CN111437619A - Multi-tower differential pressure energy-saving anhydrous alcohol distillation system and anhydrous alcohol energy-saving production method - Google Patents
Multi-tower differential pressure energy-saving anhydrous alcohol distillation system and anhydrous alcohol energy-saving production method Download PDFInfo
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- CN111437619A CN111437619A CN202010315835.1A CN202010315835A CN111437619A CN 111437619 A CN111437619 A CN 111437619A CN 202010315835 A CN202010315835 A CN 202010315835A CN 111437619 A CN111437619 A CN 111437619A
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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
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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
- B01D3/14—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
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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
- B01D3/14—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
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- 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
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- 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
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- 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
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- 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
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- 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
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Abstract
The invention discloses a multi-tower differential pressure energy-saving anhydrous alcohol distillation system and an anhydrous alcohol energy-saving production method, wherein the anhydrous alcohol distillation system comprises a multi-tower distillation device, an alcohol dehydration device and a heat conduction oil heat supply system; in the production process, the rough distillation and the molecular sieve dehydration are carried out in a negative pressure environment; the heat conducting oil continuously provides a stable heat source for the rectifying tower heater, the alcohol evaporation heater and the superheater, the rectifying tower alcohol gas is used as the heat source of the water washing tower heater and the methanol tower heater, the water washing tower alcohol gas and the methanol tower alcohol gas are respectively used as the heat source of the first crude distillation reboiler and the second crude distillation reboiler of the crude distillation tower, the wastewater discharged from the rectifying tower and the recovery tower generates secondary steam through the flash tank to be used as the heat source of the recovery tower reboiler, and the recovery tower heater is matched with the auxiliary heating. Therefore, in the whole production process of the anhydrous 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.
Description
Technical Field
The invention relates to the technical field of anhydrous alcohol production, in particular to a multi-tower differential pressure energy-saving anhydrous alcohol distillation system and an anhydrous alcohol energy-saving production method.
Background
At present, the preparation of the anhydrous alcohol is mainly to obtain edible alcohol with alcohol content of more than 95% by multi-tower distillation and then dehydrate the edible alcohol to obtain the anhydrous 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, inclusion of an extracting agent in a product, incapability of being applied to the fields of food, medicine, cosmetics and the like and unsuitability for large-scale production. The molecular sieve adsorption method commonly used in the adsorption method is greatly popularized due to high dehydration efficiency, less impurities and simple operation. For example, the patent of chinese invention with an issued publication number of CN106495988B discloses an alcohol production process, and particularly relates to a processing method of superior alcohol anhydrous alcohol, which comprises the steps of distillation and dehydration. Distilling the fermented mash in five towers to obtain edible alcohol with alcohol content of 95-96% (v/v), and dehydrating the edible alcohol by molecular sieve adsorption dehydration to obtain anhydrous alcohol. Although the method for producing alcohol disclosed in the patent can meet basic production requirements, the steam generated by a boiler is used as a first heat source in a multi-tower distillation stage, so that the energy consumption is high, the heat energy of the steam is unstable, and the distillation efficiency is low. In addition, the secondary steam generated by the rectifying tower is supplied to the coarse distillation tower and the water washing tower for use, so that the heat energy of the secondary steam generated by the rectifying tower is insufficient to supply the required heat energy, the coarse distillation tower is easy to run wine, and the quality is unstable.
Disclosure of Invention
The invention aims to provide a multi-tower differential pressure energy-saving anhydrous alcohol distillation system with high production efficiency, high safety and low energy consumption and an energy-saving anhydrous alcohol production method.
