CN101717802B - Energy-saving production method of bio-ethanol - Google Patents
Energy-saving production method of bio-ethanol Download PDFInfo
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- CN101717802B CN101717802B CN2009102449353A CN200910244935A CN101717802B CN 101717802 B CN101717802 B CN 101717802B CN 2009102449353 A CN2009102449353 A CN 2009102449353A CN 200910244935 A CN200910244935 A CN 200910244935A CN 101717802 B CN101717802 B CN 101717802B
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Abstract
The invention relates to an energy-saving production method of bio-ethanol, matured fermenting mash from a fermenting unit is blended with process waste water and enters a rough distillation tower, the rough wine collected from the tower top is sent to a refined tower 2 for feeding, and the materials collected from the side line of the rough tower pass through the pipeline and are sent to a feed inlet of a refined tower 1; the refine tower 1 kettle collection is discharged for waste water processing; industrial alcohol satisfying the national standard GB/T394.1-94 can be collected from the tower top; alcohol products satisfying custom grade edible alcohol product national standard GB 10343-2008 are collected from the side line on the upper part of the tower; the refined tower 2 kettle collection is discharged for waster water processing, fuse oil stream collected from the tower side line is sent to the fuse oil extractor for recovering fuse oil; the side line at the upper part of the refined tower 1 is collected and sent to a methanol removing tower for feeding; and qualified alcohol products meeting senior grade edible alcohol product national standard GB 10343-2008 are collected from the side line at the lower part of the methanol removing tower or the tower kettle collection. In the invention, steam is consumed by lower than 1.5 tons for producing 1 ton of custom grade edible alcohol product, and steam is consumed by lower than 2.0 tons for producing 1 ton of senior grade edible alcohol product, therefore, the invention has wide market requirements.
Description
Technical field
The present invention relates to a kind of energy-saving production method of bio-ethanol, can effectively reduce energy consumption in the bio-ethanol production process, improve the bio-ethanol competitiveness of product in market.
Background technology
Bio-ethanol is a raw material with corn, potato class, sugarcane etc., processes through fermenting, distilling.The bio-ethanol product mainly is used for beverages wine, the solvent of electronic component manufacturing, superior cosmetics and Chemical Manufacture raw material.At present, the most of production standard that adopts edible ethanol of the production of bio-ethanol product, product specification is mainly general level edible ethanol and high grade edible spirit, and the national standard of the existing edible ethanol quality product of China is GB10343-2008.In recent years, along with the development of biochemical industry industry, and the development of bio-ethanol product downstream application related industries, have higher requirement for the production technique and the energy consumption material consumption of alcohol product.
Summary of the invention
The energy-conservation new process for producing of bio-ethanol of the present invention's exploitation; Raw material is starchy materials such as corn, wheat, jowar, paddy rice, cassava and Ipomoea batatas; And saccharine materials such as sugarcane and molasses, production process mainly comprises liquefaction unit, fermentation unit, rectification cell and treatment unit for waste water.The present invention adopts utilization of energy multi-level multiple-effect and precise distillation technology, and the steam consumption of producing the bio-ethanol product is reduced, and the product operation expense descends.
Technical scheme of the present invention is following:
A kind of energy-saving production method of bio-ethanol, production process comprise liquefaction unit, fermentation unit, rectifying and dewatering unit, treatment unit for waste water; Mix back entering topping still from unitary fermenting-ripening wine with dregs of fermentation and spent process water, the thick wine of cat head extraction is sent into rectifying tower 2 chargings, sends into rectifying tower 1 opening for feed from the material of topping still side line extraction through pipeline; Rectifying tower 1 still is adopted and is expelled to wastewater treatment; The industrial spirit of GB GB/T 394.1-94 is satisfied in rectifying tower 1 cat head extraction; The alcohol product of general level edible ethanol product GB GB10343-2008 is satisfied in rectifying tower 1 tower top side line extraction; Rectifying tower 2 cats head top is adopted and is delivered to rectifying tower 1, and rectifying tower 2 stills are adopted and are expelled to wastewater treatment, and the fusel oil stream thigh of rectifying tower 2 tower side line extraction is delivered to the potato spirit extractor and reclaimed potato spirit; The eparating methanol tower charging is delivered in rectifying tower 1 tower top side line extraction; Eparating methanol tower bottom side line; Or the qualified alcohol product that satisfies high grade edible spirit product GB GB10343-2008 of tower still extraction; Eparating methanol tower cat head extraction industrial spirit product satisfies the alcohol product of GB GB/T394.1-94, and the side line extraction of methanol column bottom is qualified when satisfying the high grade edible spirit product operation, and methyl alcohol Tata still is adopted the charging of returning smart tower 2.
