CN111437619B - Multi-tower differential pressure energy-saving absolute alcohol distillation system and absolute alcohol energy-saving production method - Google Patents
Multi-tower differential pressure energy-saving absolute alcohol distillation system and absolute alcohol energy-saving production method Download PDFInfo
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- CN111437619B CN111437619B CN202010315835.1A CN202010315835A CN111437619B CN 111437619 B CN111437619 B CN 111437619B CN 202010315835 A CN202010315835 A CN 202010315835A CN 111437619 B CN111437619 B CN 111437619B
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 148
- 238000004821 distillation Methods 0.000 title claims abstract description 128
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 25
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 189
- 238000011084 recovery Methods 0.000 claims abstract description 96
- 238000005406 washing Methods 0.000 claims abstract description 49
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 49
- 238000001704 evaporation Methods 0.000 claims abstract description 21
- 230000008020 evaporation Effects 0.000 claims abstract description 21
- 239000002808 molecular sieve Substances 0.000 claims abstract description 19
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims abstract description 19
- 230000018044 dehydration Effects 0.000 claims abstract description 15
- 238000006297 dehydration reaction Methods 0.000 claims abstract description 15
- 239000002351 wastewater Substances 0.000 claims abstract description 4
- 238000003860 storage Methods 0.000 claims description 32
- 239000007788 liquid Substances 0.000 claims description 20
- 238000001179 sorption measurement Methods 0.000 claims description 18
- 238000010992 reflux Methods 0.000 claims description 13
- 239000002699 waste material Substances 0.000 claims description 11
- 238000000034 method Methods 0.000 claims description 10
- 238000001816 cooling Methods 0.000 claims description 9
- 238000009833 condensation Methods 0.000 claims description 2
- 230000005494 condensation Effects 0.000 claims description 2
- 238000005265 energy consumption Methods 0.000 abstract description 6
- 238000010438 heat treatment Methods 0.000 abstract description 6
- 239000007789 gas Substances 0.000 description 24
- 208000005156 Dehydration Diseases 0.000 description 11
- 238000000605 extraction Methods 0.000 description 5
- 238000004064 recycling Methods 0.000 description 4
- 239000001760 fusel oil Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000002537 cosmetic Substances 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 229940079593 drug Drugs 0.000 description 1
- 239000003814 drug Substances 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000284 extract Substances 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000011031 large-scale manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Classifications
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/001—Processes specially adapted for distillation or rectification of fermented solutions
- B01D3/003—Rectification of spirit
- B01D3/004—Rectification of spirit by continuous methods
- B01D3/005—Combined distillation and rectification
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
- B01D3/148—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step in combination with at least one evaporator
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/32—Other features of fractionating columns ; Constructional details of fractionating columns not provided for in groups B01D3/16 - B01D3/30
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
- Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
- Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)
Abstract
The invention discloses a multi-tower differential pressure energy-saving absolute alcohol distillation system and an absolute alcohol energy-saving production method, wherein the absolute alcohol distillation system comprises a multi-tower distillation device, an alcohol dehydration device and a heat conduction oil heating system; in the production process, coarse distillation and molecular sieve dehydration are carried out under the negative pressure environment; the heat conduction oil continuously provides a stable heat source for the rectifying tower heater, the alcohol evaporation heater and the superheater, the rectifying tower wine gas is used as the heat source of the water washing tower heater and the methanol tower heater, the water washing tower wine gas and the methanol tower wine gas are respectively used as the heat source of the first coarse distillation reboiler and the second coarse distillation reboiler of the coarse distillation tower, the waste water discharged by the rectifying tower and the recovery tower is used as the heat source of the recovery tower reboiler through the flash tank, and the recovery tower heater is matched with auxiliary heating. Therefore, in the whole production process of absolute alcohol, the initial heat energy is stable to supply, the generated heat energy can be recycled, the utilization rate of the heat energy is improved, the production efficiency is high, and the energy consumption is low.
Description
Technical Field
The invention relates to the technical field of absolute alcohol production, in particular to a multi-tower differential pressure energy-saving absolute alcohol distillation system and an absolute alcohol energy-saving production method.