In order to achieve the purpose, the invention adopts the technical scheme that: a multi-tower differential pressure energy-saving anhydrous alcohol distillation system comprises a five-tower distillation device and an alcohol dehydration device, wherein the five-tower distillation device comprises a coarse distillation tower, a water washing tower, a rectification tower, a recovery tower and a methanol tower, and the top of the coarse distillation tower is sequentially communicated with a coarse distillation tower cooler, a coarse distillation tower temporary storage tank, a coarse distillation tower alcohol discharge pump and the water washing tower; the liquid outlet of the washing tower is communicated with a liquid outlet pump of the washing tower and a liquid inlet of the rectifying tower in sequence; the middle part of the recovery tower is connected with the middle part of the rectifying tower, and the top part of the recovery tower is connected with a temporary storage tank of the recovery tower through an alcohol output pipe and a cooler of the recovery tower; 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 liquor extracting port of the recovery tower is communicated with the middle upper part of the rectifying tower, the liquor 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 coarse distillation tower is respectively connected with a first coarse distillation reboiler and a second coarse distillation reboiler, the lower parts of the water wash tower, the rectification tower, the recovery tower and the methanol tower are respectively provided with a water wash tower heater, a rectification tower heater, a recovery tower heater and a methanol tower heater, and the lower part of the recovery tower is also connected with a recovery tower reboiler; the top of the washing tower forms a circulation loop with a first coarse distillation tower reboiler, a washing tower cooler, a temporary storage tank of the washing tower and a washing tower reflux pump, the inlets and the outlets of a washing tower heater and a methanol tower heater are respectively communicated with the top of the rectifying tower and the temporary storage tank of the rectifying tower, and the temporary storage tank of the rectifying tower is communicated with the middle upper part of the rectifying tower through the rectifying reflux pump; the waste liquid discharge ports of the rectifying tower and the recovery tower are connected with a flash tank, and the gas outlet of the flash tank is communicated with a reboiler of the recovery tower; the top of the methanol tower is communicated with a second coarse distillation tower reboiler, a methanol tower cooler, a methanol tower temporary storage tank, a methanol tower reflux pump and the middle of the methanol tower in sequence through a pipeline.
The alcohol dehydration device comprises an alcohol evaporation tank, a superheater, a molecular sieve adsorption device, an anhydrous alcohol cooler and an anhydrous alcohol temporary storage tank which are sequentially connected, and 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 cooling recoverer, a light wine outlet of the light wine condenser is communicated with a light wine temporary storage tank, gas discharge ports of the light wine condenser and the rough distillation tower cooler are respectively connected with a vacuum pump, and the light wine cooling recoverer and the light wine temporary storage tank are connected with the middle part of the recovery tower 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 heat conduction oil boiler through a heat conduction oil input and output pipeline.
Further, the rough distillation tower cooler comprises a first rough distillation cooler, a second rough distillation cooler and a third rough distillation cooler which are connected in sequence. A coarse distillation preheater is arranged between the coarse distillation tower and the first coarse distillation cooler, a waste liquid outlet of the coarse distillation tower is connected with a spiral plate heat exchanger through a coarse distillation waste liquid discharge pump, fermented mature mash is conveyed through a mash conveying pump and is connected with the coarse distillation tower after sequentially passing through the coarse 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 weak liquor condenser comprises a first weak liquor cooler and a second weak liquor cooler; the fresh wine cooling recoverer comprises a steam tank and a gas phase cooler connected to the steam tank.
The invention also discloses an energy-saving anhydrous alcohol production method by utilizing the multi-tower differential pressure energy-saving anhydrous alcohol distillation device, which is characterized by comprising the following steps of: separating by adopting differential pressure distillation and layer-by-layer distillation of a five-tower distillation device, and extracting finished alcohol with the concentration of 95% V/V; evaporating the finished product alcohol generated by the five-tower distillation device by an alcohol evaporation tank, then entering a molecular sieve adsorption device through a heater for adsorption and dehydration, and condensing to obtain anhydrous alcohol with the alcohol concentration of 99.95% V/V; 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 alcohol gas coming out of the top of the rectifying tower is used as the heat source of the water scrubber heater and the methanol tower heater at the bottom of the methanol tower, the alcohol gas coming out of the top of the water scrubber is used as the heat source of the first crude distillation reboiler, the alcohol gas coming out of the top of the methanol tower is used as the heat source of the second crude distillation reboiler, the wastewater discharged from the bottoms of the rectifying tower and the recovery tower passes through the vacuum flash tank to generate secondary steam which is used as the heat source of the reboiler of the recovery tower, and the heater of the recovery tower is used as an auxiliary heat source of the recovery tower to adjust and maintain the temperature in.