Described spent process water is part clear liquid, anaerobism water, aerobic water or the fresh water of treatment unit for waste water, and requiring the alcohol volumetric concentration in the control charging is 9%-14%.
In liquefaction unit, will enter into the flash tank cooling from the material of keeping jar, the flash steam that the high-temperature material cooling produces in the flash tank is used to heat spice water.
Whole operating process is following:
1. liquefaction unit
The liquefaction unit production process is referring to Fig. 1-liquefaction unit schema.For starchy material, at first raw material handling is taken off assortedly, pulverize through kibbler again.Powder after the pulverizing adds water in spices device processes powder slurry and delivers to powder slurry jar, and stream adds subsidiary material such as glycase in powder slurry jar simultaneously.The powder slurry is delivered to Jet liquefier with the powder stock pump in powder slurry jar, and Jet liquefier is through the amount control material Heating temperature of control water vapour, and injector outlet material temperature controls to 83 ℃～140 ℃; After powder slurry temperature is elevated to the temperature of setting; With liquefied fermented glutinous rice deliver to keep stop 5～90 minutes in the jar after, material enters into flash tank and falls jar, liquefied fermented glutinous rice is cooled to 80 ℃～100 ℃; Feed liquid after the cooling enters into liquefied pot, and stream adds glycase simultaneously; Flash steam is used to heat spice water.Feed liquid stopped in liquefied pot 15～240 minutes, through whisking appliance glycase and feed liquid was mixed, the operation of liquefying.
The liquefied fermented glutinous rice of accomplishing the liquefaction operation cools the temperature to 28～38 ℃ through the water cooler cooling.Flow subsidiary material such as Ensure Liquid salt, saccharifying enzyme and sulphuric acid soln simultaneously, deliver to fermentation unit.
2. fermentation unit
The zymamsis production process is referring to Fig. 2-fermentation unit schema.The fermentation operation mode is continuously, or semicontinuous, or intermittently, total system mainly is made up of a plurality of fermentor tanks, ripe wine with dregs storage tank and CO2 washing tower etc.
From the chilled liquefied fermented glutinous rice of liquefaction unit, the partial liquefaction wine with dregs is sent into the distiller's yeast jar that spreads cultivation, and all the other deliver to fermentor tank.Distiller's yeast after the activation is put into the distiller's yeast jar that spreads cultivation, add liquefied fermented glutinous rice simultaneously, in jar, feed an amount of sterile air continuously; Under temperature 28-38 ℃ the condition of spreading cultivation, cultivate; After yeast count reached requirement, continuously to the fermentor tank feed, and yeast spread cultivation jar and to continue to add a liquefied fermented glutinous rice.After 28～38 ℃ of fermentor tank controlled temperature, ripe raw spirit degree reach fermentation and require, through fermenting-ripening wine with dregs pump to rectifying and dewatering unit fermenting-ripening wine with dregs without interruption.The CO that alcoholic fermentation process is discharged
2Introduce CO
2Washing tower, CO
2Deliver to liquefaction unit after the washing water washing of washing tower and be used for spice.
Contained a considerable amount of fermentable sugars for saccharine material, like molasses and sugar cane juice etc., acidified take off live together reason after, can directly deliver to fermentation unit and carry out fermentative prodn alcohol.
3. rectification cell
Ethanol refinery dehydration production process is referring to Fig. 3-rectification cell schema.Ripe wine with dregs from fermentation unit passes through distillation operation at rectification cell, obtains the edible ethanol product.The ethanol refinery dewatering unit mainly is made up of topping still, smart tower 1, smart tower 2, eparating methanol tower etc.