Background
At present, the preparation of absolute alcohol mainly comprises the steps of obtaining edible alcohol with alcohol content of more than 95% through multi-tower distillation, and dehydrating the edible alcohol to obtain the absolute alcohol. The dehydration method mainly comprises an extraction method and an adsorption method, and the existing extraction method has the defects of high energy consumption, and the product can be clamped with an extractant, cannot be applied to the fields of foods, medicines, cosmetics and the like, and is not suitable for large-scale production. The adsorption method is widely popularized due to the high dehydration efficiency, few impurities and simple operation of the common molecular sieve adsorption method. For example, the Chinese patent publication No. CN 106495988B discloses an alcohol production process, in particular to a processing method of absolute alcohol of superior alcohol, which comprises the steps of distillation and dehydration. Five-tower distillation is carried out on the fermented mash, edible grade alcohol with the alcohol content of 95% -96% (v/v) is obtained after distillation, and dehydration treatment is carried out on the edible grade alcohol in a molecular sieve adsorption dehydration mode, so that anhydrous alcohol is obtained. Although the alcohol production method disclosed in this patent meets basic production requirements, it adopts steam generated by a boiler as a first heat source in a multi-tower distillation stage, and the energy consumption is large and the heat energy of the steam is unstable, resulting in low distillation efficiency. In addition, the secondary steam generated by the rectifying tower is not only used by the rectifying tower, but also used by the crude rectifying tower and the water washing tower, so that the heat energy of the secondary steam generated by the rectifying tower is insufficient for supplying the required heat energy, and the crude rectifying tower is easy to run out of wine and has unstable quality.
Disclosure of Invention
The invention aims to provide a multi-tower differential pressure energy-saving absolute alcohol distillation system with high production efficiency, high safety and low energy consumption and an absolute alcohol energy-saving production method.
In order to achieve the above purpose, the technical scheme adopted by the invention is as follows: the multi-tower differential pressure energy-saving absolute alcohol distillation system comprises a five-tower distillation device and an alcohol dehydration device, wherein the five-tower distillation device comprises a crude distillation tower, a water washing tower, a rectifying tower, a recovery tower and a methanol tower, and the top of the crude distillation tower is sequentially communicated with a crude distillation tower cooler, a crude distillation tower temporary storage tank, a crude distillation tower alcohol discharge pump and the water washing tower; the liquid outlet of the water washing tower is sequentially communicated with the liquid outlet pump of the water washing tower and the liquid inlet of the rectifying tower; the middle part of the recovery tower is connected with the middle part of the rectifying tower, and the top of the recovery tower is connected with the temporary storage tank of the recovery tower through an alcohol output pipe and a recovery tower cooler; the temporary storage tank of the recovery tower is connected with the upper part of the recovery tower through a reflux pump of the recovery tower; the wine extracting port of the recovery tower is communicated with the middle upper part of the rectifying tower, the wine extracting port of the rectifying tower is communicated with the middle upper part of the methanol tower, and the discharge port of the methanol tower is communicated with the finished product tank of the methanol tower; the method is characterized in that: the lower part of the crude distillation column is respectively connected with a first crude distillation reboiler and a second crude distillation reboiler, the lower parts of the water washing column, the rectifying column, the recovery column and the methanol column are respectively provided with a water washing column heater, a rectifying column heater, a recovery column heater and a methanol column heater, and the lower part of the recovery column is also connected with a recovery column reboiler; the top of the washing tower is communicated with a first crude distillation tower reboiler, a washing tower cooler, a temporary storage tank of the washing tower and a reflux pump of the washing tower respectively, and inlets and outlets of a heater of the washing tower and a heater of the methanol tower are communicated with the top of the rectifying tower and the temporary storage tank of the rectifying tower respectively; the waste liquid discharge ports of the rectifying tower and the recovery tower are connected with a flash tank, and the air outlet of the flash tank is communicated with a reboiler of the recovery tower; the top of the methanol tower is sequentially communicated with a reboiler of the second crude distillation tower, a cooler of the methanol tower, a temporary storage tank of the methanol tower, a reflux pump of the methanol tower and the middle part of the methanol tower through pipelines.