Further, the temperature of the bottom of the rough distillation tower is 86-90 ℃, the pressure is 0.04-0.05 MPa, the temperature of the top of the tower is 75-78, the pressure is 0.05-0.56 MPa, the temperature of the bottom of the rectification tower is 135-136 ℃, the pressure is 0.16-0.18 MPa, the temperature of the top of the tower is 105-106 ℃, the temperature of the bottom of the recovery tower is 113-115, the temperature of the top of the tower is 95-97 ℃, the temperature of the bottom of the washing tower is 103-106 ℃, the temperature of the top of the tower is 93-95 ℃, the temperature of the bottom of the methanol tower is 105-107, the temperature of the top of the tower is 95-98, the temperature of the bottom of the alcohol evaporator is 108-110 ℃, the pressure is-0.058-0.06 MPa, the.
The invention has the beneficial effects that: 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 the anhydrous 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 heat sources, and the rectifying tower adopts heat-conducting oil for heat supply, so that the wine gas with high and stable temperature can be generated, and the heat requirements of the water washing tower heater and the methanol tower heater can be ensured. The wine gas generated by the water washing tower and the methanol tower is respectively used for supplying a first reboiler and a 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. Set up the true jar of sudden strain of a muscle and can utilize the waste liquid, produce the secondary steam and supply the recovery tower heater to use, when the temperature of recovery tower does not reach the requirement, through recovery tower heater boosting to control heat conduction oil flow, guarantee that recovery tower can maintain suitable operating temperature always in process of production.
Therefore, in the whole anhydrous alcohol energy-saving production process, 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 diagram of the present invention.
Detailed Description
As shown in figure 1, the multi-tower differential pressure energy-saving anhydrous 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 1, a water washing tower 2, a rectifying tower 3, a recovery tower 4 and a methanol tower 5. The top of the crude distillation tower 1 is communicated with a crude distillation tower cooler 11, a crude distillation tower temporary storage tank 12, a crude distillation tower alcohol discharge pump 13 and a water washing tower 2 in sequence; the lower part of the rectifying column 1 is connected with a first rectifying reboiler 14 and a second rectifying reboiler 15, respectively. Specifically, the rough distillation tower cooler 11 includes a first rough distillation cooler 111, a second rough distillation cooler 112, and a third rough distillation cooler 113 connected in sequence. A rough distillation preheater 16 is arranged between the top of the rough distillation tower 1 and the first rough distillation cooler 111, a waste liquid outlet of the rough distillation tower 1 is connected with a spiral plate heat exchanger 18 through a rough distillation waste liquid discharge pump 17, fermented mature mash is conveyed through a mash conveying pump 10 and is connected with a feed inlet of the rough distillation tower 1 after sequentially passing through the rough distillation preheater 16 and the spiral plate heat exchanger 18.
A liquid outlet of the water washing tower 2 is communicated with a liquid outlet pump 21 of the water washing tower and a liquid inlet of the rectifying tower 3 in sequence; the top of the washing tower 2 is sequentially connected with a first coarse distillation tower reboiler 14, a washing tower cooler 22 and a washing tower temporary storage tank 23, and the washing tower temporary storage tank 23 is connected with the middle upper part of the washing tower through a washing tower reflux pump 24 to form a circulating distillation loop. Specifically, the water wash tower cooler 22 includes a first water wash cooler 221 and a second water wash cooler 222 connected in series.
The middle part of the recovery tower 4 is connected with the middle part of the rectifying tower 3, and the top part of the recovery tower 4 is connected with a temporary storage tank 42 of the recovery tower through an alcohol output pipe by a cooler 41 of the recovery tower; the temporary storage tank 42 of the recovery tower is connected with the upper part of the recovery tower through a reflux pump 43 of the recovery tower to form a circulating distillation loop; the oil extraction port of the recovery tower is sequentially connected with a fusel oil cooler 44 and a fusel oil temporary storage tank 45 of the recovery tower. Specifically, the recovery tower cooler 41 includes a first recovery cooler 411, a second recovery cooler 412, and a third recovery cooler 413.
The liquor extraction port of the recovery tower 4 is communicated with the middle upper part of the rectifying tower 3, and the liquor 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 rough 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 hole of the methanol tower 5 is communicated with a methanol tower finished product tank 54. Specifically, the methanol tower cooler 51 includes a first methanol cooler 511 and a second methanol cooler 512.