The production operation flow process.Mix back entering topping still from unitary fermenting-ripening wine with dregs of fermentation and spent process water; Spent process water is part clear liquid or anaerobism water or the aerobic water or the fresh water of treatment unit for waste water; The alcohol volumetric concentration of controlling as requested in the charging is 9%-14%; Topping still working pressure (absolute pressure) is 0.01～0.2MPa, and mash removes water, organic acid and heavy component impurity etc. at this, and the thick wine of cat head extraction is sent into rectifying tower 2 chargings; Crude distillation column is adopted and is expelled to wastewater treatment, sends into rectifying tower 1 opening for feed from the material of topping still side line extraction through pipeline; Material carries out mass transfer operation in rectifying tower 1; Remove water, organic acid and heavy component impurity etc. at this; Rectifying tower 1 still is adopted and is expelled to wastewater treatment; Working pressure (absolute pressure) is 0.2～0.4MPa, and the industrial spirit of GB GB/T 394.1-94 is satisfied in rectifying tower 1 cat head extraction, and the alcohol product of general level edible ethanol product GB GB10343-2008 is satisfied in smart tower 1 tower top side line extraction; Thick wine from thick tower carries out mass transfer operation in rectifying tower 2 towers; Remove impurity such as water at this, concentrate recovered alcohol, working pressure (absolute pressure) is 0.4～0.8MPa; Rectifying tower 2 cats head top is adopted and is delivered to rectifying tower 1; All the other top vapour reflux after delivering to rectifying tower 1 reboiler condensation, and rectifying tower 2 stills are adopted and are expelled to wastewater treatment, and the fusel oil stream thigh of rectifying tower 2 tower side line extraction is delivered to the potato spirit extractor and reclaimed potato spirit; In order further to obtain the high grade edible spirit product; The eparating methanol tower charging is delivered in rectifying tower 1 tower top side line extraction; The cat head working pressure (absolute pressure) of eparating methanol tower is 0.01-0.4Mpa, and ethanol aqueous solution removes impurity such as methyl alcohol, eparating methanol tower bottom side line in eparating methanol tower; Or the qualified alcohol product that satisfies high grade edible spirit product GB GB10343-2008 of tower still extraction; Eparating methanol tower cat head extraction industrial spirit product satisfies the alcohol product of GB GB/T 394.1-94, and the side line extraction of methanol column bottom is qualified when satisfying the high grade edible spirit product operation, and methyl alcohol Tata still is adopted the charging of returning smart tower 2.
In the production process of bio-ethanol, because thick mash fermentation, and the instability of operation; Cause the ethanol concn of fermenting-ripening wine with dregs higher, change bigger, through in the charging of fermenting-ripening wine with dregs, sneaking into a certain amount of water; Keep the ethanol concn of fermenting-ripening wine with dregs charging stable; Make the ethanol refinery device realize stable operation, the water of sneaking into can be fresh water, or from qualified discharge water after clear liquid, anaerobism water, aerobic water and the processing of treatment unit for waste water
Topping still, rectifying tower 1, rectifying tower 2, eparating methanol tower are the combination tower of tray column or packing tower or tray column and packing tower, and higher separation efficiency is arranged.
4. treatment unit for waste water
The ethanol produce wastewater treatment process is referring to Fig. 4-treatment unit for waste water schema.Contain solid waste water and realize liquid-solid separation through equipment for separating liquid from solid from rectifying and dewatering is unitary, the wet poor drying machine of delivering to after the separation is wetly poorly done poor acts as a fuel or feed uses through drying machine is dried.Clear liquid after the separation is delivered to anaerobic device, and the biogas that anaerobic jar is discharged is sent into the boiler combustion utilization, and the anaerobic operation temperature is 30 ~ 40 ℃, or 50 ~ 65 ℃, through the discharge of wastewater up to standard of aerobic treatment.In order to keep the unitary stable operation of ethanol refinery, utilization process waste water reduces discharged waste water, with part clear liquid or anaerobism water or aerobic water, or handles the thick tower charging that back qualified discharge water returns rectification cell.
In traditional production process, produce 1 ton of general level edible ethanol product, consume steam more than 2.5 tons; Produce 1 ton of high grade edible spirit product, consume steam more than 3.0 tons.The present invention adopts utilization of energy multi-level multiple-effect and precise distillation technology, makes to produce 1 ton of general level edible ethanol product, consumes steam below 1.5 tons; Produce 1 ton of high grade edible spirit product, consume steam below 2.0 tons, the product operation expense descends, and production equipment has the market competitiveness of having more, and the market requirement is widely arranged.
Description of drawings
Fig. 1: liquefaction unit schema;
Fig. 2: fermentation unit schema;
Fig. 3: rectification cell schema;
Fig. 4: treatment unit for waste water schema.