The alcohol dehydration device comprises an alcohol evaporation tank, a superheater, a molecular sieve adsorption device, an absolute alcohol cooler and an absolute alcohol temporary storage tank which are connected in sequence, wherein an alcohol evaporation heater is arranged at the lower part of the alcohol evaporation tank; the molecular sieve adsorption device is also connected with a light wine condenser and a light wine gas cooling recovery device, a light wine outlet of the light wine condenser is communicated with a light wine temporary storage tank, gas outlets of the light wine condenser and a crude distillation column cooler are respectively connected with a vacuum pump, and the light wine gas cooling recovery device and the light wine temporary storage tank are connected with the middle part of the recovery column through a light wine reflux pump.
The rectifying tower heater, the recovery tower heater, the alcohol evaporation heater and the superheater form a loop with the conduction oil boiler through conduction oil input and output pipelines.
Further, the crude distillation column cooler comprises a first crude distillation cooler, a second crude distillation cooler and a third crude distillation cooler which are connected in sequence. And a crude distillation preheater is further arranged between the crude distillation column and the first crude distillation cooler, a waste liquid outlet of the crude distillation column is connected with a spiral plate heat exchanger through a crude distillation waste liquid discharge pump, fermented mature mash is conveyed by a mash conveying pump, and the fermented mature mash is connected with the crude distillation column after sequentially passing through the crude distillation preheater and the spiral plate heat exchanger.
Further, the water washing tower cooler comprises a first water washing cooler and a second water washing cooler which are connected in sequence. The recovery tower cooler comprises a first recovery cooler, a second recovery cooler and a third recovery cooler. The methanol tower cooler comprises a first methanol cooler and a second methanol cooler which are sequentially connected.
Further, the light wine condenser comprises a first light wine cooler and a second light wine cooler; the light wine cooling recoverer comprises a steam tank and a gas phase cooler connected to the steam tank.
The invention also discloses an energy-saving production method of absolute alcohol by using the multi-tower differential pressure energy-saving absolute alcohol distillation device, which is characterized in that: separating by adopting differential pressure distillation branch, and distilling layer by a five-tower distillation device to obtain ethanol with concentration of 95% V/V; the five-tower distillation device generates finished alcohol, the finished alcohol is evaporated by an alcohol evaporation tank, enters a molecular sieve adsorption device through a heater to be adsorbed and dehydrated, and the absolute alcohol with the alcohol concentration of 99.95% V/V is obtained after condensation; the light wine produced by the molecular sieve adsorption device flows back to the recovery tower for circular distillation;
In the production process, the heat conduction oil provided by the heat conduction oil boiler continuously provides a stable heat source for the rectifying tower heater, the alcohol evaporation heater and the superheater, the wine gas coming out of the top of the rectifying tower is used as a heat source of the water washing tower heater and the methanol tower heater at the bottom of the methanol tower, the wine gas coming out of the top of the water washing tower is used as a heat source of the first coarse distillation reboiler, the wine gas coming out of the top of the methanol tower is used as a heat source of the second coarse distillation reboiler, the waste water discharged from the bottoms of the rectifying tower and the recovery tower is used as a heat source of the recovery tower reboiler through the flash tank, and the recovery tower heater is used as an auxiliary heat source of the recovery tower to regulate and maintain the temperature in the recovery tower within a proper range.
Further, the bottom temperature of the crude distillation column is 86-90 ℃, the pressure is 0.04-0.05 megapascal, the top temperature is 75-78, the pressure is 0.05-0.56 megapascal, the bottom temperature of the rectification column is 135-136 ℃, the pressure is 0.16-0.18 megapascal, the top temperature is 105-106 ℃, the recovery bottom temperature is 113-115, the top temperature is 95-97 ℃, the bottom temperature of the water washing column is 103-106 ℃, the top temperature is 93-95 ℃, the bottom temperature of the methanol column is 105-107, the top temperature is 95-98, the bottom temperature of the alcohol evaporator is 108-110 ℃, the pressure is-0.058-0.06 megapascal, the top temperature is 85-90 ℃, and the pressure is-0.043-0.05 megapascal.