The lower parts of the wash column 2, the rectifying column 3, the recovery column 4 and the methanol column 5 are provided with a wash column heater 20, a rectifying column heater 30, a recovery column heater 40 and a methanol column heater 50, respectively. The inlets and outlets of the wash tower heater 20 and the methanol tower heater 50 are respectively communicated with the top of the rectifying tower 3 and the temporary storage tank 31 of the rectifying tower, and the temporary storage tank 31 of the rectifying tower is communicated with the middle upper part of the rectifying tower through a 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 tower 3 and the recovery tower 4 are connected with a flash tank 46, and the gas outlet of the flash tank 46 is communicated with a recovery tower 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, 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 cooling recoverer 67, a light wine outlet of the light wine condenser 66 is communicated with a light wine temporary storage tank 68, gas exhaust ports of the light wine condenser 66 and the rough distillation tower cooler 11 are respectively connected with a vacuum pump 7, and wine gas generated in the light wine cooling recoverer 67 and the light wine temporary storage tank 68 flows back to the recovery tower 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, where the two molecular sieve adsorbers alternately transport gas, one of the two molecular sieve adsorbers adsorbs gas, and the other molecular sieve adsorber analyzes gas to complete the dehydration of the alcohol gas. The weak liquor condenser 66 includes a first weak liquor cooler 661 and a second weak liquor cooler 662. The weak liquor cooling recoverer 67 comprises a steam tank 671 and a gas phase cooler 672 connected to the steam tank, and is used for cooling weak liquor gas and completing gas-liquid separation through the gas phase cooler 672.
The rectifying tower heater 30, the recovery tower heater 40, the alcohol evaporation heater 611 and the superheater 62 form a loop with the heat conduction oil boiler 8 through a heat conduction oil input and output pipeline. The outlet end of the heat conducting oil boiler 8 is provided with a heat conducting oil pump 81, an oil inlet pipe and an oil outlet pipe which are connected with each heating part are respectively provided with a flow control valve 82, and then the heating temperature of the heating parts can be controlled by controlling the oil quantity of the heat conducting oil.
The invention also discloses an energy-saving anhydrous alcohol production method utilizing the multi-tower differential pressure energy-saving anhydrous alcohol distillation device, which particularly adopts differential pressure distillation technology, separates by layer distillation of a five-tower distillation device, and extracts finished alcohol with the concentration of 95% V/V; evaporating the finished product alcohol generated by the five-tower distillation device by an alcohol evaporation tank 61, then passing through a heater 62, entering a molecular sieve adsorption device 63 for adsorption and dehydration, and condensing to obtain anhydrous alcohol with the alcohol concentration of 99.95% V/V; the light wine generated 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 by an absolute alcohol finished product pump 92 after passing through a meter 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 alcohol gas coming out of the top of the rectifying tower 3 is used as the heat source of the water scrubber heater and the methanol tower heater, the alcohol gas coming out of the top of the water scrubber 2 is used as the heat source of the first crude distillation reboiler, the alcohol gas coming out of the top of the methanol tower 5 is used as the heat source of the second crude distillation reboiler, the wastewater discharged from the bottoms of the rectifying tower 3 and the recovery tower 4 passes through the flash tank to generate secondary steam which is used as the heat source of the recovery tower reboiler, the recovery tower heater 40 is used as an auxiliary heat source of the recovery tower, and the temperature in the recovery tower is adjusted and maintained within a proper range.
Further, the temperature of the bottom of the rough distillation tower is 86-90 ℃, the pressure is 0.04-0.05 MPa, the temperature of the top of the tower is 75-78, the pressure is 0.05-0.56 MPa, the temperature of the bottom of the rectification tower is 135-136 ℃, the pressure is 0.16-0.18 MPa, the temperature of the top of the tower is 105-106 ℃, the temperature of the bottom of the recovery tower is 113-115, the temperature of the top of the tower is 95-97 ℃, the temperature of the bottom of the washing tower is 103-106 ℃, the temperature of the top of the tower is 93-95 ℃, the temperature of the bottom of the methanol tower is 105-107, the temperature of the top of the tower is 95-98, the temperature of the bottom of the alcohol evaporator is 108-110 ℃, the pressure is-0.058-0.06 MPa, the.
