CN212854692U - Fuel ethanol production device for optimizing heat supply through whole-process heat energy - Google Patents
Fuel ethanol production device for optimizing heat supply through whole-process heat energy Download PDFInfo
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- CN212854692U CN212854692U CN202020357332.6U CN202020357332U CN212854692U CN 212854692 U CN212854692 U CN 212854692U CN 202020357332 U CN202020357332 U CN 202020357332U CN 212854692 U CN212854692 U CN 212854692U
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Abstract
The utility model provides a fuel ethanol apparatus for producing of full process heat energy optimization heat supply, including rough distillation column, rectifying column, light wine tower, vapor compressor, molecular sieve dewatering system and DDGS device unit, rough distillation column, rectifying column, molecular sieve dewatering system and light wine tower all are equipped with the reboiler, the reboiler of rough distillation column is connected with the top of rectifying column and molecular sieve dewatering system respectively, the reboiler of rectifying column, molecular sieve dewatering system and light wine tower all is connected with vapor compressor gas phase entry, the gaseous phase entry end of rough distillation column with vapor compressor's steam outlet is linked together, and the gaseous phase exit end of DDGS device unit is connected with vapor compressor gas phase entry end. The utility model discloses can save the quantity of steam, guarantee the quality of product moreover.
Description
Technical Field
The utility model relates to an alcohol production technical field, especially a fuel ethanol apparatus for producing of heat supply is optimized to full process heat energy.
Background
At present, distillation purification of fuel ethanol, namely absolute alcohol, mainly uses a traditional differential pressure distillation section, and generally uses primary water vapor as a main heat supply source; the distillation mostly adopts multi-tower differential pressure distillation in the working sections as a main energy-saving technical means, the energy transmission among the working sections is mutually divided, a complete and optimized energy utilization system cannot be formed, and the steam consumption level is high.
Therefore, a solution to the above-mentioned problems is needed.
SUMMERY OF THE UTILITY MODEL
The utility model aims at providing a save the quantity of steam, guaranteed the fuel ethanol apparatus for producing of the heat supply is optimized to the full process heat energy of the quality of product moreover to the not enough of prior art.
In order to achieve the above purpose, the utility model adopts the following technical scheme: a full-process heat energy optimization heat supply fuel ethanol production device comprises a rough distillation tower, a rectification tower, a light wine tower, a steam compressor, a molecular sieve dehydration system and a DDGS device unit, wherein a feed inlet of the rough distillation tower is connected with a discharge outlet of a mash tank, the top of the rough distillation tower is connected with a feed inlet of the rectification tower, the top of the rectification tower is connected with the molecular sieve dehydration system, a discharge outlet of the rough distillation tower is connected with the DDGS device unit, a discharge outlet of the rectification tower is also connected with the light wine tower, and the light wine tower is also connected with the molecular sieve dehydration system; the distillation tower comprises a distillation tower body, a distillation tower, a molecular sieve dehydration system, a light wine tower and a DDGS device unit, wherein the distillation tower body is provided with a gas outlet end and a gas inlet end, the distillation tower body is provided with a gas inlet, the distillation tower body is provided with a gas outlet, the gas outlet end is connected with the gas inlet end, the gas inlet end is connected with the gas outlet end, the distillation tower body is provided with a gas outlet, the molecular sieve dehydration system is connected with the gas outlet end, the reboiler is connected with the gas inlet end, and the reboiler is connected with the gas outlet.
As a further improvement of the utility model: the rectifying tower and the light wine tower are indirectly heated by the raw steam.
As a further improvement of the utility model: the operation pressure at the top of the coarse distillation tower is-90 to-20 kPa, the temperature at the top of the coarse distillation tower is 45 to 85 ℃, and the temperature at the bottom of the coarse distillation tower is 50 to 90 ℃;
the operation pressure at the top of the rectifying tower is-90-10 kPa, the temperature at the top of the rectifying tower is 45-75 ℃, and the temperature at the bottom of the rectifying tower is 55-85 ℃;
the operation pressure of the top of the light wine tower is 50-300 kPa, the temperature of the top of the light wine tower is 90-115 ℃, and the temperature of the bottom of the light wine tower is 120-145 ℃;
the operating pressure of the molecular sieve dehydration system is-90-300 kPa, and the temperature is 60-130 ℃.
As a further improvement of the utility model: the DDGS device unit comprises separation equipment, drying equipment, a first-effect evaporation tower and a second-effect evaporation tower, wherein the separation equipment, the drying equipment, the first-effect evaporation tower and the second-effect evaporation tower are sequentially connected through a pipeline, a discharge hole of the second-effect evaporation tower is communicated with a feed inlet of the first-effect evaporation tower, a discharge hole of the separation equipment is communicated with a feed inlet of the second-effect evaporation tower, and a gas phase outlet end of the second-effect evaporation tower is communicated with a gas inlet of the steam compressor.
As a further improvement of the utility model: the separation equipment comprises a centrifuge and a plate-and-frame filter press.