Embodiment
Adopt the technical process like Fig. 1, Fig. 2, Fig. 3 and Fig. 4: scheme is following:
1. liquefaction unit
The liquefaction unit production process is referring to Fig. 1-liquefaction unit schema.For starchy material, at first raw material handling is taken off assortedly, pulverize through kibbler again.Powder after the pulverizing adds water in spices device processes powder slurry and delivers to powder slurry jar, and stream adds subsidiary material such as glycase in powder slurry jar simultaneously.The powder slurry is delivered to Jet liquefier with the powder stock pump in powder slurry jar, and Jet liquefier is through the amount control material Heating temperature of control water vapour, and injector outlet material temperature controls to 83 ℃～140 ℃; After powder slurry temperature is elevated to the temperature of setting; With liquefied fermented glutinous rice deliver to keep stop 5～90 minutes in the jar after, material enters into flash tank and falls jar, liquefied fermented glutinous rice is cooled to 80 ℃～100 ℃; Feed liquid after the cooling enters into liquefied pot, and stream adds glycase simultaneously; Flash steam is used to heat spice water.Feed liquid stopped in liquefied pot 15～240 minutes, through whisking appliance glycase and feed liquid was mixed, the operation of liquefying.
The liquefied fermented glutinous rice of accomplishing the liquefaction operation cools the temperature to 28～38 ℃ through the water cooler cooling.Flow subsidiary material such as Ensure Liquid salt, saccharifying enzyme and sulphuric acid soln simultaneously, deliver to fermentation unit.
2. fermentation unit
The zymamsis production process is referring to Fig. 2-fermentation unit schema.The fermentation operation mode is continuously, or semicontinuous, or intermittently, total system is mainly by a plurality of fermentor tanks, ripe wine with dregs storage tank and CO
2Compositions such as washing tower.
From the chilled liquefied fermented glutinous rice of liquefaction unit, wherein the liquefied fermented glutinous rice of 10-70% is partly sent into the distiller's yeast jar that spreads cultivation, and all the other deliver to fermentor tank.Distiller's yeast after the activation is put into the distiller's yeast jar that spreads cultivation, add liquefied fermented glutinous rice simultaneously, in jar, feed an amount of sterile air continuously; Under temperature 28-38 ℃ the condition of spreading cultivation, cultivate; After yeast count reached requirement, continuously to the fermentor tank feed, and yeast spread cultivation jar and to continue to add a liquefied fermented glutinous rice.After 28～38 ℃ of fermentor tank controlled temperature, ripe raw spirit degree reach fermentation and require, through fermenting-ripening wine with dregs pump to rectifying and dewatering unit fermenting-ripening wine with dregs without interruption.The CO that alcoholic fermentation process is discharged
2Introduce CO
2Washing tower, CO
2Deliver to liquefaction unit after the washing water washing of washing tower and be used for spice.
Contained a considerable amount of fermentable sugars for saccharine material, like molasses and sugar cane juice etc., acidified take off live together reason after, can directly deliver to fermentation unit and carry out fermentative prodn alcohol.
3. rectification cell
Ethanol refinery dehydration production process is referring to Fig. 3-rectification cell schema.Ripe wine with dregs from fermentation unit passes through distillation operation at rectification cell, obtains the edible ethanol product.The ethanol refinery dewatering unit mainly is made up of topping still, smart tower 1, smart tower 2, eparating methanol tower etc.
The production operation flow process.Mix back entering topping still from unitary fermenting-ripening wine with dregs of fermentation and spent process water; Spent process water is part clear liquid or anaerobism water or the aerobic water or the fresh water of treatment unit for waste water; The alcohol volumetric concentration of controlling as requested in the charging is 9%-14%; Topping still working pressure (absolute pressure) is 0.01～0.2MPa, and mash removes water, organic acid and heavy component impurity etc. at this, and the thick wine of cat head extraction is sent into rectifying tower 2 chargings; Crude distillation column is adopted and is expelled to wastewater treatment, sends into rectifying tower 1 opening for feed from the material of topping still side line extraction through pipeline; Material carries out mass transfer operation in rectifying tower 1; Remove water, organic acid and heavy component impurity etc. at this; Rectifying tower 1 still is adopted and is expelled to wastewater treatment; Working pressure (absolute pressure) is 0.2～0.4MPa, and the industrial spirit of GB GB/T 394.1-94 is satisfied in rectifying tower 1 cat head extraction, and the alcohol product of general level edible ethanol product GB GB10343-2008 is satisfied in smart tower 1 tower top side line extraction; Thick wine from thick tower carries out mass transfer operation in rectifying tower 2 towers; Remove impurity such as water at this, concentrate recovered alcohol, working pressure (absolute pressure) is 0.4～0.8MPa; Rectifying tower 2 cats head top is adopted and is delivered to rectifying tower 1; All the other top vapour reflux after delivering to rectifying tower 1 reboiler condensation, and rectifying tower 2 stills are adopted and are expelled to wastewater treatment, and the fusel oil stream thigh of rectifying tower 2 tower side line extraction is delivered to the potato spirit extractor and reclaimed potato spirit; In order further to obtain the high grade edible spirit product; The eparating methanol tower charging is delivered in rectifying tower 1 tower top side line extraction; The cat head working pressure (absolute pressure) of eparating methanol tower is 0.01-0.4Mpa, and ethanol aqueous solution removes impurity such as methyl alcohol, eparating methanol tower bottom side line in eparating methanol tower; Or the qualified alcohol product that satisfies high grade edible spirit product GB GB10343-2008 of tower still extraction; Eparating methanol tower cat head extraction industrial spirit product satisfies the alcohol product of GB GB/T 394.1-94, and the side line extraction of methanol column bottom is qualified when satisfying the high grade edible spirit product operation, and methyl alcohol Tata still is adopted the charging of returning smart tower 2.
