CN1086849A - The distillating method of high grade edible spirit - Google Patents
The distillating method of high grade edible spirit Download PDFInfo
- Publication number
- CN1086849A CN1086849A CN 93112138 CN93112138A CN1086849A CN 1086849 A CN1086849 A CN 1086849A CN 93112138 CN93112138 CN 93112138 CN 93112138 A CN93112138 A CN 93112138A CN 1086849 A CN1086849 A CN 1086849A
- Authority
- CN
- China
- Prior art keywords
- tower
- wine
- oil
- dregs
- rectifying
- 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.)
- Pending
Links
Images
Landscapes
- Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)
Abstract
The distillating method of a kind of starchy material fermentative Production high grade edible spirit (GB10343-89) is provided.It is the wine with dregs tower by the band overhead condenser, the three-column process flow that rectifying tower that the stripping section rectifying section is installed separately and methanol column are formed, do not need thin up can reproduce the technological operation that the dilution tower thoroughly separates potato spirit at the wine with dregs tower, rectifying tower has the distinctive gas phase of the present invention to get oil again and conventional liquid phase is got oil, can thoroughly separate potato spirit; Rectifying tower can thoroughly separate head impurties such as acetaldehyde, methyl alcohol, low boiling ester class with methanol column; Therefore, this flow process can be produced high grade edible spirit, and yield is more than 92%.
Description
The invention provides the distillating method of a kind of starchy material fermentative Production high grade edible spirit (GB10343-89).
The quality of the alcohol of starchy material fermentative Production depends primarily on distillation.Tail level impurity during distillation in the crude alcohol is separate easily relatively, discharges with useless wine with dregs, waste liquid at the bottom of wine with dregs tower, rectifying Tata.The emphasis of alcohol distillation is to separate head impurty and fusel wet goods middle rank impurity such as acetaldehyde, methyl alcohol, low boiling ester class.Rectifying tower can separate head impurty and intermediate impurity with the aldehyde tower, but all can not be thorough; Methanol column can thoroughly separate head impurty, but can not separate intermediate impurity.At present domesticly generally adopt, only limit to the various multi-tower distillations that are combined to form of wine with dregs tower, aldehyde tower, rectifying tower and methanol column, can thoroughly separate head impurty, but all can not thoroughly separate fusel wet goods middle rank impurity, also just can not produce high grade edible spirit; Even undertake to do what is apparently beyond one's ability, yield is also very low.The thorough potato spirit that separates is the key of producing preferred edible ethanol, abroad is the multi-effect distilling that adopts thin up, and promptly (EXTRACTVE DISTILLA-TION TOWER also translates the title purification column, carries and heat up in a steamer tower, extraction tower and extraction distillation tower etc. at the dilution tower; It is actually incomplete stripping section, its tower bottom distillate ethanol concn is not approximately " zero ") in will be distilled to 80～92%(v) alcohol thin up and make cat head alcohol steam concentration reduce to 30～50%(v), all the overwhelming majority refluxes after the condensation, only tells a small amount of phlegma and does foreshot's proposition; Liquid fraction is 10～20%(v) alcohol at the bottom of the tower, delivers to rectifying tower and is distilled to 96%(v again).When ethanol concn is hanged down, be that the volatility coefficient K value of potato spirit of representative is very big with the primary isoamyl alcohol, potato spirit is inevitable highly to be collected in the cat head alcohol steam, and the potato spirit content in the liquid fraction is atomic at the bottom of the tower, thereby can thoroughly separate potato spirit.The multi-effect distilling of thin up can thoroughly separate potato spirit and produce high grade edible spirit (even better), but it needs 6 towers at least, and distillation plant and relevant civil engineering costs are quite huge; To be distilled to 96%(v behind 80～92%(v) the alcohol thin ups more again), certainly will increase energy consumption; How tower has pressurization and negative-pressure operation again, and balance is difficult to grasp operation inconvenience.Applicant proves that in theory thin up just repeats distillation, real non-extractive distillation, and it just makes the operation that separates potato spirit tend towards stability and easily goes, and is not indispensable to thorough separation potato spirit.
For addressing the above problem, the purpose of this invention is to provide a kind of dilution tower of not establishing does not need thin up can thoroughly separate potato spirit yet, and, expense less with tower economized, and energy consumption is not high, and is easy to operate, the distillating method of the high grade edible spirit that yield is higher.