As a further improvement of the utility model: the drying apparatus includes a dryer.
The utility model has the advantages of: the utility model discloses by the weak liquor tower, the rectifying column, the low temperature steam of molecular sieve dewatering system and DDGS workshop section output heats through vapor compressor compression, reach the heat supply to the rough distillation tower after the temperature of rough distillation tower technology demand, the top of the tower of rectifying column and molecular sieve dewatering system are by the heat supply of rough distillation tower, the not enough heat of rectifying column is supplemented through the reboiler by heat sources such as live steam, adopt vapor compressor as the heat supply, compress the dry waste steam and the evaporation steam of each workshop section and heat, as the main heat supply source of rough distillation, thereby integrate each workshop section into an organic whole, realize that workshop section mass energy link up the transmission, the quantity of steam has been saved; in addition, in the process of producing the fuel ethanol, the liquor in the rectifying tower and the light liquor tower is produced by adopting liquid-phase material passing, so that the quality of the product is ensured.
Drawings
Fig. 1 is a schematic view of the connection structure of the device of the present invention.
Detailed Description
The present invention will be further described with reference to the accompanying drawings, and it should be noted that the present embodiment is based on the technical solution, and the detailed embodiments and the specific operation processes are provided, but the protection scope of the present invention is not limited to the present embodiment.
Referring to fig. 1, a full-process heat energy optimized heat supply fuel ethanol production device comprises a rough distillation tower, a rectification tower, a light wine tower, a steam compressor, a molecular sieve dehydration system and a DDGS device unit, wherein a feed inlet of the rough distillation tower is connected with a discharge outlet of a mash tank, a tower top of the rough distillation tower is connected with a feed inlet of the rectification tower, a tower top of the rectification tower is connected with the molecular sieve dehydration system, a discharge outlet of the rough distillation tower is connected with the DDGS device unit, a discharge outlet of the rectification tower is connected with the light wine tower, and the light wine tower is also connected with the molecular sieve dehydration system.
The crude distillation tower, the rectifying tower, the molecular sieve dehydration system and the light wine tower are respectively provided with a reboiler, the reboiler of the crude distillation tower is respectively connected with the top of the rectifying tower and the molecular sieve dehydration system, the reboilers of the rectifying tower, the molecular sieve dehydration system and the light wine tower are respectively connected with a vapor inlet of a vapor compressor, the vapor inlet end of the crude distillation tower is communicated with a vapor outlet of the vapor compressor, and the vapor outlet end of the DDGS device unit is connected with the vapor inlet end of the vapor compressor.
The first embodiment is as follows:
in this embodiment, the light wine tower is indirectly heated by the raw steam, the DDGS device unit includes a separation device, a drying device, a first-effect evaporation tower and a second-effect evaporation tower, the separation device, the drying device, the first-effect evaporation tower and the second-effect evaporation tower are sequentially connected through a pipeline, a discharge port of the second-effect evaporation tower is communicated with a feed port of the first-effect evaporation tower, a discharge port of the separation device is communicated with a feed port of the second-effect evaporation tower, and a gas-phase outlet end of the second-effect evaporation tower is communicated with a gas inlet of the vapor compressor. The separation equipment comprises a centrifuge and a plate-and-frame filter press; the drying apparatus includes a dryer.
The operation parameters of each section are as follows:
the operation pressure at the top of the coarse distillation tower is-90 to-20 kPa, the temperature at the top of the coarse distillation tower is 45 to 85 ℃, and the temperature at the bottom of the coarse distillation tower is 50 to 90 ℃;
the operation pressure at the top of the rectifying tower is-90-10 kPa, the temperature at the top of the rectifying tower is 45-75 ℃, and the temperature at the bottom of the rectifying tower is 55-85 ℃;
the operation pressure of the top of the light wine tower is 50-300 kPa, the temperature of the top of the wine tower is 90-115 ℃, and the temperature of the bottom of the wine tower is 120-145 ℃;
the operating pressure of the molecular sieve dehydration system is-90-300 kPa, and the temperature is 60-130 ℃;
the operating pressure of the low-temperature steam of the DDGS section is as follows: -90 to-30 kPa, at a temperature of 35 to 90 ℃;
the operating pressure of the high-temperature steam of the steam compressor is-80 to-10 kPa, and the temperature is 60 to 100 ℃;
the operating pressure of the waste distiller's grains is 300-800 kPa, and the temperature is 60-100 ℃.
The working principle is as follows:
the method is characterized in that a crude distillation tower, a rectifying tower, a weak liquor tower and a molecular sieve dehydration system are operated for producing fuel ethanol, and the specific method comprises the following steps:
enabling self-fermented mature mash in the mash tank to enter a degassing section of a coarse distillation tower through a first preheater, and enabling the degassed mash to enter a stripping section of the coarse distillation tower; gas-phase crude wine vapor after distillation in the crude distillation tower enters a rectifying tower, the wine vapor taken out of the rectifying tower is divided into three parts, one part enters a vapor compressor through a reboiler, and the vapor compressor provides a heat source for the reboiler of the crude distillation tower; the second part is extracted from the bottom of the rectifying tower and enters a weak liquor tower after being preheated; and heating the third part and the liquor extracted from the weak liquor tower in a second preheater, and then dehydrating in a molecular sieve dehydration system to obtain the finished product fuel ethanol. And the mash discharged from the rough distillation tower is sent to a DDGS removing device unit for processing, and the mixed liquor rich in the fusel oil in the rectification tower enters a weak liquor tower for processing to extract the fusel oil.
