeotropic distillation combined heat pump anhydrous ethanol production system comprises an ethanol dehydration tower and a solvent recovery tower which are sequentially communicated, and further comprises an ethanol dehydration tower heat pump compressor connected with the ethanol dehydration tower and used for recovering heat of light component azeotrope at the top of the ethanol dehydration tower, and a solvent recovery tower heat pump compressor connected with the solvent recovery tower and used for recovering heat of light component at the top of the solvent recovery tower.
The absolute ethanol production system has the advantages that:
Firstly, the heterogeneous azeotropic rectification system is adopted to send the aqueous ethanol into an ethanol dehydration tower, and the water in the aqueous ethanol can be removed by adding an entrainer such as cyclohexane, benzene and other organic solvents. The tower top of the ethanol dehydration tower obtains ternary heterogeneous azeotrope of ethanol, water and entrainer, the tower bottom of the ethanol dehydration tower can obtain high-purity absolute ethanol, and the water content of the high-purity absolute ethanol is lower than 0.01 weight percent.
And secondly, cooling the ternary heterogeneous azeotrope obtained at the top of the ethanol dehydration tower, and layering in a reflux tank of the ethanol dehydration tower to obtain an oil phase and a water phase. The oil phase is totally refluxed and circulated back to the ethanol dehydration tower, and the water phase enters the solvent recovery tower for separation. Through the separation of the solvent recovery tower, the entrainer in the water phase can be recovered from the top of the solvent recovery tower, part of the entrainer is recycled to the solvent recovery tower after being cooled, and the other part of entrainer is returned to the ethanol dehydration tower, the wastewater is extracted from the bottom of the solvent recovery tower, and the COD of the wastewater can be lower than 1000mg/L.
Furthermore, by combining the heat pump energy-saving technology, the energy generated in the production process can be recycled, and the production energy consumption is reduced. The heat pump is a high-efficiency energy-saving technology which can convert low-temperature heat energy which cannot be directly utilized into available high-temperature heat energy and then is used by people. The heat pump technology has the advantages of being capable of converting low-quality heat energy into high-quality heat energy, high-efficiency, energy-saving and the like. By combining the heat pump energy-saving technology, the absolute ethyl alcohol production system not only has higher production efficiency and product purity, but also can greatly reduce energy consumption. In order to improve the energy utilization rate and reduce the energy consumption, the tower tops of the ethanol dehydration tower and the solvent recovery tower are used for supplying gas phase at the tower top to a tower kettle reboiler after the gas phase at the tower top is heated and boosted by adopting a heat pump compressor. In the reboiler, the gas phase material is condensed after heat supply, so that the liquefied latent heat of the gas phase at the top of the azeotropic distillation tower is recycled, and the heat supply steam consumption is greatly reduced. In the system operation process, except for the steam needed to be provided during the opening period, the two rectifying towers do not need to consume steam in other time, and only the two heat pump compressors are needed to be powered, so that the energy consumption is greatly reduced. By using this advanced process flow we can efficiently dehydrate ethanol and recover solvent while reducing energy consumption and environmental impact.
In particular, conventional rectifying columns typically employ circulating cooling water to condense the overhead vapor phase material, which is then fed into a reflux drum. However, this approach has some drawbacks. First, a large amount of circulating water needs to be consumed, which increases not only water consumption but also electricity consumption because the circulating pump needs to consume electric power to circulate the cooling water. Second, the latent heat of the overhead vapor phase is also wasted, as this heat is not recovered.
In contrast, these disadvantages can be overcome with heat pump rectification techniques. After the heat pump rectification is adopted, the gas phase material at the top of the tower is heated and boosted to proper temperature and pressure by a heat pump compressor, so that the saturation temperature of the gas phase at the top of the tower is higher than the operation temperature of a tower kettle. Thus, the gas phase at the top of the tower can supply heat to the tower kettle through the reboiler, and the gas phase is condensed into liquid phase during heat supply. Thus, the latent heat of liquefaction of the overhead vapor phase is recovered. Meanwhile, only a small amount of circulating water is needed to cool the liquefied material, so that heat consumption can be greatly reduced, and energy utilization efficiency is improved.
