CN102992952A - Alcohol differential pressure distillation production equipment - Google Patents
Alcohol differential pressure distillation production equipment Download PDFInfo
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- CN102992952A CN102992952A CN2012104500341A CN201210450034A CN102992952A CN 102992952 A CN102992952 A CN 102992952A CN 2012104500341 A CN2012104500341 A CN 2012104500341A CN 201210450034 A CN201210450034 A CN 201210450034A CN 102992952 A CN102992952 A CN 102992952A
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Abstract
The invention provides alcohol differential pressure distillation production equipment comprising a undecanted wine column, an aldehyde column, a rectifying column, a condenser group, preheaters, a reboiler group and a flash evaporator, wherein the undecanted wine column adopts reduced pressure distillation, the aldehyde column adopts atmospheric distillation, and the rectifying column adopts differential pressure distillation mode by pressure distillation. High-temperature wine fume generated by the rectifying column is adopted for heating undecanted wine, the undecanted wine is boiled and evaporated at the temperature being 80-90 DEG C and the pressure being -0.03MPa to -0.08MPa, steam is produced by high-temperature waste liquor discharged from the bottom of the rectifying column and is taken as the heat energy for the preheating of crude alcohol and the undecanted wine, as well as the distillation of the aldehyde column. According to the alcohol differential pressure distillation production equipment, the energy consumption is reduced to be 1.5t steam/h in the alcohol distillation process, and the purposes of energy conservation and emission reduction are achieved.
Description
Technical field
The present invention relates to a kind of alcohol differential pressure distillation production unit, belong to the Alcohol Production field.
Background technology
The at present production of alcohol is take fermentation method as main, and the mash ethanol content that obtains by fermentation must carry out evaporation concentration to mash and just can obtain the high concentration ethanol product at 11～16 degree (volume fraction).The extracting and concentrating technology of alcohol is at present, and the distillation mash obtains thick wine, and then distills and remove aldehyde material, just can obtain alcohol in high concentration finally by crossing rectifying tower rectifying.The distillation of alcohol, rectifying are very high processes of energy consumption, energy consumption cost accounts for 50%～70% of Alcohol Production cost, the every raising one percentage point of the alcohol concn that mash contains, the cost of Alcohol Production can descend 10%, and the main direction of studying that therefore reduces at present the production cost of Ethanol is how to improve the ethanol concn of the rear mash of fermentation.The mash ethanol concn is higher, and the tolerance of yeast descends, and wants to improve the mash alcohol concn, must cultivate the yeast of resisting high-concentration ethanol.Ethanol concn improves, and can stimulate yeast, makes in its process of growth except producing alcohol, and the secretory volume of other organic substances has also increased, and this purity to the later separation purifying ethanol has increased difficulty.Therefore ethanol content may not reduce the production cost (particularly edible ethanol) of Ethanol in simply the raising mash.Except reducing the production cost of Ethanol from the method that increases the mash alcohol concn, can also be used for reducing energy consumption from the distillation of alcohol, the recovery of latent heat comprehensive utilization of rectifying, reduce production costs.
The appearance of alcohol differential pressure distillation technology reduces the energy consumption of alcohol distillation process greatly.Such as superfine edible ethanol six column distillation device and the techniques thereof of patent ZL200610035346.0(), adopt topping still, the 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 have power loss in the flow process of material from the tower to the tower, therefore energy consumption is still larger, increasing of technique, the consumption of power-equipment also can increase, and also beneficiating ingredient is separated through the alcohol behind six column distillations that (objectionable constituent are potato spirit in the alcohol, 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 descends, butylacetate, Isoamyl Acetate FCCs etc. are separated to be fallen), therefore simply the pursuit product purity and to abandon quality product be unadvisable, also be unscientific.Harmful composition is aldehyde material, methyl alcohol and potato spirit in the alcohol, and the alcohol that contains these materials is passed to such an extent that emperor's body is poisoned in edible meeting.The purpose of therefore producing edible ethanol is to get rid of objectionable constituent (formaldehyde, acetaldehyde, methyl alcohol, potato spirit), 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 is reduced, and quality product descends.