In the production process of bio-ethanol, because thick mash fermentation, and the instability of operation; Cause the ethanol concn of fermenting-ripening wine with dregs higher, change bigger, through in the charging of fermenting-ripening wine with dregs, sneaking into a certain amount of water; Keep the ethanol concn of fermenting-ripening wine with dregs charging stable; Make the ethanol refinery device realize stable operation, the water of sneaking into can be fresh water, or from qualified discharge water after clear liquid, anaerobism water, aerobic water and the processing of treatment unit for waste water
Topping still, rectifying tower 1, rectifying tower 2, eparating methanol tower are the combination tower of tray column or packing tower or tray column and packing tower, and higher separation efficiency is arranged.
4. treatment unit for waste water
The ethanol produce wastewater treatment process is referring to Fig. 4-treatment unit for waste water schema.Contain solid waste water and realize liquid-solid separation through equipment for separating liquid from solid from rectifying and dewatering is unitary, the wet poor drying machine of delivering to after the separation is wetly poorly done poor acts as a fuel or feed uses through drying machine is dried.Clear liquid after the separation is delivered to anaerobic device, and the biogas that anaerobic jar is discharged is sent into the boiler combustion utilization, and the anaerobic operation temperature is 30 ~ 40 ℃, or 50 ~ 65 ℃, through the discharge of wastewater up to standard of aerobic treatment.In order to keep the unitary stable operation of ethanol refinery, utilization process waste water reduces discharged waste water, with part clear liquid or anaerobism water or aerobic water, or handles the thick tower charging that back qualified discharge water returns rectification cell.
Embodiment 1:
Adopting cassava is the alcohol product that raw material production satisfies general level edible ethanol product GB GB10343-2008, and production process mainly comprises liquefaction unit, fermentation unit, rectification cell, treatment unit for waste water.Concrete steps are following:
1. liquefaction unit
The liquefaction unit production process is referring to Fig. 1-liquefaction unit schema.At first cassava is done raw material handling and take off assortedly, pulverize again.Raw material after the pulverizing adds water in spices device processes powder slurry and delivers to powder slurry jar, and stream adds subsidiary material such as glycase simultaneously.The powder slurry is delivered to Jet liquefier with the powder stock pump in powder slurry jar; Jet liquefier is through the amount control material Heating temperature of control water vapour, and injector outlet material temperature controls to 115 ℃, delivers to keep to stop after 35 minutes in the jar; Material enters into the liquefied fermented glutinous rice flash tank and is cooled to 85 ℃; Feed liquid after the cooling enters into liquefied pot, and flash steam is used to heat spice water, and stream adds glycase simultaneously.Feed liquid stopped in liquefied pot 120 minutes, through whisking appliance glycase and feed liquid was mixed, the operation of liquefying.
The liquefied fermented glutinous rice cooling of accomplishing the liquefaction operation cools the temperature to 29 ℃.Flow subsidiary material such as Ensure Liquid salt, saccharifying enzyme and sulphuric acid soln simultaneously.
2. fermentation unit
The zymamsis production process is referring to Fig. 2-fermentation unit schema.The fermentation operation mode is that total system is mainly by 7 fermentor tanks and 1 CO continuously
2Compositions such as washing tower.