Preferably, the ethanol dehydration tower is provided with an ethanol dehydration tower reflux tank, an ethanol dehydration tower top condenser, an ethanol dehydration tower steam reboiler and an ethanol dehydration tower heat pump reboiler.
The steam reboiler of the ethanol dehydration tower is generally used for providing steam for the tower bottom of the ethanol dehydration tower in the start-up stage so as to improve the rectification efficiency of the ethanol dehydration tower. In the starting stage, the steam reboiler of the ethanol dehydration tower is required to provide steam to accelerate the evaporation process of materials and enable the system to reach a stable state as soon as possible. The heat pump reboiler of the ethanol dehydration tower heats the tower kettle material of the ethanol dehydration tower by taking the light component azeotrope after the temperature and the pressure of the top of the ethanol dehydration tower as a heat source, so that the liquefied latent heat of the gas phase of the light component azeotrope at the top of the ethanol dehydration tower can be effectively recycled, the heat is more fully utilized, and the energy consumption is reduced.
Preferably, the solvent recovery tower is provided with a solvent recovery tower reflux tank, a solvent recovery tower top condenser, a solvent recovery tower steam reboiler and a solvent recovery tower heat pump reboiler.
The solvent recovery tower steam reboiler is used for providing steam for the solvent recovery tower so as to promote evaporation and recovery of materials in the tower. In the start-up stage, as the materials in the solvent recovery tower are not completely recovered, steam needs to be provided to accelerate the recovery process and enable the system to reach a stable state as soon as possible. The heat pump reboiler of the solvent recovery tower heats the tower kettle material of the solvent recovery tower by taking the light component of the top of the solvent recovery tower after temperature and pressure rise as a heat source, so that the liquefied latent heat of the light component gas phase at the top of the solvent recovery tower can be effectively recycled, the heat is more fully utilized, and the energy consumption is reduced.
Preferably, the heat pump compressor of the ethanol dehydration tower is connected with a light component azeotrope pipeline at the top of the ethanol dehydration tower, and the light component azeotrope at the top of the ethanol dehydration tower is sent into the heat pump reboiler of the ethanol dehydration tower after being heated and boosted by the heat pump compressor of the ethanol dehydration tower and is used for supplying heat to the tower bottom of the ethanol dehydration tower.
After the light component azeotrope at the top of the ethanol dehydration tower is heated and boosted by the heat pump compressor of the ethanol dehydration tower, the light component azeotrope is used as a heat source of a reboiler of the ethanol dehydration tower to heat materials at the tower bottom of the ethanol dehydration tower, so that heat in the ethanol dehydration tower can be more fully utilized, and the energy consumption is reduced.
Preferably, the condenser at the top of the ethanol dehydration tower is connected with the outlet pipeline of the light component azeotrope of the heat pump reboiler of the ethanol dehydration tower, and the light component azeotrope of the heat pump reboiler of the ethanol dehydration tower enters the reflux tank of the ethanol dehydration tower after being cooled by the condenser at the top of the ethanol dehydration tower and is used for layering the light component azeotrope into an oil phase and a water phase.
The light component azeotrope of the heat pump reboiler of the ethanol dehydration tower is further condensed and separated through a condenser at the top of the ethanol dehydration tower, and the condensed light component azeotrope is layered through a reflux tank of the ethanol dehydration tower, wherein the upper layer is an oil phase, and the lower layer is a water phase. Thereby ensuring the full separation of oil phase and water phase, and the improvement of the separation effect can reduce the burden of the subsequent treatment process and improve the overall process efficiency.