For achieving the above object, the invention provides a kind of by wine with dregs tower with an overhead condenser, the three column distillation flow processs that the rectifying tower that the stripping section rectifying section is installed separately and methanol column are formed.Characteristics and function to three towers are explained as follows.
With the wine with dregs tower of an overhead condenser, can not only separate tail level impurity, can also separate potato spirit and part head impurty quite up hill and dale.When the ripe wine with dregs that gives heat enters wine with dregs cat head layer column plate and promptly seethed with excitement by the rising steam heating, crude alcohol steam imports overhead condenser, and all the overwhelming majority refluxes after the condensations, only takes out a small amount of phlegma, makes for the first time vapour phase and gets oil; The discharging of wine with dregs tower is to extract low-concentration ethanol solution out from wine with dregs tower middle and lower part side line, delivers to the rectifying tower stripping section.The volatility coefficient K value of potato spirit that when ethanol concn is low with the primary isoamyl alcohol is representative is very big, potato spirit is inevitable highly to be collected in the wine with dregs column overhead crude alcohol steam, head impurty also is collected at wherein in a large number, and potato spirit content is atomic from the low-concentration ethanol that wine with dregs tower middle and lower part side line is extracted out.Vapour phase is got oil and is got the different of oil in the conventional vapour phase of rectifying tower for the first time, be that not only it takes out from wine with dregs column overhead condenser, the more important thing is that extracting the atomic low-concentration ethanol of potato spirit content out from wine with dregs tower middle and lower part side line delivers to rectifying tower continuation rectifying, and conventional vapour phase to get oil be the alcohol steam identical substantially with the potato spirit content of the potato spirit alcohol that takes out (without washing) to be delivered to rectifying section continue rectifying, this can not thoroughly separate potato spirit.Therefore, vapour phase was got oil and substantially was different from conventional vapour phase and gets oil first time of the present invention, but had very reproduced the technological operation that the dilution tower separates potato spirit on the wine with dregs tower approx, and it can separate potato spirit quite up hill and dale, also can partly separate head impurty.For guaranteeing separating effect, wine with dregs tower stage number is more slightly than conventional wine with dregs tower.The wine with dregs tower both can place on the base, made the wine with dregs tower go out bed of material column plate and was higher than the stripping section top, and the reliable potential difference of discharging flows into stripping section top layer column plate automatically; Also can place same horizontal plane, stripping section top layer column plate be delivered in discharging with pump with stripping section.
Rectifying tower is the conventional rectification tower, and stripping section and rectifying section both were installed separately can place same horizontal plane, with reflux pump the rectifying section phegma is returned stripping section top layer column plate; Also rectifying section can be placed on the base, base should be higher than stripping section, guarantees that the rectifying section phegma is back to the stripping section top automatically by potential difference.The purpose that is installed separately is that the airway between two sections is told on a small quantity from the alcohol steam of stripping section, all makes for the second time vapour phase after the condensations and gets oil.The charging of rectifying section is a low-concentration ethanol, and potato spirit still can be collected in the alcohol steam of stripping section section top in a large number, and head impurty also gathers wherein, and for the second time vapour phase is got oil and can be separated potato spirit and head impurty effectively.Get the change that oil level is put, it is effective to make it get the more stable easy row of oil than conventional vapour phase.This vapour phase is got the method and apparatus of oil, can also be widely used in gas phase and cross on the wine with dregs tower and the airway between rectifying tower or the aldehyde tower of tower.For guaranteeing separating effect, rectifying section need have more column plate: more than the work in-process extract phase abundant column plate will be arranged, make head impurty be collected at cat head more; Below also abundant column plate to be arranged, block intermediate impurity effectively.Rectifying tower can separate head impurty and intermediate impurity effectively.
Methanol column can thoroughly separate head impurty; Both available normal pressure methanol column with the rectifying Tata at the bottom of the heating of thermal effluent and live steam, also available negative pressure methanol column with rectifying tower cat head alcohol steam and tower at the bottom of the thermal effluent heating.
