CN102992952B - Alcohol differential pressure distillation production unit - Google Patents
Alcohol differential pressure distillation production unit Download PDFInfo
- Publication number
- CN102992952B CN102992952B CN201210450034.1A CN201210450034A CN102992952B CN 102992952 B CN102992952 B CN 102992952B CN 201210450034 A CN201210450034 A CN 201210450034A CN 102992952 B CN102992952 B CN 102992952B
- Authority
- CN
- China
- Prior art keywords
- tower
- wine
- reboiler
- condenser
- steam
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Distillation Of Fermentation Liquor, Processing Of Alcohols, Vinegar And Beer (AREA)
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The invention provides a kind of alcohol differential pressure distillation equipment.Comprise wine with dregs tower, aldehyde tower, rectifying tower, condenser group, preheater, reboiler group and flasher, wine with dregs tower adopts underpressure distillation, and aldehyde tower adopts air distillation, and rectifying tower adopts the differential distillation mode of pressure distillation.The high temperature fume adopting rectifying tower to produce heats mash, make mash at 80 ~ 90 DEG C, explosive evaporatoin under-0.03MPa ~-0.08Mpa pressure, and the high temperature waste liquid of discharging at the bottom of rectifying tower is produced steam, as the heat energy of thick wine, mash preheating and aldehyde column distillation, by the present invention can make alcohol distillation process energy consumption reduce 1.5t steam/hour, reach the object of energy-saving and emission-reduction.
Description
Technical field
The present invention relates to a kind of alcohol differential pressure distillation production unit, belong to Alcohol Production field.
Background technology
The production of current alcohol is based on fermentation method, and the mash ethanol content obtained by fermentation, 11 ~ 16 degree (volume fractions), must carry out evaporation concentration to mash and just can obtain high concentration ethanol product.The extracting and concentrating technology of current alcohol is, distillation mash, obtains thick wine, and then distillation removing aldehyde material, eventually passes rectifying tower rectifying and just can obtain alcohol in high concentration.The distillation of alcohol, rectifying are the processes that an energy consumption is very high, energy consumption cost accounts for 50% ~ 70% of Alcohol Production cost, the alcohol concn that mash contains often improves one percentage point, the cost of Alcohol Production can decline 10%, and the main direction of studying therefore reducing the production cost of Ethanol at present how to improve the ethanol concn of the rear mash of fermentation.Mash ethanol concn is higher, and the tolerance of yeast declines, and wants to improve mash alcohol concn, must cultivate the yeast of resisting high-concentration ethanol.Ethanol concn improves, and can stimulate yeast, and make in its process of growth except producing alcohol, the secretory volume of other organic substances too increases, and this adds difficulty to the purity of later separation purifying ethanol.Therefore in raising mash simply, ethanol content may not reduce the production cost (particularly edible ethanol) of Ethanol.Except reducing except the production cost of Ethanol from the method increasing mash alcohol concn, can also be used for reducing energy consumption from the recovery of latent heat comprehensive utilization of the distillation of alcohol, rectifying, reduce production cost.
The appearance of alcohol differential pressure distillation technology, reduces the energy consumption of alcohol distillation process greatly.Edible ethanol six column distillation device as superfine in patent ZL200610035346.0(and technique thereof), adopt topping still, vacuum dealdehyder tower, water wash column, rectifying tower, methanol column and recovery tower six-column differential-pressure distillation technique, obtain the alcohol of superfine food grade, energy consumption is 2.2 ~ 2.3t/t wine, but adopt six tower distillating methods, unavoidably power loss is had in the flow process of material from tower to tower, therefore energy consumption is still larger, increasing of technique, the consumption of power-equipment also can increase, and the alcohol after six column distillations also separates beneficiating ingredient, and (in alcohol, objectionable constituent are potato spirit, aldehydes and methyl alcohol, and ethyl acetate, butylacetates etc. are beneficiating ingredient), although products obtained therefrom purity is higher, (the flavour ingredient ethyl acetate but the fragrance of product declines, butylacetate, Isoamyl Acetate FCC etc. separated fall), therefore pursuit product simply purity and to abandon quality product be unadvisable, also be unscientific.Composition harmful in alcohol is aldehyde material, methyl alcohol and potato spirit, and the alcohol containing these materials is passed ediblely can poison emperor's body.The object of therefore producing edible ethanol objectionable constituent (formaldehyde, acetaldehyde, methyl alcohol, potato spirit) will be got rid of, and fragrance ingredient ethyl acetate, butylacetate, Isoamyl Acetate FCC etc. there is no need to get rid of, if in order to pursue purity, not only increase the energy consumption of still-process, product yield also can be made to reduce, and quality product declines.