The beneficial effects of the invention are as follows: by adopting the structure and the method, the heat conduction oil is used for continuously providing heat sources for the rectifying tower heater, the alcohol evaporation heater and the superheater, the heat conduction speed can be increased, the heat supply is stable, the energy consumption for producing absolute alcohol is low, the safety is high, and the problem of adopting water vapor as the heat source is avoided.
The invention can recycle the high-temperature wine gas generated by the rectifying tower, the water washing tower and the methanol tower as a heat source, and the rectifying tower can generate high-temperature and stable wine gas due to the heat supply of the heat conducting oil, thereby ensuring the heat requirements of the water washing tower heater and the methanol tower heater. The liquor gas generated by the water washing tower and the methanol tower is respectively used for supplying the first reboiler and the second reboiler of the crude distillation tower, so that the heat energy supply of the crude distillation tower is ensured, and the crude distillation efficiency is improved. The flash tank is arranged to utilize the waste liquid, secondary steam is generated for the recovery tower heater to use, when the temperature of the recovery tower does not reach the requirement, the recovery tower heater is used for auxiliary heating, the flow of heat conduction oil is controlled, and the recovery tower can be kept at a proper working temperature all the time in the production process.
Therefore, in the whole energy-saving production process of the absolute alcohol, the initial heat energy is stably supplied, the generated heat energy can be recycled, the utilization rate of the heat energy is improved, the production efficiency is high, and the energy consumption is low.
Drawings
The present invention will be described in further detail with reference to the accompanying drawings.
Fig. 1 is a schematic structural view of the present invention.
Detailed Description
As shown in FIG. 1, the multi-tower differential pressure energy-saving absolute alcohol distillation system comprises a five-tower distillation device and an alcohol dehydration device.
Wherein, five tower distillation plant includes crude distillation tower 1, washing tower 2, rectifying column 3, recovery tower 4 and methyl alcohol tower 5. The top of the crude distillation column 1 is sequentially communicated with a crude distillation column cooler 11, a crude distillation column temporary storage tank 12, a crude distillation column liquor discharge pump 13 and a water scrubber 2; the lower part of the crude distillation column 1 is respectively connected with a first crude distillation reboiler 14 and a second crude distillation reboiler 15. Specifically, the crude distillation column cooler 11 includes a first crude distillation cooler 111, a second crude distillation cooler 112, and a third crude distillation cooler 113, which are sequentially connected. A crude distillation preheater 16 is further arranged between the top of the crude distillation column 1 and the first crude distillation cooler 111, the waste liquid outlet of the crude distillation column 1 is connected with a spiral plate heat exchanger 18 through a crude distillation waste liquid discharge pump 17, fermented mature mash is conveyed by a mash conveying pump 10, and sequentially passes through the crude distillation preheater 16 and the spiral plate heat exchanger 18 and then is connected with the feed inlet of the crude distillation column 1.
The liquid outlet of the water washing tower 2 is sequentially communicated with a liquid outlet pump 21 of the water washing tower and a liquid inlet of the rectifying tower 3; the top of the water scrubber 2 is sequentially connected with a first crude distillation column reboiler 14, a water scrubber cooler 22 and a water scrubber temporary storage tank 23, and the water scrubber temporary storage tank 23 is connected with the middle upper part of the water scrubber through a water scrubber reflux pump 24 to form a circulating distillation loop. Specifically, the water scrubber cooler 22 includes a first water scrubber cooler 221 and a second water scrubber cooler 222 connected in sequence.
The middle part of the recovery tower 4 is connected with the middle part of the rectifying tower 3, and the top of the recovery tower 4 is connected with a recovery tower temporary storage tank 42 through an alcohol output pipe and a recovery tower cooler 41; the recovery tower temporary storage tank 42 is connected with the upper part of the recovery tower through a recovery tower reflux pump 43 to form a circulating distillation loop; the oil extraction port of the recovery tower is sequentially connected with a recovery tower fusel oil cooler 44 and a fusel oil temporary storage tank 45. Specifically, the recovery tower cooler 41 includes a first recovery cooler 411, a second recovery cooler 412, and a third recovery cooler 413.