Summary of the invention
The objective of the invention is for present bio-ethanol distillation, rectifying energy consumption height, the problems such as the recovery of latent heat rate is low, a kind of alcohol differential pressure distillation method has been proposed, 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 and optimize the distillation parameter of each tower for each distillation tower, objectionable impurities potato spirit, aldehydes and methyl alcohol in the product alcohol are got rid of, and the reservation fragrance ingredient, the products obtained therefrom fragrant odour also can reach food grade.Can access the high quality edible ethanol by the present invention, and can improve the recovery utilization rate of still-process latent heat, 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 enters by the top of pipeline from preheater 4, preheater 4 bottoms link to each other with the opening for feed of wine with dregs tower 1 with pipeline, the top of wine with dregs tower 1 links to each other with the opening for feed of condenser 17 with pipeline, and the discharge port of condenser 17 links to each other with condenser 18 opening for feeds; The discharge port of condenser 18 links to each other with the top of thick wine storage tank 5; The top of thick wine storage tank 5 links to each other with vacuum pump with pipeline, the bottom links to each other with pump 14 with pipeline, pump 14 links to each other with the opening for feed of preheater 6 sides, the discharge port of preheater 6 links to each other with the opening for feed of aldehyde tower 2, the top of aldehyde tower 2 links to each other with the entrance of condenser 11 with pipeline, the outlet of condenser 11 links to each other with the entrance of condenser 12, and the outlet of condenser 12 links to each other with the entrance of condenser 13, and the import of condenser 11 and condenser 12 links to each other with the phegma import of pipeline with aldehyde tower 2 sides; Aldehyde tower 2 bottoms link to each other with the opening for feed of pump 15 with pipeline, the discharge port of pump 15 links to each other with the opening for feed of side, rectifying tower 3 top with pipeline, the top of rectifying tower 3 links to each other with the import of reboiler 8 with pipeline, the outlet of reboiler 8 links to each other with the import of reboiler 9, the outlet of reboiler 9 links to each other with the import of reboiler 10, and the import of reboiler 8, reboiler 9 and reboiler 10 all uses pipeline to be connected with the phegma import of rectifying tower 3 sides; The bottom of rectifying tower 3 links to each other with the opening for feed of pump 16 with pipeline, and the discharge port of pump 16 links to each other with the opening for feed of flasher 7; Wine with dregs tower 1 lower side links to each other with the phlegma import of reboiler 8 with pipeline, the condensate outlet of reboiler 8 links to each other with the phlegma import of reboiler 9, the condensate outlet of reboiler 9 links to each other with the phlegma import of reboiler 10, and the condensate outlet of reboiler 10 links to each other with the opening for feed of aldehyde tower 1 with pipeline; Flasher 7 tops link to each other with the steam-in of preheater 4, preheater 6 with pipeline.
Described mash evaporator tower, stage number are 20～30, and the column plate type is bubble plate, and the mash of heat adds from the 6th～15 block of column plate.
Described aldehyde distillation tower, stage number are 35～45, bubble plate 15 plates wherein, and counter direction jet trays is 20～35.
Described rectifying tower, stage number are 65～80, all are counter direction jet trays, down count at the 4th～8 layer from cat head and take out alcohol product.
Advantage of the present invention is:
1, mash is as the heat exchange material of rectifying tower vapor condensation, and namely playing the rectifying tower vapor condensation does not need water coolant, can heat again mash and make temperature reach the temperature of boiling, has saved the steam consumption that distills mash, reaches the purpose of energy-saving and emission-reduction.
2, use a flasher, the high temperature waste liquid that rectifying tower is discharged partly evaporates generation steam, the steam that produces is as the heat energy of mash, thick wine preheating and the heat energy of aldehyde column distillation and the heating of potato spirit tower, by the recovery of latent heat utilization, reduced the consumption of alcohol production process steam, reduced production costs.
3, the present invention adopts three-tower differential pressure distillation plant and technology, by stage number and the distil process of each tower of appropriate design, makes the equipment that less input can output quality meet the food grade alcohol of national standard, less energy consumption, and cost is low.
Description of drawings
Fig. 1 is the equipment drawing of alcohol differential pressure distillation production unit of the present invention.