Preferably, an oil phase pipeline at the upper part of the reflux tank of the ethanol dehydration tower is connected with a circulating pipeline of the ethanol dehydration tower through a reflux pump, and a water phase pipeline is connected with a feed pipeline of the solvent recovery tower through a feed pump.
The oil phase separated from the upper part of the reflux tank of the ethanol dehydration tower is returned to the ethanol dehydration tower for recycling through a reflux pump, and the water phase separated from the lower part of the reflux tank of the ethanol dehydration tower is sent into a solvent recovery tower through a feed pump for further separation, so that the recycling of the entrainer is realized, the consumption of the entrainer is reduced, and the cost is reduced.
Preferably, the heat pump compressor of the solvent recovery tower is connected with the light component line at the top of the solvent recovery tower, and the light component at the top of the solvent recovery tower is sent to the heat pump reboiler of the solvent recovery tower after being heated and boosted by the heat pump compressor of the solvent recovery tower and is used for supplying heat to the tower bottom of the solvent recovery tower.
After the temperature and pressure of the light component azeotrope at the top of the solvent recovery tower are increased by the heat pump compressor of the solvent recovery tower, the light component azeotrope is used as a heat source of the reboiler of the solvent recovery tower to heat the materials at the bottom of the solvent recovery tower, so that the heat in the ethanol dehydration tower can be more fully utilized, and the energy consumption is reduced.
Preferably, the inlet pipeline of the condenser at the top of the solvent recovery dehydration tower is connected with the outlet pipeline of the light component of the heat pump reboiler of the solvent recovery tower, the outlet pipeline of the condenser at the top of the solvent recovery dehydration tower is connected with the inlet pipeline of the reflux tank of the solvent recovery tower, one path of the outlet pipeline of the reflux tank of the solvent recovery tower is connected with the circulating line of the solvent recovery tower after being pressurized by the reflux pump, and the other path of the outlet pipeline of the reflux tank of the solvent recovery tower is connected with the return line of the ethanol dehydration tower.
The inlet pipeline of the tower top condenser of the solvent recovery dehydration tower is connected with the light component outlet pipeline of the heat pump reboiler of the solvent recovery tower, the light component of the heat pump reboiler of the solvent recovery tower is further condensed, the condensed light component enters the reflux tank of the solvent recovery tower, part of the condensed light component is circulated back to the solvent recovery tower through the reflux pump, the rectification efficiency of the solvent recovery tower is improved, and the part of condensed light component is returned to the ethanol dehydration tower, so that the recovery and utilization of the entrainer are realized.
Preferably, the ethanol dehydration tower is provided with a feed preheater, and the raw materials of the ethanol dehydration tower are fed into the ethanol dehydration tower after being heated by the feed preheater; and cooling an absolute ethyl alcohol product at the bottom of the ethyl alcohol dehydration tower by a feed preheater and then extracting.
The feed preheater is used for preheating the materials to be processed and improves the processing efficiency of the ethanol dehydration tower. The materials to be processed enter the ethanol dehydration tower after passing through the feed preheater, thereby being beneficial to reducing the energy consumption and improving the processing efficiency.
Preferably, the waste water in the tower bottom of the solvent recovery tower is pumped and pressurized to be extracted.
The waste water is pumped out from the bottom pumping outlet of the solvent recovery tower and is pumped out of the device after being boosted by the booster pump. The design can not only improve the efficiency of wastewater treatment, but also reduce the energy consumption and the environmental impact.
Compared with the prior art, the utility model has the beneficial effects that:
First, by using heterogeneous azeotropic distillation techniques, water in the aqueous ethanol mixture may be removed to yield high purity absolute ethanol having a water content of less than 0.01wt%.
Secondly, through the separation of the solvent recovery tower, the entrainer can be recovered from the top of the solvent recovery tower, and the COD of the wastewater extracted from the bottom of the solvent recovery tower is lower than 1000mg/L.