The alcohol extraction port of the recovery tower 4 is communicated with the middle upper part of the rectifying tower 3, and the alcohol extraction port of the rectifying tower 3 is communicated with the middle upper part of the methanol tower 5.
The top of the methanol tower 5 is sequentially connected with a second crude distillation tower reboiler 15, a methanol tower cooler 51 and a methanol tower temporary storage tank 52 through pipelines, and the methanol tower temporary storage tank 52 is connected with the upper part of the methanol tower 5 through a methanol tower reflux pump 53 to form a circulating distillation loop; the discharge port of the methanol tower 5 is communicated with a finished product tank 54 of the methanol tower. Specifically, the methanol tower cooler 51 includes a first methanol cooler 511 and a second methanol cooler 512.
The lower parts of the water washing tower 2, the rectifying tower 3, the recovery tower 4 and the methanol tower 5 are respectively provided with a water washing tower heater 20, a rectifying tower heater 30, a recovery tower heater 40 and a methanol tower heater 50. The inlet and outlet of the water washing tower heater 20 and the methanol tower heater 50 are respectively communicated with the top of the rectifying tower 3 and the rectifying tower temporary storage tank 31, and the rectifying tower temporary storage tank 31 is communicated with the middle upper part of the rectifying tower through the rectifying reflux pump 32 to form a circulating distillation loop. The lower part of the recovery tower 4 is also connected with a recovery tower reboiler 47; the waste liquid discharge ports of the rectifying column 3 and the recovery column 4 are connected to a flash tank 46, and the gas outlet of the flash tank 46 is communicated with a recovery column reboiler 47.
The alcohol dehydration device comprises an alcohol evaporation tank 61, a superheater 62, a molecular sieve adsorption device 63, an anhydrous alcohol cooler 64 and an anhydrous alcohol temporary storage tank 65 which are sequentially connected, wherein an alcohol evaporation heater 611 is arranged at the lower part of the alcohol evaporation tank 61, and a methanol tower finished product tank 54 is communicated with the alcohol evaporation tank 61 through a finished product transfer pump 55. The molecular sieve adsorption device 63 is also connected with a light wine condenser 66 and a light wine gas cooling and recycling device 67, a light wine outlet of the light wine condenser 66 is communicated with a light wine temporary storage tank 68, gas outlets of the light wine condenser 66 and the crude distillation column cooler 11 are respectively connected with a vacuum pump 7, and wine gas generated in the light wine gas cooling and recycling device 67 and the light wine temporary storage tank 68 is refluxed to the recycling column 4 through a light wine reflux pump 69. The molecular sieve adsorption device 63 includes a first molecular sieve adsorber 631 and a first molecular sieve adsorber 632, and the two molecular sieve adsorbers alternately transport gas, wherein one adsorbs, and the other analyzes, and the dehydration of the wine gas is completed in cooperation. The light wine condenser 66 includes a first light wine cooler 661 and a second light wine cooler 662. The light wine gas cooling and recycling device 67 comprises a steam tank 671 and a gas phase cooler 672 connected to the steam tank, and the light wine gas is cooled by the gas phase cooler 672 and is subjected to gas-liquid separation.
The rectifying column heater 30, the recovery column heater 40, the alcohol evaporation heater 611 and the superheater 62 form a loop with the conduction oil boiler 8 through conduction oil input and output pipes. The outlet end of the heat conduction oil boiler 8 is provided with a heat conduction oil pump 81, and the oil inlet pipe and the oil outlet pipe connected with each heating component are respectively provided with a flow control valve 82, so that the heating temperature of the heating component can be controlled by controlling the oil quantity of the heat conduction oil.
The invention also discloses an energy-saving production method of absolute alcohol by using the multi-tower differential pressure energy-saving absolute alcohol distillation device, which specifically adopts differential pressure distillation branch technology, separates by layer-by-layer distillation of the five-tower distillation device, and extracts finished alcohol with the concentration of 95% V/V; the alcohol produced by the five-tower distillation device is evaporated by an alcohol evaporation tank 61, enters a molecular sieve adsorption device 63 through a heater 62 for adsorption and dehydration, and is condensed to obtain absolute alcohol with the alcohol concentration of 99.95 percent V/V; the light wine produced by the molecular sieve adsorption device flows back to the recovery tower 4 for circular distillation; the dehydrated absolute alcohol enters the absolute alcohol temporary storage tank 65, and can be discharged from the absolute alcohol product pump 92 after passing through the gauge 91.