Summary of the invention
The object of the invention is for the distillation of current bio-ethanol, energy consumption of rectification high, the problems such as recovery of latent heat rate is low, propose a kind of alcohol differential pressure distillation method, the present invention adopts the distillation technique of three-tower differential pressure, by appropriate design recovery of latent heat system, and select suitable stage number for each distillation tower and optimize the distillation parameter of each tower, objectionable impurities potato spirit, aldehydes and methyl alcohol in product alcohol are got rid of, and retaining fragrance ingredient, products obtained therefrom fragrant odour also can reach food grade.High quality edible ethanol can be obtained by the present invention, and the recovery utilization rate of still-process latent heat can be improved, reach the effect of energy-saving and emission-reduction.
The present invention is achieved in that a kind of alcohol differential pressure distillation production unit, comprise wine with dregs tower, aldehyde tower, rectifying tower, preheater, condenser group, flasher and reboiler group, it is characterized in that: ripe mash is entered by the top of pipeline from preheater 4, be connected with the opening for feed of wine with dregs tower 1 with pipeline bottom preheater 4, the top pipeline of wine with dregs tower 1 is connected with the opening for feed of condenser 17, and the discharge port of condenser 17 is connected with condenser 18 opening for feed; The discharge port of condenser 18 is connected with the top of thick wine storage tank 5; The top pipeline of thick wine storage tank 5 is connected with vacuum pump, bottom pipeline is connected with pump 14, pump 14 is connected with the opening for feed of preheater 6 side, the discharge port of preheater 6 is connected with the opening for feed of aldehyde tower 2, the top pipeline of aldehyde tower 2 is connected with the entrance of condenser 11, the outlet of condenser 11 is connected with the entrance of condenser 12, and the outlet of condenser 12 is connected with the entrance of condenser 13, and condenser 11 is connected with the phegma import of aldehyde tower 2 side with the import pipeline of condenser 12; Be connected with the opening for feed of pump 15 with pipeline bottom aldehyde tower 2, the discharge port pipeline of pump 15 is connected with the opening for feed of side above rectifying tower 3, the top pipeline of rectifying tower 3 is connected with the import of reboiler 8, the outlet of reboiler 8 is connected with the import of reboiler 9, the outlet of reboiler 9 is connected with the import of reboiler 10, and reboiler 8, reboiler 9 and the import of reboiler 10 all use pipeline to be connected with the phegma import of rectifying tower 3 side; The bottom pipeline of rectifying tower 3 is connected with the opening for feed of pump 16, and the discharge port of pump 16 is connected with the opening for feed of flasher 7; Wine with dregs tower 1 lower side pipeline is connected with the phlegma import of reboiler 8, the condensate outlet of reboiler 8 is connected with the phlegma import of reboiler 9, the condensate outlet of reboiler 9 is connected with the phlegma import of reboiler 10, and the condensate outlet pipeline of reboiler 10 is connected with the opening for feed of aldehyde tower 1; Flasher 7 top pipeline is connected with the steam-in of preheater 4, preheater 6.
Described mash evaporator tower, stage number is 20 ~ 30 pieces, and column plate type is bubble plate, and the mash of heat adds from 6th ~ 15 blocks of column plates.