Thirdly, by combining the heat pump energy-saving technology, the vapor phase materials at the top of the ethanol dehydration tower and the solvent recovery tower are heated and boosted to proper temperature and pressure by the heat pump compressor and then supply heat to the tower kettle reboiler, so that the latent heat of liquefaction of the vapor phase materials at the top of the tower is recycled, the vapor consumption of heat supply of the ethanol dehydration tower and the solvent recovery tower is greatly reduced, the heat consumption is greatly reduced, and the energy utilization efficiency is improved.
Drawings
In order to more clearly illustrate the technical solutions of the embodiments of the present application, the drawings that are needed in the embodiments will be briefly described below, it being understood that the following drawings only illustrate some embodiments of the present application and therefore should not be considered as limiting the scope, and other related drawings may be obtained according to these drawings without inventive effort for a person skilled in the art.
FIG. 1 is a schematic diagram of a heterogeneous azeotropic distillation heat pump combined absolute ethanol production system according to an embodiment of the present utility model.
Description of the reference numerals:
The device comprises a feed preheater-1, an ethanol dehydration tower-2, an ethanol dehydration tower heat pump compressor-3, an ethanol dehydration tower top condenser-4, an ethanol dehydration tower reflux tank-5, an ethanol dehydration tower steam reboiler-6, an ethanol dehydration tower heat pump reboiler-7, a solvent recovery tower-8, a solvent recovery tower heat pump compressor-9, a solvent recovery tower top condenser-10, a solvent recovery tower reflux tank-11, a solvent recovery tower steam reboiler-12 and a solvent recovery tower heat pump reboiler-13.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present application more apparent, the technical solutions of the embodiments of the present application will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present application, and it is apparent that the described embodiments are some embodiments of the present application, but not all embodiments of the present application. The components of the embodiments of the present application generally described and illustrated in the figures herein may be arranged and designed in a wide variety of different configurations.
Thus, the following detailed description of the embodiments of the application, as presented in the figures, is not intended to limit the scope of the application, as claimed, but is merely representative of selected embodiments of the application. All other embodiments, which can be made by those skilled in the art based on the embodiments of the application without making any inventive effort, are intended to be within the scope of the application.
It should be noted that: like reference numerals and letters denote like items in the following figures, and thus once an item is defined in one figure, no further definition or explanation thereof is necessary in the following figures. In the description of the embodiments of the present application, it should be understood that the terms "upper", "lower", "left", "right", "vertical", "horizontal", etc. indicate orientations or positional relationships based on those shown in the drawings, or orientations or positional relationships that are conventionally put in use of the product of the application, or orientations or positional relationships that are conventionally understood by those skilled in the art, are merely for convenience in describing the present application and simplifying the description, and do not indicate or imply that the device or element to be referred to must have a specific orientation, be configured and operated in a specific orientation, and therefore should not be construed as limiting the present application.
It should be noted that, without conflict, the embodiments of the present application and features of the embodiments may be combined with each other.
The technical scheme of the application will be described below with reference to the accompanying drawings.
The embodiment provides a heterogeneous azeotropic distillation combined heat pump absolute ethyl alcohol production system, which comprises an ethyl alcohol dehydration tower 2 and a solvent recovery tower 8 which are sequentially communicated, wherein the absolute ethyl alcohol production system further comprises an ethyl alcohol dehydration tower heat pump compressor 3 connected with the ethyl alcohol dehydration tower 2 and used for recovering heat of light component azeotrope at the top of the ethyl alcohol dehydration tower 2, and a solvent recovery tower heat pump compressor 9 connected with the solvent recovery tower 8 and used for recovering heat of light component at the top of the solvent recovery tower 8.
The absolute ethanol production system has the advantages that:
Firstly, the heterogeneous azeotropic rectification system is adopted to send the aqueous ethanol into the ethanol dehydration tower 2, and the water in the aqueous ethanol can be removed by adding an entrainer such as cyclohexane, benzene and other organic solvents. The tower top of the ethanol dehydration tower 2 obtains ternary heterogeneous azeotrope of ethanol, water and entrainer, while the tower bottom of the ethanol dehydration tower 2 can obtain high-purity absolute ethanol, and the water content of the high-purity absolute ethanol is lower than 0.01 weight percent.