In the production process, the heat conduction oil provided by the heat conduction oil boiler 7 continuously provides a stable heat source for the rectifying tower heater 30, the alcohol evaporation heater 611 and the superheater 62, the wine gas coming out of the top of the rectifying tower 3 is used as a heat source of a water washing tower heater and a methanol tower heater, the wine gas coming out of the top of the water washing tower 2 is used as a heat source of a first coarse distillation reboiler, the wine gas coming out of the top of the methanol tower 5 is used as a heat source of a second coarse distillation reboiler, the waste water discharged from the bottoms of the rectifying tower 3 and the recovery tower 4 is used as a heat source of a recovery tower reboiler through a flash tank, and the recovery tower heater 40 is used as an auxiliary heat source of the recovery tower to regulate and maintain the temperature in the recovery tower within a proper range.
Further, the bottom temperature of the crude distillation column is 86-90 ℃, the pressure is 0.04-0.05 megapascal, the top temperature is 75-78, the pressure is 0.05-0.56 megapascal, the bottom temperature of the rectification column is 135-136 ℃, the pressure is 0.16-0.18 megapascal, the top temperature is 105-106 ℃, the recovery bottom temperature is 113-115, the top temperature is 95-97 ℃, the bottom temperature of the water washing column is 103-106 ℃, the top temperature is 93-95 ℃, the bottom temperature of the methanol column is 105-107, the top temperature is 95-98, the bottom temperature of the alcohol evaporator is 108-110 ℃, the pressure is-0.058-0.06 megapascal, the top temperature is 85-90 ℃, and the pressure is-0.043-0.05 megapascal.
The invention has good energy-saving effect, and takes the production of 10 ten thousand tons of alcohol plants per year as an example by using the method of the invention. The method can reduce the discharge amount of waste mash by about 30-50 ten thousand m < 3 >, reduce the yield of discharged waste gas by 5000 ten thousand m < 3 >, reduce the discharge smoke dust by 600 tons and reduce the discharge of So < 2 > by about 1500 tons; the production cost of each ton of alcohol is reduced by about 400 yuan.
The foregoing is merely illustrative of the present invention, and simple modifications and equivalents may be made thereto by those skilled in the art without departing from the spirit and scope of the present invention.
Claims (6)
1. The multi-tower differential pressure energy-saving absolute alcohol distillation system comprises a five-tower distillation device and an alcohol dehydration device, wherein the five-tower distillation device comprises a crude distillation tower, a water washing tower, a rectifying tower, a recovery tower and a methanol tower, and the top of the crude distillation tower is sequentially communicated with a crude distillation tower cooler, a crude distillation tower temporary storage tank, a crude distillation tower alcohol discharge pump and the water washing tower; the liquid outlet of the water washing tower is sequentially communicated with the liquid outlet pump of the water washing tower and the liquid inlet of the rectifying tower; the middle part of the recovery tower is connected with the middle part of the rectifying tower, the top of the recovery tower is connected with a recovery tower temporary storage tank through an alcohol output pipe and a recovery tower cooler, and the recovery tower temporary storage tank is connected with the upper part of the recovery tower through a recovery tower reflux pump; the wine extracting port of the recovery tower is communicated with the middle upper part of the rectifying tower, the wine extracting port of the rectifying tower is communicated with the middle upper part of the methanol tower, and the discharge port of the methanol tower is communicated with the finished product tank of the methanol tower; the method is characterized in that: the lower part of the crude distillation column is respectively connected with a first crude distillation reboiler and a second crude distillation reboiler, the lower parts of the water washing column, the rectifying column, the recovery column and the methanol column are respectively provided with a water washing column heater, a rectifying column heater, a recovery column heater and a methanol column heater, and the lower part of the recovery column is also connected with a recovery column reboiler; the top of the washing tower is communicated with a first crude distillation tower reboiler, a washing tower cooler, a temporary storage tank of the washing tower and a reflux pump of the washing tower respectively, and inlets and outlets of a heater of the washing tower and a heater of the methanol tower are communicated with the top of the rectifying tower and the temporary storage tank of the rectifying tower respectively; the waste liquid discharge ports of the rectifying tower and the recovery tower are connected with a flash tank, and the air outlet of the flash tank is communicated with a reboiler of the recovery tower; the top of the methanol tower is sequentially communicated with a second crude distillation tower reboiler, a methanol tower cooler, a methanol tower temporary storage tank, a methanol tower reflux pump and the middle part of the methanol tower through pipelines;