Described aldehyde distillation tower, stage number is 35 ~ 45 pieces, wherein bubble plate 15 plate, and counter direction jet trays is 20 ~ 35 pieces.
Described rectifying tower, stage number is 65 ~ 80 pieces, is all counter direction jet trays, down counts take out alcohol products at 4th ~ 8 layers from tower top.
Advantage of the present invention is:
1, mash is as the heat exchange material of rectifying tower vapor condensation, and namely playing rectifying tower vapor condensation does not need water coolant, can heat again mash and make temperature reach the temperature of boiling, saves the steam consumption of distillation mash, reaches the object of energy-saving and emission-reduction.
2, a flasher is used, the high temperature waste liquid part evaporation that rectifying tower is discharged is produced steam, the heat energy of the steam produced as mash, thick wine preheating and the heat energy of aldehyde column distillation and the heating of potato spirit tower, utilized by recovery of latent heat, reduce the consumption of alcohol production process steam, reduce production cost.
3, the present invention adopts three-tower differential pressure distillation plant and technology, and by stage number and the distil process of each tower of appropriate design, make the equipment energy output quality that less input meet the food grade alcohol of national standard, less energy consumption, cost is low.
Accompanying drawing explanation
Fig. 1 is the equipment drawing of alcohol differential pressure distillation production unit of the present invention.
Wherein: 1 is wine with dregs tower, 2 is aldehyde tower, and 3 is rectifying tower, and 4,6 is preheater, and 5 is thick wine storage tank, and 7 is flasher, and 8,9,10 is reboiler, and 11,12,13,17,18 is condenser, 14,15,16, and be pump.
Embodiment
Below in conjunction with accompanying drawing, the specific embodiment of the present invention is described:
The mash of fermenting-ripening enters preheater 4, adopt and be steam heated to 60 DEG C as flasher 7, the 9th layer from wine with dregs tower 1 joins wine with dregs tower 1, open vacuum pump, the vacuum tightness in wine with dregs tower 1 is made to reach-0.05MPa, mash passes through vacuum action bottom wine with dregs tower 1, 3 condensers of connecting 8 that automatic inflow is connected with rectifying tower, 9, in 10, after rectifying tower 3 tower top steam heat-exchanging out, from the condenser 8 of series connection, 9, the cooling water outlet of 10 flows back to wine with dregs tower, owing to adopting steam and the mash heat exchange of rectifying tower, mash temperature can be made to reach 85 ~ 90 DEG C, seethe with excitement under negative pressure, produce steam, therefore wine with dregs tower does not need the steam heating of boiler house, decrease energy consumption, from the condenser 17 of steam through connecting that wine with dregs tower 1 tower top produces, thick wine is obtained after 18 condensations, thick wine enters thick wine storage tank 5, thick wine is conveyed into preheater 6 from the bottom pump 14 of thick wine storage tank 5, the steam heating be used for as flasher, obtain the thick wine of heat, join in aldehyde tower 2, the steam coming from flasher is adopted to distill as the heat energy distilled, steam passes through the condenser 11 of the series connection be connected with aldehyde tower 2, 12, 13 condensations are condensed into liquid, phlegma is from condenser 11, 12 are back to multiple in aldehyde tower 2 steaming, difficult condensation or not condensation composition are lower boiling objectionable impurities, discharge from condenser 13, from the bottom of aldehyde tower 2, the liquid in aldehyde tower is input to rectifying tower 3 with pump 15, rectifying tower 3 adopts pressure distillation method, pressure is 1.0MPa, adopt the high-temperature steam of 250 DEG C as the rectifying heat energy of rectifying tower 3, the steam that rectifying tower 3 produces enters the condenser 8,9 of the series connection be connected with rectifying tower 3,10, the heat-eliminating medium of the steam adopting ripe mash to produce as rectifying tower 3, condensation process does not need tap water to be used as water coolant, has therefore saved water resources, the phlegma obtained is from condenser 8, and the steam-in of 9,10 is back to rectifying tower 3 and carries out multiple steaming, and difficult condensation or not condensed material are discharged from the top of condenser 10, from rectifying tower 3 tower top down several 6th layer of extraction alcohol product, the waste liquid got rid of at the bottom of rectifying tower 3 tower passes into flasher 7, the heat energy that the steam of discharging from flasher 7 top duct distills as aldehyde tower 1 and the heat energy as thick wine preheating, mash preheating.