In the process, low-temperature steam produced by a weak liquor tower, a rectifying tower, a molecular sieve dehydration system and a DDGS section is compressed and heated by a steam compressor to reach the temperature required by the process of the crude distillation tower and then is sent to the crude distillation tower for heat supply, the tower top of the rectifying tower and the molecular sieve dehydration system are heated by the crude distillation tower, the insufficient heat of the rectifying tower is supplemented by heat sources such as raw steam and the like through a reboiler, the steam compressor is used for heat supply, and the drying waste steam and the evaporation steam of each section are compressed and heated to be used as main heat supply sources for the crude distillation, so that each section is integrated into a whole, the section can realize through transmission, and the consumption of the steam is saved; in the process of producing the fuel ethanol, the rectifying tower and the weak liquor tower adopt liquid-phase material passing production, thereby ensuring the quality of products.
Various corresponding changes and modifications can be made by those skilled in the art according to the above technical solutions and concepts, and all such changes and modifications should be included in the protection scope of the present invention.
Claims (5)
1. The utility model provides a fuel ethanol apparatus for producing of heat supply is optimized to overall process heat energy which characterized in that: the device comprises a rough distillation tower, a rectifying tower, a light wine tower, a steam compressor, a molecular sieve dehydration system and a DDGS device unit, wherein a feed inlet of the rough distillation tower is connected with a discharge outlet of a mash tank, the top of the rough distillation tower is connected with a feed inlet of the rectifying tower, the top of the rectifying tower is connected with the molecular sieve dehydration system, a discharge outlet of the rough distillation tower is connected with the DDGS device unit, a discharge outlet of the rectifying tower is connected with the light wine tower, and the light wine tower is also connected with the molecular sieve dehydration system; the distillation tower comprises a distillation tower body, a distillation tower, a molecular sieve dehydration system, a light wine tower and a DDGS device unit, wherein the distillation tower body is provided with a gas outlet end and a gas inlet end, the distillation tower body is provided with a gas inlet, the distillation tower body is provided with a gas outlet, the gas outlet end is connected with the gas inlet end, the gas inlet end is connected with the gas outlet end, the distillation tower body is provided with a gas outlet, the molecular sieve dehydration system is connected with the gas outlet end, the reboiler is connected with the gas inlet end, and the reboiler is connected with the gas outlet.
2. The plant for producing fuel ethanol with optimized heat supply for the whole process according to claim 1, wherein: the weak liquor tower is indirectly heated by the raw steam.
3. The plant for producing fuel ethanol with optimized heat supply for the whole process according to claim 1, wherein: the DDGS device unit comprises separation equipment, drying equipment, a first-effect evaporation tower and a second-effect evaporation tower, wherein the separation equipment, the drying equipment, the first-effect evaporation tower and the second-effect evaporation tower are sequentially connected through a pipeline, a discharge hole of the second-effect evaporation tower is communicated with a feed inlet of the first-effect evaporation tower, a discharge hole of the separation equipment is communicated with a feed inlet of the second-effect evaporation tower, and a gas phase outlet end of the second-effect evaporation tower is communicated with a gas inlet of the steam compressor.
4. The plant for producing fuel ethanol with optimized heat supply for the whole process according to claim 3, wherein: the separation equipment comprises a centrifuge and a plate-and-frame filter press.
5. The plant for producing fuel ethanol with optimized heat supply for the whole process according to claim 3, wherein: the drying apparatus includes a dryer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020357332.6U CN212854692U (en) | 2020-03-19 | 2020-03-19 | Fuel ethanol production device for optimizing heat supply through whole-process heat energy |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN202020357332.6U CN212854692U (en) | 2020-03-19 | 2020-03-19 | Fuel ethanol production device for optimizing heat supply through whole-process heat energy |
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| Publication Number | Publication Date |
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| CN212854692U true CN212854692U (en) | 2021-04-02 |
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| CN202020357332.6U Active CN212854692U (en) | 2020-03-19 | 2020-03-19 | Fuel ethanol production device for optimizing heat supply through whole-process heat energy |
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Denomination of utility model: A Fuel Ethanol Production Device with Full Process Thermal Energy Optimization Heating Effective date of registration: 20230725 Granted publication date: 20210402 Pledgee: Societe Generale Bank Limited by Share Ltd. Guangzhou branch Pledgor: GUANGDONG ZHONGKE TIANYUAN NEW ENERGY SCIENCE & TECHNOLOGY Co.,Ltd. Registration number: Y2023980049753 |