the alcohol dehydration device comprises an alcohol evaporation tank, a superheater, a molecular sieve adsorption device, an absolute alcohol cooler and an absolute alcohol temporary storage tank which are connected in sequence, wherein an alcohol evaporation heater is arranged at the lower part of the alcohol evaporation tank; the molecular sieve adsorption device is also connected with a light wine condenser and a light wine gas cooling recovery device, a light wine outlet of the light wine condenser is communicated with a light wine temporary storage tank, gas outlets of the light wine condenser and a crude distillation column cooler are respectively connected with a vacuum pump, and the light wine gas cooling recovery device and the light wine temporary storage tank are connected with the middle part of the recovery column through a light wine reflux pump;
The rectifying tower heater, the recovery tower heater, the alcohol evaporation heater and the superheater form a loop with the conduction oil boiler through a conduction oil input and output pipeline;
the crude distillation column cooler comprises a first crude distillation cooler, a second crude distillation cooler and a third crude distillation cooler which are connected in sequence;
A crude distillation preheater is arranged between the crude distillation column and the first crude distillation cooler, a waste liquid outlet of the crude distillation column is connected with a spiral plate heat exchanger through a crude distillation waste liquid discharge pump, fermented mature mash is conveyed by a mash conveying pump, and is connected with the crude distillation column after sequentially passing through the crude distillation preheater and the spiral plate heat exchanger;
the light wine condenser comprises a first light wine cooler and a second light wine cooler; the light wine cooling recoverer comprises a steam tank and a gas phase cooler connected to the steam tank.
2. The multi-tower differential pressure energy-saving absolute alcohol distillation system according to claim 1, wherein: the water washing tower cooler comprises a first water washing cooler and a second water washing cooler which are sequentially connected.
3. The multi-tower differential pressure energy-saving absolute alcohol distillation system according to claim 1, wherein: the recovery tower cooler comprises a first recovery cooler, a second recovery cooler and a third recovery cooler.
4. The multi-tower differential pressure energy-saving absolute alcohol distillation system according to claim 1, wherein: the methanol tower cooler comprises a first methanol cooler and a second methanol cooler which are sequentially connected.
5. A process for the energy-efficient production of absolute alcohol using the multi-column differential pressure energy-efficient absolute alcohol distillation system according to any one of claims 1 to 4, characterized in that: separating by adopting differential pressure distillation branch, and distilling layer by a five-tower distillation device to obtain ethanol with concentration of 95% V/V; the five-tower distillation device generates finished alcohol, the finished alcohol is evaporated by an alcohol evaporation tank, enters a molecular sieve adsorption device through a heater to be adsorbed and dehydrated, and the absolute alcohol with the alcohol concentration of 99.95% V/V is obtained after condensation; the light wine produced by the molecular sieve adsorption device flows back to the recovery tower for circular distillation;
In the production process, the heat conduction oil provided by the heat conduction oil boiler continuously provides a stable heat source for the rectifying tower heater, the alcohol evaporation heater and the superheater, the wine gas coming out of the top of the rectifying tower is used as a heat source of the water washing tower heater and the methanol tower heater at the bottom of the methanol tower, the wine gas coming out of the top of the water washing tower is used as a heat source of the first coarse distillation reboiler, the wine gas coming out of the top of the methanol tower is used as a heat source of the second coarse distillation reboiler, the waste water discharged from the bottoms of the rectifying tower and the recovery tower is used as a heat source of the recovery tower reboiler through the flash tank, and the recovery tower heater is used as an auxiliary heat source of the recovery tower to regulate and maintain the temperature in the recovery tower within a proper range.