The stage number of wine with dregs tower is 30 pieces of bubble plates;
The stage number of aldehyde tower is 40 pieces, and wherein 15 pieces is bubble plate, make 25 pieces for counter direction jet trays;
The stage number of rectifying tower is 78 pieces of counter direction jet trays;
Table 1 is the detected result that method of the present invention obtains food grade alcohol
| Main test item | Technical requirements | Detected result |
| Ethanol/(%vol) | ≥95.0 | 95.4 |
| Oxidization time/min | ≥20 | 47 |
| Aldehyde (in acetaldehyde)/(mg/L) | ≤30 | 3 |
| Methyl alcohol/(mg/L) | ≤150 | 13 |
| N-propyl alcohol/(mg/L) | ≤100 | ＜1 |
| Isopropylcarbinol+primary isoamyl alcohol/(mg/L) | ≤30 | 4 |
It can be seen from the table, by three-tower differential pressure distillation technique of the present invention, use the content of the objectionable impurities aldehydes in ethanol and methyl alcohol very low, reach the index that top grade is pure, partial detection reaches superfine pure requirement.Because the present invention adopts three column distillation technology, compare the distillation techniques such as four towers, five towers, six towers, because material decreases the power consumption and facility investment exchanged between tower and tower, it is low that the present invention has energy consumption, less investment, low cost and other advantages.
Claims (3)
1. an alcohol differential pressure distillation production unit, comprise wine with dregs tower (1), aldehyde tower (2), rectifying tower (3) and flasher (7), it is characterized in that: ripe mash is entered by the top of pipeline from preheater (4), preheater (4) bottom pipeline is connected with the opening for feed of wine with dregs tower (1), the top pipeline of wine with dregs tower (1) is connected with the opening for feed of condenser (17), and the discharge port of condenser (17) is connected with condenser (18) opening for feed;
The discharge port of condenser (18) is connected with the top of thick wine storage tank (5), the top pipeline of thick wine storage tank (5) is connected with vacuum pump, bottom pipeline is connected with pump (14), pump (14) is connected with the opening for feed of preheater (6) side, the discharge port of preheater (6) is connected with the opening for feed of aldehyde tower (2), the top pipeline of aldehyde tower (2) is connected with the entrance of condenser (11), the outlet of condenser (11) is connected with the entrance of condenser (12), the outlet of condenser (12) is connected with the entrance of condenser (13), condenser (11) is connected with the phegma import of aldehyde tower (2) side with the import pipeline of condenser (12),
Aldehyde tower (2) bottom pipeline is connected with the opening for feed of pump (15), the discharge port pipeline of pump (15) is connected with the opening for feed of side, rectifying tower (3) top, the top pipeline of rectifying tower (3) is connected with the import of reboiler (8), the outlet of reboiler (8) is connected with the import of reboiler (9), the outlet of reboiler (9) is connected with the import of reboiler (10), reboiler (8), reboiler (9) and the import of reboiler (10) all use pipeline to be connected with the phegma import of rectifying tower (3) side, the bottom pipeline of rectifying tower (3) is connected with the opening for feed of pump (16), and the discharge port of pump (16) is connected with the opening for feed of flasher (7), wine with dregs tower (1) lower side pipeline is connected with the phlegma import of reboiler (8), the condensate outlet of reboiler (8) is connected with the phlegma import of reboiler (9), the condensate outlet of reboiler (9) is connected with the phlegma import of reboiler (10), and the condensate outlet pipeline of reboiler (10) is connected with the opening for feed of wine with dregs tower (1), flasher (7) top pipeline is connected with the steam-in of preheater (4), preheater (6),