And secondly, layering the ternary heterogeneous azeotrope obtained at the top of the ethanol dehydration tower 2 in a reflux tank 5 of the ethanol dehydration tower after cooling to obtain an oil phase and a water phase. The oil phase is circulated back to the ethanol dehydration tower 2 in a total reflux way, and the water phase enters the solvent recovery tower 8 for separation. Through the separation of the solvent recovery tower 8, the entrainer in the water phase can be recovered from the top of the solvent recovery tower 8, part of the entrainer is recycled to the solvent recovery tower 8 after being cooled, and the other part of entrainer is returned to the ethanol dehydration tower 2, the wastewater is extracted from the tower bottom of the solvent recovery tower 8, and the COD of the wastewater can be lower than 1000 mg/L.
Furthermore, by combining the heat pump energy-saving technology, the energy generated in the production process can be recycled, and the production energy consumption is reduced. The heat pump is a high-efficiency energy-saving technology which can convert low-temperature heat energy which cannot be directly utilized into available high-temperature heat energy and then is used by people. The heat pump technology has the advantages of being capable of converting low-quality heat energy into high-quality heat energy, high-efficiency, energy-saving and the like. By combining the heat pump energy-saving technology, the absolute ethyl alcohol production system not only has higher production efficiency and product purity, but also can greatly reduce energy consumption. In order to improve the energy utilization rate and reduce the energy consumption, the tops of the ethanol dehydration tower 2 and the solvent recovery tower 8 are used for supplying gas phase at the top of the tower to a reboiler at the bottom of the tower after the gas phase is heated and boosted by adopting a heat pump compressor. In the reboiler, the gas phase material is condensed after heat supply, so that the liquefied latent heat of the gas phase at the top of the azeotropic distillation tower is recycled, and the heat supply steam consumption is greatly reduced. In the system operation process, except for the steam needed to be provided during the opening period, the two rectifying towers do not need to consume steam in other time, and only the two heat pump compressors are needed to be powered, so that the energy consumption is greatly reduced. By using this advanced process flow we can efficiently dehydrate ethanol and recover solvent while reducing energy consumption and environmental impact.
In particular, conventional rectifying columns typically employ circulating cooling water to condense the overhead vapor phase material, which is then fed into a reflux drum. However, this approach has some drawbacks. First, a large amount of circulating water needs to be consumed, which increases not only water consumption but also electricity consumption because the circulating pump needs to consume electric power to circulate the cooling water. Second, the latent heat of the overhead vapor phase is also wasted, as this heat is not recovered.
In contrast, these disadvantages can be overcome with heat pump rectification techniques. After the heat pump rectification is adopted, the gas phase material at the top of the tower is heated and boosted to proper temperature and pressure by a heat pump compressor, so that the saturation temperature of the gas phase at the top of the tower is higher than the operation temperature of a tower kettle. Thus, the gas phase at the top of the tower can supply heat to the tower kettle through the reboiler, and the gas phase is condensed into liquid phase during heat supply. Thus, the latent heat of liquefaction of the overhead vapor phase is recovered. Meanwhile, only a small amount of circulating water is needed to cool the liquefied material, so that heat consumption can be greatly reduced, and energy utilization efficiency is improved.
Preferably, the ethanol dehydration tower 2 is provided with an ethanol dehydration tower reflux tank 5, an ethanol dehydration tower top condenser 4, an ethanol dehydration tower steam reboiler 6 and an ethanol dehydration tower heat pump reboiler 7.