6. The energy-saving production method of absolute alcohol according to claim 5, characterized in that: the temperature of the bottom of the crude distillation column is 86-90 ℃, the pressure is 0.04-0.05 megapascal, the temperature of the top of the column is 75-78, the pressure is 0.05-0.56 megapascal, the temperature of the bottom of the distillation column is 135-136 ℃, the pressure is 0.16-0.18 megapascal, the temperature of the top of the column is 105-106 ℃, the temperature of the recovery column is 113-115, the temperature of the top of the column is 95-97 ℃, the temperature of the bottom of the water washing column is 103-106 ℃, the temperature of the top of the column is 93-95 ℃, the temperature of the bottom of the methanol column is 105-107, the temperature of the top of the column is 95-98, the temperature of the bottom of the alcohol evaporator is 108-110 ℃, the pressure is-0.058-0.06 megapascal, and the pressure of the temperature of the top of the column is 85-90 ℃ and the pressure is-0.043-0.05 megapascal.
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| CN202010315835.1A CN111437619B (en) | 2020-04-21 | 2020-04-21 | Multi-tower differential pressure energy-saving absolute alcohol distillation system and absolute alcohol energy-saving production method |
| PCT/CN2021/100334 WO2021213552A1 (en) | 2020-04-21 | 2021-06-16 | Multi-column differential pressure energy-saving anhydrous alcohol distillation system and anhydrous alcohol energy-saving production method |
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| CN111821712B (en) * | 2020-07-27 | 2022-04-05 | 广东中科天元新能源科技有限公司 | Seven-tower differential pressure distillation energy-saving production system and method for top-grade edible alcohol |
| CN113105309A (en) * | 2021-03-23 | 2021-07-13 | 江苏罗迈特生物科技有限公司 | Alcohol molecular sieve dehydration method |
| CN115368986A (en) * | 2022-08-15 | 2022-11-22 | 滨州中裕食品有限公司 | Method for producing alcohol with different grades by multi-tower distillation |
| CN115322862B (en) * | 2022-08-31 | 2024-07-30 | 宁波沪港食品机械制造有限公司 | Malt whisky distillation device and distillation process |
| CN116692775B (en) * | 2023-07-12 | 2024-05-07 | 深圳市超纯环保股份有限公司 | Low-concentration hydrofluoric acid waste liquid recovery equipment |
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| CA2518809C (en) * | 2003-03-28 | 2009-06-30 | Thermal Kinetics Systems, Llc | Ethanol distillation with distillers soluble solids recovery apparatus |
| CN201049932Y (en) * | 2007-05-10 | 2008-04-23 | 林国宁 | Multi-tower energy-saving distilling apparatus |
| CN201668968U (en) * | 2010-05-24 | 2010-12-15 | 中国轻工业西安设计工程有限责任公司 | An energy-saving system for the production of edible ethanol by five-tower three-stage differential pressure distillation |
| CN102716596B (en) * | 2012-07-06 | 2014-08-06 | 广东高科生物工程有限公司 | Five-tower differential-pressure energy-saving alcohol distillation device |
| US20190076751A1 (en) * | 2017-03-29 | 2019-03-14 | LucasE3, L.C. | Expanded distillation for ethanol production |
| US10596486B2 (en) * | 2017-09-21 | 2020-03-24 | Louis Phillip Nevitt | Plant matter fractional distillation system using heated air induction into precisely heated chamber to extract a plant's organic compounds without use of solvents |
| CN108531342B (en) * | 2018-03-16 | 2021-08-06 | 天津大学 | A kind of production method and equipment of neutral edible brewing alcohol product |
| JP6612961B1 (en) * | 2018-12-20 | 2019-11-27 | 木村化工機株式会社 | Distillation equipment |
| CN109776266A (en) * | 2019-02-28 | 2019-05-21 | 肥城金塔酒精化工设备有限公司 | A kind of energy-saving equipment and its power-economizing method producing absolute alcohol |
| CN111437619B (en) * | 2020-04-21 | 2024-08-02 | 广东高科生物工程有限公司 | Multi-tower differential pressure energy-saving absolute alcohol distillation system and absolute alcohol energy-saving production method |
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