From the chilled liquefied fermented glutinous rice of liquefaction unit, wherein 40% liquefied fermented glutinous rice is sent into the distiller's yeast jar that spreads cultivation, and all the other deliver to fermentor tank.Distiller's yeast after the activation is put into the distiller's yeast jar that spreads cultivation; Add liquefied fermented glutinous rice simultaneously, in jar, feed continuously an amount of sterile air, under the condition of 29 ℃ of temperature that spreads cultivation, cultivate; After yeast count reaches requirement; Continuously to the fermentor tank feed, beer is successively continuously through 7 fermentor tanks, and yeast spreads cultivation and jar continues to add a liquefied fermented glutinous rice.30 ℃ of fermentor tank controlled temperature, last fermentation cylinder for fermentation wine with dregs through fermenting-ripening wine with dregs pump to rectifying and dewatering unit fermenting-ripening wine with dregs without interruption.The CO that alcoholic fermentation process is discharged
2Introduce CO
2Washing tower, CO
2Deliver to liquefaction unit after the washing water washing of washing tower and be used for spice.
3. rectification cell
The production operation flow process.Ethanol refinery dehydration production process is referring to Fig. 3-rectification cell schema.Ripe wine with dregs from fermentation unit passes through distillation operation at rectification cell, obtains general level edible ethanol product.The ethanol refinery dewatering unit mainly is made up of topping still, smart tower 1 and smart tower 2.
Part clear liquid from unitary fermenting-ripening wine with dregs of fermentation and treatment unit for waste water mixes back entering topping still; Control charging alcohol volumetric concentration is 10%, and topping still working pressure (absolute pressure) is 0.05MPa, and mash removes water, organic acid and heavy component impurity etc. at this; The thick wine of cat head extraction is sent into smart tower 2 chargings; Crude distillation column is adopted the discharge system to wastewater treatment, and top vapour is used for the topping still heating, sends into smart tower 1 opening for feed from the material of thick tower side line extraction through pipeline; Material carries out mass transfer operation in smart tower 1; Remove water, organic acid and heavy component impurity etc. at this; Smart tower 1 still is adopted and is expelled to wastewater treatment, and working pressure (absolute pressure) is 0.2MPa, cat head extraction industrial spirit product; The industrial spirit product of GB GB/T 394.1-94 is satisfied in smart tower 1 cat head extraction, and the alcohol product of general level edible ethanol product GB GB10343-2008 is satisfied in smart tower 1 tower top side line extraction; Thick wine from thick tower carries out mass transfer operation in smart tower 2 towers; Remove impurity such as water at this, concentrate recovered alcohol, working pressure (absolute pressure) is 0.5MPa; The cat head top is adopted and is delivered to smart tower 1; All the other top vapour reflux after delivering to smart tower 1 reboiler condensation, and smart tower 2 stills are adopted and are expelled to wastewater treatment, and the fusel oil stream thigh of tower side line extraction is delivered to the potato spirit extractor and reclaimed potato spirit.
Topping still is that tray column, smart tower 1 are the combination tower of tray column and packing tower for tray column, smart tower 2.
Adopt above production technique, the steam consumption of producing 1 ton of general level edible ethanol product is 1.4 tons.
4. treatment unit for waste water
The ethanol produce wastewater treatment process is referring to Fig. 4-treatment unit for waste water schema.Contain solid waste water and realize liquid-solid separation through equipment for separating liquid from solid from rectifying and dewatering is unitary, the wet poor drying machine of delivering to after the separation is wetly poorly done the poor use that acts as a fuel through drying machine is dried.Clear liquid after the separation is delivered to anaerobic device, and the biogas that anaerobic jar is discharged is sent into the boiler combustion utilization, and the anaerobic operation temperature is 30 ~ 40 ℃, through the discharge of wastewater up to standard of aerobic treatment.In order to keep the unitary stable operation of ethanol refinery, utilization process waste water reduces discharged waste water, the part clear liquid is returned the thick tower charging of rectification cell.