Flow process after described device start is:
The mash of fermenting-ripening enters preheater (4), what employing came from flasher (7) is steam heated to 60 DEG C, the 9th layer from wine with dregs tower (1) joins wine with dregs tower (1), open vacuum pump, the vacuum tightness in wine with dregs tower (1) is made to reach-0.05MPa, mash passes through vacuum action from wine with dregs tower (1) bottom, 3 reboilers of connecting (8) that automatic inflow is connected with rectifying tower, (9), (10) in, after rectifying tower (3) tower top steam heat-exchanging out, from the reboiler (8) of series connection, (9), (10) cooling water outlet flows back to wine with dregs tower, adopt steam and the mash heat exchange of rectifying tower, mash temperature can be made to reach 85 ~ 90 DEG C, seethe with excitement under negative pressure, produce steam, therefore wine with dregs tower does not need the steam heating of boiler house, decrease energy consumption,
From the condenser (17) of steam through connecting that wine with dregs tower (1) tower top produces, (18) thick wine is obtained after condensation, thick wine enters thick wine storage tank (5), thick wine is conveyed into preheater (6) from the bottom pump (14) of thick wine storage tank (5), by the steam heating coming from flasher, obtain the thick wine of heat, join in aldehyde tower (2), the steam coming from flasher is adopted to distill as the heat energy distilled, steam passes through the condenser (11) of the series connection be connected with aldehyde tower (2), (12), (13) condensation is condensed into liquid, phlegma is from condenser (11), (12) multiple in aldehyde tower (2) steaming is back to, difficult condensation or not condensation composition are lower boiling objectionable impurities, discharge from condenser (13),
Pump (15) is input to the liquid in aldehyde tower rectifying tower (3) from the bottom of aldehyde tower (2), rectifying tower (3) adopts pressure distillation method, pressure is 1.0MPa, adopt the high-temperature steam of 250 DEG C as the rectifying heat energy of rectifying tower (3), the steam that rectifying tower (3) produces enters reboiler (8), (9), (10) of the series connection be connected with rectifying tower (3), the heat-eliminating medium of the steam adopting ripe mash to produce as rectifying tower (3), condensation process does not need tap water to be used as water coolant, has saved water resources; The phlegma obtained is back to rectifying tower (3) from the steam-in of reboiler (8), (9), (10) and carries out multiple steaming, difficult condensation or not condensed material are discharged from the top of condenser (10), from rectifying tower (3) tower top down several 6th layer of extraction alcohol product; The waste liquid of discharging at the bottom of rectifying tower (3) tower passes into flasher (7), the heat energy that the steam of discharging from flasher (7) top duct distills as aldehyde tower (1) and the heat energy as thick wine preheating, mash preheating;
Described mash evaporator tower, stage number is 20-30 block, and column plate type is bubble plate, and the mash of heat adds from 6-15 block column plate.
2. the alcohol differential pressure distillation production unit according to claim l, is characterized in that: described aldehyde distillation tower, and stage number is 35-45 block, wherein bubble plate 15 plate, and counter direction jet trays is 20-35 block.