The ethanol dehydration tower steam reboiler 6 is generally used for providing steam for the tower bottom of the ethanol dehydration tower 2 in the start-up stage so as to improve the rectification efficiency of the ethanol dehydration tower 2. In the start-up stage, the steam reboiler 6 of the ethanol dehydration tower is required to provide steam to accelerate the evaporation process of materials and enable the system to reach a stable state as soon as possible. The heat pump reboiler 7 of the ethanol dehydration tower heats the materials at the tower bottom of the ethanol dehydration tower 2 by taking the light component azeotrope after the temperature and the pressure of the top of the ethanol dehydration tower 2 as a heat source, so that the liquefied latent heat of the gas phase of the light component azeotrope at the tower top of the ethanol dehydration tower 2 can be effectively recycled, the heat is more fully utilized, and the energy consumption is reduced.
Preferably, the solvent recovery tower 8 is provided with a solvent recovery tower reflux tank 11, a solvent recovery tower top condenser 10, a solvent recovery tower steam reboiler 12 and a solvent recovery tower heat pump reboiler 13.
The solvent recovery column steam reboiler 12 is used to provide steam to the solvent recovery column 8 to facilitate evaporation and recovery of the column contents. In the start-up phase, since the materials in the solvent recovery tower 8 are not completely recovered, it is necessary to provide steam to accelerate the recovery process and bring the system to a stable state as soon as possible. The heat pump reboiler 13 of the solvent recovery tower heats the tower kettle material of the solvent recovery tower 8 by taking the light component after the temperature and the pressure of the top of the solvent recovery tower 8 as a heat source, so that the liquefied latent heat of the light component gas phase at the top of the solvent recovery tower 8 can be effectively recycled, the heat is more fully utilized, and the energy consumption is reduced.
Preferably, the heat pump compressor 3 of the ethanol dehydration tower is connected with a light component azeotrope pipeline at the top of the ethanol dehydration tower 2, and the light component azeotrope at the top of the ethanol dehydration tower 2 is sent into the heat pump reboiler 7 of the ethanol dehydration tower after being heated and boosted by the heat pump compressor 3 of the ethanol dehydration tower for supplying heat to the tower kettle of the ethanol dehydration tower 2.
After the temperature and the pressure of the light component azeotrope at the top of the ethanol dehydration tower 2 are raised through the ethanol dehydration tower heat pump compressor 3, the light component azeotrope is used as a heat source of a reboiler of the ethanol dehydration tower 2 to heat materials at the tower bottom of the ethanol dehydration tower 2, so that the heat in the ethanol dehydration tower 2 can be more fully utilized, and the energy consumption is reduced.
Preferably, the condenser 4 at the top of the ethanol dehydration tower is connected with the outlet pipeline of the light component azeotrope of the heat pump reboiler 7 of the ethanol dehydration tower, and the light component azeotrope of the heat pump reboiler 7 of the ethanol dehydration tower enters the reflux tank 5 of the ethanol dehydration tower after being cooled by the condenser 4 at the top of the ethanol dehydration tower and is used for layering the light component azeotrope into an oil phase and a water phase.
The light component azeotrope of the heat pump reboiler 7 of the ethanol dehydration tower is further condensed and separated by the condenser 4 at the top of the ethanol dehydration tower, and the condensed light component azeotrope is layered by the reflux tank 5 of the ethanol dehydration tower, wherein the upper layer is an oil phase, and the lower layer is a water phase. Thereby ensuring the full separation of oil phase and water phase, and the improvement of the separation effect can reduce the burden of the subsequent treatment process and improve the overall process efficiency.
Preferably, an oil phase pipeline at the upper part of the reflux tank 5 of the ethanol dehydration tower is connected with a circulating pipeline of the ethanol dehydration tower 2 through a reflux pump, and a water phase pipeline is connected with a feed pipeline of the solvent recovery tower 8 through a feed pump.