Embodiment 2:
Adopting corn is the alcohol product that raw material production satisfies high grade edible spirit product GB GB10343-2008, and production process mainly comprises liquefaction unit, fermentation unit, rectification cell, treatment unit for waste water.Concrete steps are following:
1. liquefaction unit
The liquefaction unit production process is referring to Fig. 1-liquefaction unit schema.At first maize raw material cleaning is taken off assortedly, pulverize again.Raw material after the pulverizing adds water in spices device processes powder slurry and delivers to powder slurry jar, and stream adds subsidiary material such as glycase simultaneously.The powder slurry is delivered to Jet liquefier with the powder stock pump in powder slurry jar; Jet liquefier is through the amount control material Heating temperature of control water vapour, and injector outlet material temperature controls to 140 ℃, delivers to keep to stop after 12 minutes in the jar; Material enters into the liquefied fermented glutinous rice flash tank and is cooled to 80 ℃; Feed liquid after the cooling enters into liquefied pot, and flash steam is used to heat spice water, and stream adds glycase simultaneously.Feed liquid stopped in liquefied pot 130 minutes, through whisking appliance glycase and feed liquid was mixed, the operation of liquefying.
The liquefied fermented glutinous rice cooling of accomplishing the liquefaction operation cools the temperature to 30 ℃.Flow subsidiary material such as Ensure Liquid salt, saccharifying enzyme and sulphuric acid soln simultaneously.
2. fermentation unit
The zymamsis production process is referring to Fig. 2-fermentation unit schema.The fermentation operation mode is that intermittently total system is mainly by 9 fermentor tanks and 1 CO
2Compositions such as washing tower.
From the chilled liquefied fermented glutinous rice of liquefaction unit, part is sent into the distiller's yeast jar that spreads cultivation, and part is delivered to fermentor tank.Distiller's yeast after the activation is put into the distiller's yeast jar that spreads cultivation; Add liquefied fermented glutinous rice simultaneously, in jar, feed continuously an amount of sterile air, under the condition of 30 ℃ of temperature that spreads cultivation, cultivate; After yeast count reaches requirement; To the fermentor tank feed, beer is sent into 9 fermentor tanks successively respectively continuously, and yeast spreads cultivation jar and to continue to add a liquefied fermented glutinous rice.38 ℃ of fermentor tank controlled temperature, after fermentation cylinder for fermentation raw spirit degree reaches requirement, through fermenting-ripening wine with dregs pump to rectifying and dewatering unit fermenting-ripening wine with dregs without interruption.The CO that alcoholic fermentation process is discharged
2Introduce CO
2Washing tower, CO
2Deliver to liquefaction unit after the washing water washing of washing tower and be used for spice.
3. rectification cell
Ethanol refinery dehydration production process is referring to Fig. 3-rectification cell schema.Ripe wine with dregs from fermentation unit passes through distillation operation at rectification cell, obtains the edible ethanol product.The ethanol refinery dewatering unit mainly is made up of topping still, smart tower 1, smart tower 2 and eparating methanol tower.
The production operation flow process.Part anaerobism water from unitary fermenting-ripening wine with dregs of fermentation and treatment unit for waste water mixes back entering topping still; Control charging alcohol volumetric concentration is 11%; Topping still working pressure (absolute pressure) is 0.1MPa, and mash removes water, organic acid and heavy component impurity etc. at this, and the thick wine of cat head extraction is sent into smart tower 2 chargings; Crude distillation column is adopted the discharge system to wastewater treatment, sends into smart tower 1 opening for feed from thick tower side line extraction material through pipeline; Material carries out mass transfer operation in smart tower 1; Remove water, organic acid and heavy component impurity etc. at this; Smart tower 1 still is adopted and is expelled to wastewater treatment, and working pressure (absolute pressure) is 0.3MPa, cat head extraction industrial spirit product; The industrial spirit product satisfies GB GB/T 394.1-94, and eparating methanol tower is delivered in smart tower 1 tower top side line extraction; Thick wine from thick tower carries out mass transfer operation in smart tower 2 towers; Remove impurity such as water at this, concentrate recovered alcohol, working pressure (absolute pressure) is 0.6MPa; The cat head top is adopted and is delivered to smart tower 1; All the other top vapour reflux after delivering to smart tower 1 reboiler condensation, and smart tower 2 stills are adopted and are expelled to wastewater treatment, and the fusel oil stream thigh of tower side line extraction is delivered to the potato spirit extractor and reclaimed potato spirit; The eparating methanol tower charging is delivered in smart tower 1 tower top side line extraction; The cat head working pressure (absolute pressure) of eparating methanol tower is 0.1Mpa; Ethanol aqueous solution from smart tower 1 removes impurity such as methyl alcohol in eparating methanol tower; The alcohol product that satisfies high grade edible spirit product GB GB10343-2008 that the side line extraction of eparating methanol tower bottom is qualified, cat head extraction industrial spirit product satisfies the alcohol product of GB GB/T394.1-94, and the tower still is adopted the charging of returning smart tower 2.