Wherein: 1 is the wine with dregs tower, and 2 is the 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, be pump.
Embodiment
Below in conjunction with description of drawings the specific embodiment of the present invention:
The mash of fermenting-ripening enters preheater 4, adopt be steam heated to 60 ℃ as for flasher 7, the 9th layer from wine with dregs tower 1 joins the wine with dregs tower 1, opens vacuum pump, and the vacuum tightness in the wine with dregs tower 1 is reached-0.05MPa, mash passes through vacuum action from wine with dregs tower 1 bottom, automatically flow in the condenser 8,9,10 of 3 series connection that link to each other with rectifying tower, behind rectifying tower 3 cats head steam heat-exchanging out, flow back to the wine with dregs tower from the cooling water outlet of condenser 8,9,10 of series connection, owing to adopt steam and the mash heat exchange of rectifying tower, can make the mash temperature reach 85～90 ℃, under negative pressure, seethe with excitement, produce steam, therefore the wine with dregs tower does not need the steam heating of boiler house, has reduced energy consumption; The condenser 17 of steam through connecting from the generation of wine with dregs tower 1 cat head, obtain thick wine after 18 condensations, thick wine enters thick wine storage tank 5, thick wine is conveyed into the preheater 6 with pump 14 from the bottom of thick wine storage tank 5, be used for steam heating as for flasher, obtain the thick wine of heat, join in the aldehyde tower 2, adopt the steam that comes from flasher to distill as the heat energy that distills, the condenser 11 of the series connection that the steam process links to each other with aldehyde tower 2,12,13 condensations are condensed into liquid, and phlegma is back to multiple steaming the in the aldehyde tower 2 from condenser 11,12, difficult condensation or not condensation composition are lower boiling objectionable impurities, discharge from condenser 13; With the bottom of pump 15 from aldehyde tower 2 liquid in the aldehyde tower is input to the rectifying tower 3, rectifying tower 3 adopts the pressure distillation method, pressure is 1.0MPa, adopt 250 ℃ high-temperature steam 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 that links to each other with rectifying tower 3,10, adopt ripe mash as the heat-eliminating medium of the steam of rectifying tower 3 generations, condensation process does not need tap water to be used as water coolant, has therefore saved water resources; The phlegma that obtains is from condenser 8,9, and 10 steam-in is back to rectifying tower 3 and carries out multiple steaming, difficult condensation or not condensed material discharge from the top of condenser 10, from rectifying tower 3 cats head down several the 6th layer extract alcohol products; The waste liquid of getting rid of at the bottom of rectifying tower 3 towers passes into flasher 7, and the steam of discharging from flasher 7 top ducts is as the heat energy of aldehyde tower 1 distillation and as the heat energy of thick wine preheating, mash preheating.
The stage number of wine with dregs tower is 30 bubble plates;
The stage number of aldehyde tower is 40, and wherein 15 is bubble plate,, make 25 to be counter direction jet trays;
The stage number of rectifying tower is 78 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, the objectionable impurities aldehydes in the use ethanol and the content of methyl alcohol are very low, have reached the pure index of top grade, and partial detection has reached superfine pure requirement.Because the present invention adopts three column distillation technology, compares the distillation techniques such as four towers, five towers, six towers, because material has reduced power consumption and the facility investment that exchanges between tower and the tower, it is low that the present invention has energy consumption, less investment, low cost and other advantages.