The oil phase separated from the upper part of the ethanol dehydration tower reflux tank 5 is returned to the ethanol dehydration tower 2 for recycling through a reflux pump, and the water phase separated from the lower part of the ethanol dehydration tower reflux tank 5 is sent into the solvent recovery tower 8 for further separation through a feed pump, so that the recycling of the entrainer is realized, the consumption of the entrainer is reduced, and the cost is reduced.
Preferably, the heat pump compressor 9 of the solvent recovery tower is connected with the light component line at the top of the solvent recovery tower 8, and the light component at the top of the solvent recovery tower 8 is sent to the heat pump reboiler 13 of the solvent recovery tower after being heated and boosted by the heat pump compressor 9 of the solvent recovery tower and is used for supplying heat to the tower bottom of the solvent recovery tower 8.
After the temperature and pressure of the light component azeotrope at the top of the solvent recovery tower 8 are raised by the heat pump compressor 9 of the solvent recovery tower, the light component azeotrope is used as a heat source of a reboiler of the solvent recovery tower 8 to heat the material at the bottom of the solvent recovery tower 8, so that the heat in the ethanol dehydration tower 2 can be more fully utilized, and the energy consumption is reduced.
Preferably, the inlet pipeline of the condenser at the top of the solvent recovery dehydration tower is connected with the outlet pipeline of the light component of the heat pump reboiler 13 of the solvent recovery tower, the outlet pipeline of the condenser at the top of the solvent recovery dehydration tower is connected with the inlet pipeline of the reflux tank 11 of the solvent recovery tower, one path of the outlet pipeline of the reflux tank 11 of the solvent recovery tower is connected with the circulating line of the solvent recovery tower 8 after being pressurized by a reflux pump, and the other path of the outlet pipeline of the reflux tank is connected with the return line of the ethanol dehydration tower 2.
The inlet pipeline of the tower top condenser of the solvent recovery dehydration tower is connected with the light component outlet pipeline of the solvent recovery tower heat pump reboiler 13, the light component of the solvent recovery tower heat pump reboiler 13 is further condensed, the condensed light component enters the solvent recovery tower reflux tank 11, part of the condensed light component is circulated back to the solvent recovery tower 8 through the reflux pump, the rectification efficiency of the solvent recovery tower 8 is improved, and the part of the condensed light component is returned to the ethanol dehydration tower 2, so that the recovery and the utilization of the entrainer are realized.
Preferably, the ethanol dehydration tower 2 is provided with a feed preheater 1, and the raw materials of the ethanol dehydration tower 2 are fed into the ethanol dehydration tower 2 after being heated by the feed preheater 1; the absolute ethanol product at the bottom of the ethanol dehydration tower 2 is cooled by the feed preheater 1 and then extracted.
The feed preheater 1 is used for preheating the materials to be processed and improves the processing efficiency of the ethanol dehydration tower 2. The materials to be processed enter the ethanol dehydration tower 2 after passing through the feed preheater 1, which is beneficial to reducing energy consumption and improving treatment efficiency.
Preferably, the wastewater in the tower kettle of the solvent recovery tower 8 is pumped and pressurized to be extracted.
The waste water is pumped out from the bottom pumping outlet of the solvent recovery tower 8, and is pumped out of the device after being boosted by the booster pump. The design can not only improve the efficiency of wastewater treatment, but also reduce the energy consumption and the environmental impact.
Although embodiments of the present utility model have been shown and described, it will be understood by those skilled in the art that various changes, modifications, substitutions and alterations can be made therein without departing from the principles and spirit of the utility model, the scope of which is defined in the appended claims and their equivalents.
Claims (10)
1. The heterogeneous azeotropic distillation combined heat pump anhydrous ethanol production system comprises an ethanol dehydration tower and a solvent recovery tower which are sequentially communicated, and is characterized by further comprising an ethanol dehydration tower heat pump compressor which is connected with the ethanol dehydration tower and is used for recovering heat of light component azeotropes at the top of the ethanol dehydration tower, and a solvent recovery tower heat pump compressor which is connected with the solvent recovery tower and is used for recovering heat of light components at the top of the solvent recovery tower.