Topping still is tray column, smart tower 1 and smart tower 2 combination tower for tray column and packing tower.
Adopt above production technique, the steam consumption of producing 1 ton of high grade edible spirit product is 1.8 tons.
4. treatment unit for waste water
The ethanol produce wastewater treatment process is referring to Fig. 4-treatment unit for waste water schema.Contain solid waste water and realize liquid-solid separation from rectifying and dewatering is unitary, the wet poor drying machine of delivering to after the separation, wet poorly poorly uses as feed through dried the doing of drying machine through equipment for separating liquid from solid.Clear liquid after the separation is delivered to anaerobic device, and the biogas that anaerobic jar is discharged is sent into the boiler combustion utilization, and the anaerobic operation temperature is 50 ~ 65 ℃, through the discharge of wastewater up to standard of aerobic treatment.In order to keep the unitary stable operation of ethanol refinery, utilization process waste water reduces discharged waste water, part anaerobism water is returned the thick tower charging of rectification cell.
Claims (2)
1. energy-saving production method of bio-ethanol, production process comprises liquefaction unit, fermentation unit, rectifying and dewatering unit, treatment unit for waste water; It is characterized in that: ferment certainly unitary fermenting-ripening wine with dregs and spent process water mix the back and get into topping still, and the thick wine of cat head extraction is sent into rectifying tower 2 chargings, sends into rectifying tower 1 opening for feed from the material of topping still side line extraction through pipeline; Described spent process water is part clear liquid, anaerobism water, aerobic water or the fresh water of treatment unit for waste water, and requiring the alcohol volumetric concentration in the control charging is 9%-14%; Rectifying tower 1 still is adopted and is expelled to wastewater treatment; The industrial spirit of GB GB/T 394.1 one 94 is satisfied in rectifying tower 1 cat head extraction; The alcohol product of general level edible ethanol product GB GB10343-2008 is satisfied in rectifying tower 1 tower top side line extraction; Rectifying tower 2 cats head top is adopted and is delivered to rectifying tower 1, and rectifying tower 2 stills are adopted and are expelled to wastewater treatment, and the fusel oil stream thigh of rectifying tower 2 tower side line extraction is delivered to the potato spirit extractor and reclaimed potato spirit; The eparating methanol tower charging is delivered in rectifying tower 1 tower top side line extraction; Eparating methanol tower bottom side line; Or the qualified alcohol product that satisfies high grade edible spirit product GB GB10343-2008 of tower still extraction; Eparating methanol tower cat head extraction industrial spirit product satisfies the alcohol product of GB GB/T 394.1 one 94, and the side line extraction of methanol column bottom is qualified when satisfying the high grade edible spirit product operation, and methyl alcohol Tata still is adopted the charging of returning smart tower 2.
2. a kind of energy-saving production method of bio-ethanol as claimed in claim 1 is characterized in that: in liquefaction unit, will enter into the flash tank cooling from the material of keeping jar, the flash steam that the high-temperature material cooling produces in the flash tank is used to heat spice water.
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| CN105733905A (en) * | 2014-12-09 | 2016-07-06 | 商南县时代生物科技有限公司 | Method for preparing alcohol through slagless distillation |
| CN106422388B (en) * | 2016-10-26 | 2019-02-19 | 广东中科天元新能源科技有限公司 | The differential distillation energy saver and its production technology of double thick tower production top grade alcohol |
| CN107418979B (en) * | 2017-07-05 | 2020-08-28 | 天津大学 | Energy-saving clean production method of fuel ethanol |
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| WO2006086792A2 (en) * | 2005-02-07 | 2006-08-17 | Novozymes North America, Inc. | Fermentation product production processes |
| CN101045937A (en) * | 2006-03-30 | 2007-10-03 | 大连理工大学 | Clean fuel ethanol producing technology |
| CN101157890A (en) * | 2007-08-14 | 2008-04-09 | 天津大学 | Fuel ethanol production equipment and method |
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| WO2006086792A2 (en) * | 2005-02-07 | 2006-08-17 | Novozymes North America, Inc. | Fermentation product production processes |
| CN101045937A (en) * | 2006-03-30 | 2007-10-03 | 大连理工大学 | Clean fuel ethanol producing technology |
| CN101157890A (en) * | 2007-08-14 | 2008-04-09 | 天津大学 | Fuel ethanol production equipment and method |
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