Claims (4)
1. 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 enters by the top of pipeline from preheater (4), preheater (4) bottom links to each other with the opening for feed of wine with dregs tower (1) with pipeline, the top of wine with dregs tower (1) links to each other with the opening for feed of condenser (17) with pipeline, and the discharge port of condenser (17) links to each other with condenser (18) opening for feed; The discharge port of condenser (18) links to each other with the top of thick wine storage tank (5); The top of thick wine storage tank (5) links to each other with vacuum pump with pipeline, the bottom links to each other with pump (14) with pipeline, pump (14) links to each other with the opening for feed of preheater (6) side, the discharge port of preheater (6) links to each other with the opening for feed of aldehyde tower (2), the top of aldehyde tower (2) links to each other with the entrance of condenser (11) with pipeline, the outlet of condenser (11) links to each other with the entrance of condenser (12), the outlet of condenser (12) links to each other with the entrance of condenser (13), and the import of condenser (11) and condenser (12) links to each other with the phegma import of pipeline with aldehyde tower (2) side; Aldehyde tower (2) bottom links to each other with the opening for feed of pump (15) with pipeline, the discharge port of pump (15) links to each other with the opening for feed of pipeline with side, rectifying tower (3) top, the top of rectifying tower (3) links to each other with the import of reboiler (8) with pipeline, the outlet of reboiler (8) links to each other with the import of reboiler (9), the outlet of reboiler (9) links to each other with the import of reboiler (10), and the import of reboiler (8), reboiler (9) and reboiler (10) all uses pipeline to be connected with the phegma import of rectifying tower (3) side; The bottom of rectifying tower (3) links to each other with the opening for feed of pump (16) with pipeline, and the discharge port of pump (16) links to each other with the opening for feed of flasher (7); Wine with dregs tower (1) lower side links to each other with the phlegma import of reboiler (8) with pipeline, the condensate outlet of reboiler (8) links to each other with the phlegma import of reboiler (9), the condensate outlet of reboiler (9) links to each other with the phlegma import of reboiler (10), and the condensate outlet of reboiler (10) links to each other with the opening for feed of aldehyde tower (1) with pipeline; Flasher (7) top links to each other with the steam-in of preheater (4), preheater (6) with pipeline.
2. alcohol differential pressure distillation production unit according to claim 1, it is characterized in that: described mash evaporator tower, stage number are 20～30, and the column plate type is bubble plate, and the mash of heat adds from the 6th～15 block of column plate.
3. alcohol differential pressure distillation production unit according to claim 1, it is characterized in that: described aldehyde distillation tower, stage number are 35～45, bubble plate 15 plates wherein, counter direction jet trays is 20～35.
4. alcohol differential pressure distillation production unit according to claim 1, it is characterized in that: described rectifying tower, stage number are 65～80, all are counter direction jet trays, from cat head down number take out alcohol product at the 4th～8 layer.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201210450034.1A CN102992952B (en) | 2012-11-12 | 2012-11-12 | Alcohol differential pressure distillation production unit |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201210450034.1A CN102992952B (en) | 2012-11-12 | 2012-11-12 | Alcohol differential pressure distillation production unit |
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| CN102992952A true CN102992952A (en) | 2013-03-27 |
| CN102992952B CN102992952B (en) | 2015-08-05 |
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| CN201210450034.1A Expired - Fee Related CN102992952B (en) | 2012-11-12 | 2012-11-12 | Alcohol differential pressure distillation production unit |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106635706A (en) * | 2017-01-04 | 2017-05-10 | 广东中科天元绿色食品有限公司 | Differential-pressure distillation energy-saving production device for double-distillation retort Baijiu and production method of double distillation retort liquor |
| CN109908616A (en) * | 2019-04-24 | 2019-06-21 | 中国轻工业西安设计工程有限责任公司 | The energy-saving distillation system and its distillating method of carbon monoxide ethyl alcohol |
| CN110922303A (en) * | 2019-12-30 | 2020-03-27 | 肥城金塔酒精化工设备有限公司 | Negative pressure mash tower degassing and aldehyde-discharging 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 |
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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 |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106635706A (en) * | 2017-01-04 | 2017-05-10 | 广东中科天元绿色食品有限公司 | Differential-pressure distillation energy-saving production device for double-distillation retort Baijiu and production method of double distillation retort liquor |
| 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 |
| CN109908616A (en) * | 2019-04-24 | 2019-06-21 | 中国轻工业西安设计工程有限责任公司 | The energy-saving distillation system and its distillating method of carbon monoxide ethyl alcohol |
| CN110922303A (en) * | 2019-12-30 | 2020-03-27 | 肥城金塔酒精化工设备有限公司 | Negative pressure mash tower degassing and aldehyde-discharging acid-discharging device for fuel ethanol and edible alcohol |
| 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 |
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| CN102992952B (en) | 2015-08-05 |
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