In sum, three-column process flow of the present invention has twice vapour phase to get oil, a liquid phase is got oil, can thoroughly separate fusel wet goods middle rank impurity, puies forward 1% of low on fuel finished product alcohol amount at every turn; Twice vapour phase got oil removable part head impurty again simultaneously, makes the equal less than 3% of twice foreshot's extraction yield thereafter, but is enough to thoroughly separate head impurty.Therefore, it can produce high grade edible spirit (GB10343-89), and yield is more than 92%.The mounting means of wine with dregs tower rectifying tower and the working pressure of methanol column all respectively have two kinds of different selections, and three-column process flow provided by the invention has 8 kinds of different array configurations can be for practical.
Below in conjunction with accompanying drawing, be that the stripping section and the rectifying section of wine with dregs tower, rectifying tower all places different level to meet China actual, and adopt the three-column process flow of normal pressure methanol column, further set forth embodiment of the present invention.
Accompanying drawing is the synoptic diagram of above-mentioned three-column process flow.
1, wine with dregs tower 2, wine with dregs column overhead condenser 3, rectifying tower stripping section 4, airway 5, valve 6, carry oil pipe 7, condenser 8, rectifying tower rectifying section 9, mash and give hot device 10,12, partial condenser 11, methanol column 13, pump 14,15, reboiler
Ripe wine with dregs gives through mash and enters wine with dregs tower (1) top layer column plate after hot device (9) gives heat and promptly seethed with excitement by the rising steam heating, and fusel wet goods middle rank impurity height is collected in the cat head crude alcohol steam, and also enrichment is wherein for head impurty; The overwhelming majority refluxes after the whole condensations of crude alcohol steam importing overhead condenser (2) quilt, takes out a small amount of phlegma work vapour phase first time and gets oil, can quite thoroughly separate potato spirit and partly separate head impurty; Extract the atomic low-concentration ethanol solution of potato spirit content out from wine with dregs tower middle and lower part side line, flow to stripping section (3) top by potential difference and advance tower; Non-volatile impurity and tail level impurity are discharged with useless wine with dregs at the bottom of the wine with dregs Tata, and the wine with dregs tower heats with open steam.Low-concentration ethanol enters stripping section section top and is promptly seethed with excitement by the rising steam heating, and residual potato spirit still can be collected in the alcohol steam in a large number, and also enrichment is wherein for head impurty; Alcohol steam imports rectifying section (8) bottom along steam guiding tube (4), and the rectifying section phegma is back to stripping section automatically by potential difference, and rectifying tower heats with open steam; Tell a small amount of alcohol steam from steam guiding tube (4) and enter condenser (7) and all make for the second time vapour phase after the condensations and get oil along carrying oil pipe (6), can separate potato spirit and head impurty effectively, valve (5) may command is put forward oil mass; Get the foreshot from rectifying section top partial condenser (10) and separate head impurty, liquid phase is got oil in the rectifying section bottom, and tail level impurity is beaten to the discharge of reboiler (14) heating methanol tower (11) back with pump (13) with waste liquid at the bottom of stripping section; Get 96%(v from rectifying section top) more than work in-process alcohol send methanol column middle part to advance tower.Get the foreshot from methanol column dephlegmator of top of the tower (12) and thoroughly separate head impurty, at the bottom of tower, take out high grade edible spirit (GB10343-89); Feed reboiler (15) with live steam in addition, the heat supply deficiency of thermal effluent at the bottom of the additional rectifying Tata.
Implement distillating method of the present invention and can produce high grade edible spirit (GB10343-89), and following benefit is arranged: the product yield is more than 92%; Tower is few, saving equipment and relevant construction investment; Mostly be atmospheric operation and grasp easily, energy consumption is lower when using the negative pressure methanol column; Use normal pressure methanol column distillation energy consumption slightly high, but the equipment simple operations is convenient, the latent heat of wine with dregs tower rectifying tower overhead vapours can be used for other link of Alcohol Production again, and the Alcohol Production total energy consumption can not significantly improve; Wine with dregs tower discharging ethanol concn is lower than conventional wine with dregs tower, and useless wine with dregs solid load is also corresponding slightly high, is convenient to the comprehensive utilization of useless wine with dregs.