2. The heterogeneous azeotropic distillation heat pump-combined absolute ethyl alcohol production system according to claim 1, wherein the ethyl alcohol dehydration tower is provided with an ethyl alcohol dehydration tower reflux tank, an ethyl alcohol dehydration tower top condenser, an ethyl alcohol dehydration tower steam reboiler, and an ethyl alcohol dehydration tower heat pump reboiler.
3. The heterogeneous azeotropic distillation heat pump-combined absolute ethanol production system according to claim 1, wherein the solvent recovery tower is provided with a solvent recovery tower reflux tank, a solvent recovery tower top condenser, a solvent recovery tower steam reboiler, and a solvent recovery tower heat pump reboiler.
4. The heterogeneous azeotropic distillation heat pump-combined absolute ethyl alcohol production system according to claim 2, wherein the heat pump compressor of the ethyl alcohol dehydration tower is connected with a light component azeotrope pipeline at the top of the ethyl alcohol dehydration tower, and the light component azeotrope at the top of the ethyl alcohol dehydration tower is sent into the heat pump reboiler of the ethyl alcohol dehydration tower after being heated and boosted by the heat pump compressor of the ethyl alcohol dehydration tower.
5. The heterogeneous azeotropic rectification heat pump-combined absolute ethyl alcohol production system according to claim 2, wherein the condenser at the top of the ethyl alcohol dehydration tower is connected with the outlet pipeline of the light component azeotrope of the heat pump reboiler of the ethyl alcohol dehydration tower, and the light component azeotrope of the heat pump reboiler of the ethyl alcohol dehydration tower enters the reflux tank of the ethyl alcohol dehydration tower after being cooled by the condenser at the top of the ethyl alcohol dehydration tower.
6. The heterogeneous azeotropic distillation heat pump-combined absolute ethyl alcohol production system according to claim 5, wherein an upper oil phase pipeline of the reflux tank of the ethyl alcohol dehydration tower is connected with a circulating pipeline of the ethyl alcohol dehydration tower through a reflux pump, and a water phase pipeline is connected with a feed pipeline of the solvent recovery tower through a feed pump.
7. The heterogeneous azeotropic distillation heat pump-combined absolute ethyl alcohol production system according to claim 3, wherein the heat pump compressor of the solvent recovery tower is connected with the light component line at the top of the solvent recovery tower, and the light component at the top of the solvent recovery tower is sent to the heat pump reboiler of the solvent recovery tower after being heated and pressurized by the heat pump compressor of the solvent recovery tower.
8. The heterogeneous azeotropic distillation heat pump-combined absolute ethyl alcohol production system according to claim 7, wherein the inlet pipeline of the tower top condenser of the solvent recovery dehydrating tower is connected with the outlet pipeline of the light component of the heat pump reboiler of the solvent recovery tower, the outlet pipeline of the tower top condenser of the solvent recovery dehydrating tower is connected with the inlet pipeline of the reflux tank of the solvent recovery tower, one path of the outlet pipeline of the reflux tank of the solvent recovery tower is connected with the circulation line of the solvent recovery tower after being pressurized by the reflux pump, and the other path of the outlet pipeline of the reflux tank of the solvent recovery dehydrating tower is connected with the return line of the ethanol dehydrating tower.
9. The heterogeneous azeotropic distillation heat pump-combined absolute ethanol production system according to claim 1, wherein the ethanol dehydration tower is provided with a feed preheater, and the ethanol dehydration tower raw material is fed into the ethanol dehydration tower after being heated by the feed preheater; and cooling an absolute ethyl alcohol product at the bottom of the ethyl alcohol dehydration tower by a feed preheater and then extracting.
10. The heterogeneous azeotropic distillation heat pump-combined absolute ethyl alcohol production system according to claim 1, wherein the wastewater in the bottom of the solvent recovery tower is pumped and extracted.
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