3. the alcohol differential pressure distillation production unit according to claim l, is characterized in that: described rectifying tower, and stage number is 65-80 pieces, is all counter direction jet trays, and from tower top post, number takes out alcohol product at 4-8 layer.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210450034.1A CN102992952B (en) | 2012-11-12 | 2012-11-12 | Alcohol differential pressure distillation production unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201210450034.1A CN102992952B (en) | 2012-11-12 | 2012-11-12 | Alcohol differential pressure distillation production unit |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN102992952A CN102992952A (en) | 2013-03-27 |
| CN102992952B true CN102992952B (en) | 2015-08-05 |
Family
ID=47922137
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201210450034.1A Expired - Fee Related CN102992952B (en) | 2012-11-12 | 2012-11-12 | Alcohol differential pressure distillation production unit |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN102992952B (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106635706B (en) * | 2017-01-04 | 2020-10-23 | 广东省九江酒厂有限公司 | Differential pressure distillation energy-saving production device and method for white spirit with double distillation retorts |
| CN109908616B (en) * | 2019-04-24 | 2024-06-25 | 中国轻工业西安设计工程有限责任公司 | Energy-saving distillation system for preparing ethanol from carbon monoxide and distillation method thereof |
| CN110922303B (en) * | 2019-12-30 | 2024-04-19 | 肥城金塔酒精化工设备有限公司 | Negative pressure mash tower degassing, aldehyde and acid discharging device for fuel ethanol and edible alcohol |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101085717A (en) * | 2007-06-01 | 2007-12-12 | 蓝仁水 | Method for rectifying ethanol by three-tower heat integration device |
| CN102126920A (en) * | 2010-01-13 | 2011-07-20 | 中国石油化工集团公司 | Method for preparing azeotropic ethanol through three-tower triple-effect differential pressure heat integration |
-
2012
- 2012-11-12 CN CN201210450034.1A patent/CN102992952B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101085717A (en) * | 2007-06-01 | 2007-12-12 | 蓝仁水 | Method for rectifying ethanol by three-tower heat integration device |
| CN102126920A (en) * | 2010-01-13 | 2011-07-20 | 中国石油化工集团公司 | Method for preparing azeotropic ethanol through three-tower triple-effect differential pressure heat integration |
Also Published As
| Publication number | Publication date |
|---|---|
| CN102992952A (en) | 2013-03-27 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN106334327B (en) | A kind of alcohol distillation production method | |
| CN103305391B (en) | Method for improving quality grade of white spirit | |
| CN204702730U (en) | A kind of Novel steam distillation unit for liquor production by liquid fermentation | |
| CN102992952B (en) | Alcohol differential pressure distillation production unit | |
| CN109294893A (en) | A kind of resource utilization system and method for brewed spirit by-product yellow water | |
| CN112403005A (en) | Novel acid discharge equipment for white spirit production and processing and use method thereof | |
| CN103695475B (en) | Method for in-situ separation of ethanol by membrane separation technology | |
| CN102942445A (en) | Alcohol differential distillation production method | |
| CN203256177U (en) | Alcohol preparation device | |
| CN103409303B (en) | A kind of base wine of the aromatic Chinese spirit through membrane distillation upgrading and membrane distillation method thereof | |
| CN101381279B (en) | Fuel ethanol dehydration apparatus and method | |
| CN104232454B (en) | The method producing whiskey with waste yeast in beer production | |
| CN201668968U (en) | Energy-saving system for five-tower three-stage differential-pressure distilling production of edible alcohol | |
| CN205874359U (en) | Brandy distiller | |
| CN205576087U (en) | Cooling device in wine processing | |
| CN108795677A (en) | The former wine purification process and device of solid state fermentation | |
| CN110016425A (en) | A kind of energy-saving brewing device | |
| CN208814987U (en) | The former wine purification device of solid state fermentation | |
| CN201817458U (en) | Device for instantly distilling citronella oil by utilizing low temperature thin films | |
| CN207877702U (en) | A kind of energy-saving brewing device | |
| CN101935590B (en) | Low-temperature thin film citronella oil instantaneous distilling device | |
| CN203602599U (en) | Equipment for processing molasses alcohol liquid waste | |
| CN202173793U (en) | Alcohol prefractionator reboiling system using centrifugal clear liquid as cyclic medium | |
| CN201710997U (en) | Energy-saving plant active ingredient extracting and concentrating device | |
| CN103184133A (en) | Method and special system for forced reflux of brandy/fruit wine for distillation |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C14 | Grant of patent or utility model | ||
| GR01 | Patent grant | ||
| CF01 | Termination of patent right due to non-payment of annual fee | ||
| CF01 | Termination of patent right due to non-payment of annual fee |
Granted publication date: 20150805 Termination date: 20211112 |