Claims (3)
1, the distillating method of a kind of starchy material fermentative Production high grade edible spirit (GB10343-89), much more slightly feature of the present invention is by the column plate wine with dregs tower (1) with an overhead condenser (2), the three column distillation flow processs that rectifying tower that the more rectifying section (8) of stripping section (3) and column plate is installed separately and methanol column (11) are formed.It has the distinctive vapour phase of twice the present invention and gets oil, and once conventional liquid phase is got the impurities removal ability quite completely that oil and twice routine are got the foreshot.
2, the distillating method of high grade edible spirit as claimed in claim 1 is characterized in that wine with dregs tower (1) cat head establishes a condenser (2).The overwhelming majority refluxes after the ripe wine with dregs that gives heat enters wine with dregs cat head layer column plate and promptly seethed with excitement by the rising steam heating, and crude alcohol steam imports the whole condensations of overhead condenser, takes out a small amount of phlegma and makes for the first time vapour phase and get oil; The discharging of wine with dregs tower is to extract the atomic low-concentration ethanol of potato spirit content out from tower middle and lower part side line, delivers to stripping section (3) and continues rectifying; Useless wine with dregs is discharged at the bottom of tower.For the first time vapour phase is got oil and can be separated potato spirit quite up hill and dale, and part is separated head impurties such as acetaldehyde, methyl alcohol, low boiling ester class simultaneously.
3, as the distillating method of claim 1,2 described high grade edible spirits, it is characterized in that steam guiding tube (4) between stripping section (3) and rectifying section (8) be linked in sequence valve (5), carry oil pipe (6) and condenser (7), constitute vapour phase and get oily device.When low-concentration ethanol enters the risen steam heating boiling of stripping section top layer column plate, alcohol steam imports the rectifying section bottom along steam guiding tube; Tell a small amount of alcohol steam from airway and enter condenser (7) along carrying oil pipe (6), all make for the second time vapour phase after the condensations and get oil, valve (5) may command is put forward oil mass, and vapour phase is got oil and can be stablized and separate potato spirit and head impurty effectively for the second time.This vapour phase is got the method and apparatus of oil, can be widely used in vapour phase and cross on the wine with dregs tower and the airway between rectifying tower or the aldehyde tower of tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 93112138 CN1086849A (en) | 1993-09-01 | 1993-09-01 | The distillating method of high grade edible spirit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 93112138 CN1086849A (en) | 1993-09-01 | 1993-09-01 | The distillating method of high grade edible spirit |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN1086849A true CN1086849A (en) | 1994-05-18 |
Family
ID=4989871
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN 93112138 Pending CN1086849A (en) | 1993-09-01 | 1993-09-01 | The distillating method of high grade edible spirit |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN1086849A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102008831A (en) * | 2010-09-27 | 2011-04-13 | 浙江金安制药机械有限公司 | Rectification and recovery system of alcohol with high purity |
| CN102119136A (en) * | 2008-09-04 | 2011-07-06 | 戴维加工技术有限公司 | Process for the purification of methanol by distillation |
| CN102787063A (en) * | 2012-09-04 | 2012-11-21 | 山东中德设备有限公司 | Distilling method for foreshots and feints of solid-fermentation white spirit and special system for implementing distilling method |
| CN103706140A (en) * | 2013-12-31 | 2014-04-09 | 泰兴金江化学工业有限公司 | Device for extracting fusel oil by alcohol distillation |
| CN105753651A (en) * | 2014-12-17 | 2016-07-13 | 中粮生化能源（肇东）有限公司 | Method for production of edible alcohol |
| CN106334327A (en) * | 2016-08-30 | 2017-01-18 | 安徽安特食品股份有限公司 | Alcohol distilling production method |
| CN107694138A (en) * | 2017-10-11 | 2018-02-16 | 肥城金威机械有限公司 | Rectifier unit, method and its application for fusel oil |
| CN108342287A (en) * | 2018-05-16 | 2018-07-31 | 广东省九江酒厂有限公司 | A kind of distillating method reducing Fusel Oil in Liquor |