The invention has good energy-saving effect, and takes the production of 10 ten thousand tons of alcohol plants every year by using the method of the invention as an example. The method can reduce the discharge amount of waste mash by about 30-50 ten thousand m3, reduce the discharge amount of waste gas by 5000 ten thousand m3, reduce the discharge amount of smoke dust by 600 tons, and reduce the discharge amount of So2 by about 1500 tons; the production cost of each ton of alcohol is reduced by about 400 yuan.
The above description is only for the purpose of illustrating the technical solutions of the present invention, and those skilled in the art can make simple modifications or equivalent substitutions on the technical solutions of the present invention without departing from the spirit and scope of the technical solutions of the present invention.
Claims (9)
1. A multi-tower differential pressure energy-saving anhydrous alcohol distillation system comprises a five-tower distillation device and an alcohol dehydration device, wherein the five-tower distillation device comprises a coarse distillation tower, a water washing tower, a rectification tower, a recovery tower and a methanol tower, and the top of the coarse distillation tower is sequentially communicated with a coarse distillation tower cooler, a coarse distillation tower temporary storage tank, a coarse distillation tower alcohol discharge pump and the water washing tower; the liquid outlet of the washing tower is communicated with a liquid outlet pump of the washing tower and a liquid inlet of the rectifying tower in sequence; the middle part of the recovery tower is connected with the middle part of the rectifying tower, the top part of the recovery tower is connected with a temporary storage tank of the recovery tower through an alcohol output pipe and a cooler of the recovery tower, and 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 liquor extracting port of the recovery tower is communicated with the middle upper part of the rectifying tower, the liquor 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 coarse distillation tower is respectively connected with a first coarse distillation reboiler and a second coarse distillation reboiler, the lower parts of the water wash tower, the rectification tower, the recovery tower and the methanol tower are respectively provided with a water wash tower heater, a rectification tower heater, a recovery tower heater and a methanol tower heater, and the lower part of the recovery tower is also connected with a recovery tower reboiler; the top of the washing tower forms a circulation loop with a first coarse distillation tower reboiler, a washing tower cooler, a temporary storage tank of the washing tower and a washing tower reflux pump, the inlets and the outlets of a washing tower heater and a methanol tower heater are respectively communicated with the top of the rectifying tower and the temporary storage tank of the rectifying tower, and the temporary storage tank of the rectifying tower is communicated with the middle upper part of the rectifying tower through the rectifying reflux pump; the waste liquid discharge ports of the rectifying tower and the recovery tower are connected with a flash tank, and the gas 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 coarse 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 anhydrous alcohol cooler and an anhydrous alcohol temporary storage tank which are sequentially connected, and 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 cooling recoverer, a light wine outlet of the light wine condenser is communicated with a light wine temporary storage tank, gas discharge ports of the light wine condenser and the rough distillation tower cooler are respectively connected with a vacuum pump, and the light wine cooling recoverer and the light wine temporary storage tank are connected with the middle part of the recovery tower 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 heat conduction oil boiler through a heat conduction oil input and output pipeline.
2. The multi-tower differential pressure energy-saving anhydrous alcohol distillation apparatus according to claim 1, wherein: the rough distillation tower cooler comprises a first rough distillation cooler, a second rough distillation cooler and a third rough distillation cooler which are connected in sequence.
3. The multi-tower differential pressure energy-saving anhydrous alcohol distillation apparatus according to claim 2, wherein: a coarse distillation preheater is arranged between the coarse distillation tower and the first coarse distillation cooler, a waste liquid outlet of the coarse distillation tower is connected with a spiral plate heat exchanger through a coarse distillation waste liquid discharge pump, fermented mature mash is conveyed through a mash conveying pump and is connected with the coarse distillation tower after sequentially passing through the coarse distillation preheater and the spiral plate heat exchanger.
4. The multi-tower differential pressure energy-saving anhydrous alcohol distillation apparatus 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.
5. The multi-tower differential pressure energy-saving anhydrous alcohol distillation apparatus according to claim 1, wherein: the recovery tower cooler comprises a first recovery cooler, a second recovery cooler and a third recovery cooler.
6. The multi-tower differential pressure energy-saving anhydrous alcohol distillation apparatus according to claim 1, wherein: the methanol tower cooler comprises a first methanol cooler and a second methanol cooler which are sequentially connected.
7. The multi-tower differential pressure energy-saving anhydrous alcohol distillation apparatus according to claim 1, wherein: the weak liquor condenser comprises a first weak liquor cooler and a second weak liquor cooler; the fresh wine cooling recoverer comprises a steam tank and a gas phase cooler connected to the steam tank.
8. An energy-saving anhydrous alcohol production method using the multi-tower differential pressure energy-saving anhydrous alcohol distillation apparatus according to any one of claims 1 to 7, characterized in that: separating by adopting differential pressure distillation and layer-by-layer distillation of a five-tower distillation device, and extracting finished alcohol with the concentration of 95% V/V; evaporating the finished product alcohol generated by the five-tower distillation device by an alcohol evaporation tank, then entering a molecular sieve adsorption device through a heater for adsorption and dehydration, and condensing to obtain anhydrous alcohol with the alcohol concentration of 99.95% V/V; 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 alcohol gas coming out of the top of the rectifying tower is used as the heat source of the water scrubber heater and the methanol tower heater at the bottom of the methanol tower, the alcohol gas coming out of the top of the water scrubber is used as the heat source of the first crude distillation reboiler, the alcohol gas coming out of the top of the methanol tower is used as the heat source of the second crude distillation reboiler, the wastewater discharged from the bottoms of the rectifying tower and the recovery tower passes through the vacuum flash tank to generate secondary steam which is used as the heat source of the reboiler of the recovery tower, and the heater of the recovery tower is used as an auxiliary heat source of the recovery tower to adjust and maintain the temperature in.
9. The energy-saving production method of anhydrous alcohol according to claim 8, characterized in that: the temperature of the bottom of the rough distillation tower is 86-90 ℃, the pressure is 0.04-0.05 MPa, the temperature of the top of the tower is 75-78, the pressure is 0.05-0.56 MPa, the temperature of the bottom of the rectification tower is 135-136 ℃, the pressure is 0.16-0.18 MPa, the temperature of the top of the tower is 105-106 ℃, the temperature of the bottom of the recovery tower is 113-115, the temperature of the top of the tower is 95-97 ℃, the temperature of the bottom of the washing tower is 103-106 ℃, the temperature of the top of the tower is 93-95 ℃, the temperature of the bottom of the methanol tower is 105-107, the temperature of the top of the tower is 95-98, the temperature of the bottom of the alcohol evaporator is 108-110 ℃, the pressure is-0.058-0.06 MPa.
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| CN202010315835.1A CN111437619A (en) | 2020-04-21 | 2020-04-21 | Multi-tower differential pressure energy-saving anhydrous alcohol distillation system and anhydrous 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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| CN111821712A (en) * | 2020-07-27 | 2020-10-27 | 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 |
| WO2021213552A1 (en) * | 2020-04-21 | 2021-10-28 | 广东高科生物工程有限公司 | Multi-column differential pressure energy-saving anhydrous alcohol distillation system and anhydrous alcohol energy-saving production method |
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| 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 |
| CN115322862A (en) * | 2022-08-31 | 2022-11-11 | 宁波沪港食品机械制造有限公司 | Malt whisky distilling device and distilling process |
| CN116692775A (en) * | 2023-07-12 | 2023-09-05 | 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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| EP1608448A4 (en) * | 2003-03-28 | 2007-10-24 | Thermal Kinetics Systems Llc | Ethanol distillation with distillers soluble solids recovery 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 | Energy-saving system for five-tower three-stage differential-pressure distilling production of edible alcohol |
| 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 |
| 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 |
| CN111437619A (en) * | 2020-04-21 | 2020-07-24 | 广东高科生物工程有限公司 | Multi-tower differential pressure energy-saving anhydrous alcohol distillation system and anhydrous alcohol energy-saving production method |
| CN212818177U (en) * | 2020-04-21 | 2021-03-30 | 广东高科生物工程有限公司 | Multi-tower differential pressure energy-saving anhydrous alcohol distillation system |
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| WO2021213552A1 (en) * | 2020-04-21 | 2021-10-28 | 广东高科生物工程有限公司 | Multi-column differential pressure energy-saving anhydrous alcohol distillation system and anhydrous alcohol energy-saving production method |
| CN111821712A (en) * | 2020-07-27 | 2020-10-27 | 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 |
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