-
1993
- 1993-09-01 CN CN 93112138 patent/CN1086849A/en active Pending
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102119136A (en) * | 2008-09-04 | 2011-07-06 | 戴维加工技术有限公司 | Process for the purification of methanol by distillation |
| CN102008831A (en) * | 2010-09-27 | 2011-04-13 | 浙江金安制药机械有限公司 | Rectification and recovery system of alcohol with high purity |
| CN102787063A (en) * | 2012-09-04 | 2012-11-21 | 山东中德设备有限公司 | Distilling method for foreshots and feints of solid-fermentation white spirit and special system for implementing distilling method |
| CN102787063B (en) * | 2012-09-04 | 2013-12-04 | 山东中德设备有限公司 | Distilling method for foreshots and feints of solid-fermentation white spirit and special system for implementing distilling method |
| CN103706140A (en) * | 2013-12-31 | 2014-04-09 | 泰兴金江化学工业有限公司 | Device for extracting fusel oil by alcohol distillation |
| CN105753651A (en) * | 2014-12-17 | 2016-07-13 | 中粮生化能源（肇东）有限公司 | Method for production of edible alcohol |
| CN105753651B (en) * | 2014-12-17 | 2018-05-08 | 中粮生化能源（肇东）有限公司 | A kind of method for producing edible alcohol |
| CN106334327A (en) * | 2016-08-30 | 2017-01-18 | 安徽安特食品股份有限公司 | Alcohol distilling production method |
| CN106334327B (en) * | 2016-08-30 | 2018-05-04 | 安徽安特食品股份有限公司 | A kind of alcohol distillation production method |
| CN107694138A (en) * | 2017-10-11 | 2018-02-16 | 肥城金威机械有限公司 | Rectifier unit, method and its application for fusel oil |
| CN108342287A (en) * | 2018-05-16 | 2018-07-31 | 广东省九江酒厂有限公司 | A kind of distillating method reducing Fusel Oil in Liquor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4217178A (en) | Distillation system for motor fuel grade anhydrous alcohol | |
| CN100525874C (en) | Six-column differential-pressure distillation device for extra edible alcohol and process therefor | |
| CN101153257B (en) | Five-tower two-grade difference pressure distillation equipment for senior edible ethanol and technique thereof | |
| CN102399130B (en) | Method for simplifying rectification process for preparing ethanol through hydrogenation of acetic acid | |
| CN102471195A (en) | Recovery of butanol from a mixture of butanol, water, and an organic extractant | |
| CN102471785A (en) | Recovery of butanol from a mixture of butanol, water and an organic extractant | |
| WO2019174485A1 (en) | Production method and equipment for neutral edible brewed alcohol products | |
| CN107418979A (en) | A kind of alcohol fuel energy-saving clean production method | |
| CN1814739A (en) | Method for making low-alcohol or alcohol-less raw juice fermented alcohol drink by low-temperature two-tower rectification method | |
| CN1086849A (en) | The distillating method of high grade edible spirit | |
| CN203494195U (en) | Wall-dividing rectification tower applicable to azeotropic distillation | |
| RU2678100C2 (en) | Dividing wall in ethanol purification process | |
| CN220176078U (en) | Distillation system for preparing high-quality absolute ethyl alcohol from synthetic gas fermented mash | |
| CN210495287U (en) | Novel distillation tower without extracting industrial alcohol | |
| CN110393938B (en) | Distillation tower without extracting industrial alcohol | |
| JPS6261006B2 (en) | ||
| CN1123370C (en) | Methanol and ethyl acetate separating method | |
| CN106582053B (en) | The process and device of the tower methanol distillation column by-product ethyl alcohol of partition | |
| CN214361263U (en) | Whiskey distiller for crude distillation and rectification | |
| CN211199068U (en) | Negative pressure mash tower degassing and aldehyde-discharging acid-discharging device for fuel ethanol and edible alcohol | |
| CN1179347A (en) | Multi-tower distillation method for producing alcohol of different grade | |
| CN215592969U (en) | Separation system for separating coal-to-ethanol by adopting differential pressure thermal coupling | |
| CN1047338A (en) | Distillation of edible alcohol | |
| CN206404352U (en) | The device of the tower methanol distillation column by-product ethanol of dividing plate | |
| RU2007123176A (en) | METHOD FOR THE PRODUCTION OF RECTIFIED ETHYL ALCOHOL "ALPHA" |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| C06 | Publication | ||
| PB01 | Publication | ||
| C10 | Entry into substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| C01 | Deemed withdrawal of patent application (patent law 1993) | ||
| WD01 | Invention patent application deemed withdrawn after publication |