CN101153257B - Five-tower two-grade difference pressure distillation equipment for senior edible ethanol and technique thereof - Google Patents
Five-tower two-grade difference pressure distillation equipment for senior edible ethanol and technique thereof Download PDFInfo
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- CN101153257B CN101153257B CN2007100305508A CN200710030550A CN101153257B CN 101153257 B CN101153257 B CN 101153257B CN 2007100305508 A CN2007100305508 A CN 2007100305508A CN 200710030550 A CN200710030550 A CN 200710030550A CN 101153257 B CN101153257 B CN 101153257B
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Abstract
The invention discloses a five-tower two-level differential pressure distillation device for high quality edible alcohol and the process. The top of a rectification tower is connected with a shell side inlet of a reboiler of water scrubbing tower through a pipe; a shell side vapor phase outlet of the reboiler of water scrubbing tower is connected with a shell side inlet of a reboiler of methanol tower; a shell side liquid phase outlet is connected with an inlet of a return tank of rectification tower through a pipe; a shell side outlet of the reboiler of the methanol tower is connected with the inlet of the return tank of rectification tower through a pipe; the top of the water scrubbing tower is connected with a shell side inlet of a reboiler of first fractionating tower through a pipe; a shell side outlet of the reboiler of first fractionating tower is connected with an inlet of a return tank of water scrubbing tower through a pipe; the top of the methanol tower is connected with a shell side inlet of a reboiler of second fractionating tower through a pipe, and a shell side outlet of the reboiler of second fractionating tower is connected with an inlet of a return tank of methanol tower. By adopting two-level differential pressure thermal coupling mode, for the mutually matched using of the energy, the invention ensures the stability of the process operation, makes the setting of the on-line remote centralized control by auto-control system, and also saves vapor and cooling water with environmental protection and energy saving effect.
Description
Technical field
The present invention relates to a kind of device and technology thereof of producing high grade edible spirit, especially relate to a kind of multitower difference pressure distillation equipment and technology.
Background technology
Fermentation and distillation processing through to cereal, cassava and saccharine material can make edible ethanol.Along with country to the raising of edible ethanol standard, the deterioration of domestic water resource situation and the growing tension of global energy, seek a kind ofly can improve the edible ethanol quality, rationally utilize water resources and reduce the novel process of producing the edible ethanol energy consumption and become the task of top priority fully.Produce edible ethanol multitower differential distillation commonly used at present and mainly contain following several kinds of technologies:
(1) three-tower differential pressure technology.Three towers comprise topping still, water wash column and rectifying tower, and it is more that this method is used to produce general level alcohol.And along with the raising of country to the edible ethanol standard, this three-tower differential pressure technology is applied to produce the distillation in early stage of raw spirit more and carries dense.
(2) four tower differential pressure technologies.Four towers comprise topping still, water wash column, rectifying tower and methanol column, and the output of industrial spirit is bigger when using this four towers differential pressure explained hereafter top grade alcohol, and energy consumption is higher and consumption recirculated cooling water is also big.
(3) six-column differential-pressure technology: six towers comprise topping still, dealdehyder tower, water wash column, rectifying tower, methanol column and regenerating column.Use this technology and can reach the purpose that improves the edible ethanol quality, be used for producing superfine edible ethanol more.But this six-column differential-pressure technology is comparatively complicated, so technology controlling and process is also relatively difficult, and water coolant is also corresponding with energy consumption bigger.
(4) five tower differential pressure technologies: five towers are topping still, water wash column, rectifying tower, methanol column and regenerating column, and topping still and methanol column are that vacuum distillation tower, water wash column are that little negative pressure tower, rectifying tower are that pressurizing tower, regenerating column are atmospheric tower in the five traditional tower differential pressure technologies.Rectifying tower is by the open steam indirect heating, and rectifying tower cat head wine vapour is to the topping still heat supply; Water wash column is by the open steam indirect heating, and water wash column cat head wine vapour is to the methanol column heat supply; Regenerating column is by the open steam heat supply.Use these five traditional tower differential pressure technologies and can reduce industrial spirit output, thereby improved high grade edible spirit output.But because rectifying tower only realized thermal coupling with topping still, so the rectifying tower reflux ratio receives certain limitation, and impurity-eliminating effect is undesirable, has too much low-grade energy simultaneously, and recirculated cooling water large usage quantity and energy consumption are higher.
Above deficiency in view of traditional five tower differential pressure technologies existence; These traditional five tower differential pressure technologies are improved; In application number was 200510035598.9 " alcohol quinque-towel differential pressure distilling arrangement and technology thereof ", topping still after the improvement and methanol column were vacuum distillation tower, and water wash column is little negative pressure tower; Rectifying tower is a pressurizing tower, and regenerating column is an atmospheric tower.Rectifying tower is by the open steam indirect heating, and rectifying tower cat head wine vapour is to topping still and water wash column heat supply; Water wash column cat head fume is to the methanol column heat supply, and the flash distillation water of the steam condensate under the condensation of rectifying tower reboiler after flash distillation directly feeds water wash column; Regenerating column is by the open steam heat supply.Because rectifying tower has been realized thermal coupling with topping still and water wash column simultaneously, has improved the quality of product, has reduced energy consumption; But the consumption of recirculated cooling water is still bigger, and because topping still tower still is bigger with the temperature difference of washing Tata still, the operation easier of rectifying tower is bigger, is unfavorable for the steady running of whole device.
Summary of the invention
The objective of the invention is existing quinque-towel differential pressure distilling arrangement and technology are improved, so that a kind of five-tower two-grade difference pressure distillation equipment for senior edible ethanol and technology to be provided, thereby improve the quality of edible ethanol, and reduce water consumption and energy consumption.
Technical solution of the present invention is: a kind of five-tower two-grade difference pressure distillation equipment for senior edible ethanol; Comprise topping still, water wash column, rectifying tower, methanol column and regenerating column; Wherein the rectifying tower top links to each other with water wash column reboiler shell-side inlet through pipeline; Water wash column reboiler shell-side is provided with two outlets, and wherein the shell-side vapor phase exit links to each other with methanol column reboiler shell-side inlet through pipeline, and the outlet of shell-side liquid phase links to each other with rectifying tower return tank inlet through pipeline; The outlet of methanol column reboiler shell-side links to each other with rectifying tower return tank inlet through pipeline; Link to each other with rectifying tower reflux pump inlet through pipeline at the bottom of the rectifying tower return tank, rectifying tower reflux pump exit end links to each other with rectifying tower top refluxing opening through pipeline, and the water wash column top links to each other with first topping still reboiler shell-side inlet through pipeline; The outlet of the first topping still reboiler shell-side links to each other with water wash column return tank inlet through pipeline; Water wash column return tank top links to each other with vacuum system through pipeline, and water wash column return tank bottom links to each other with water wash column reflux pump inlet end through pipeline, and water wash column reflux pump exit end links to each other with water wash column top refluxing opening through pipeline; The methanol column top links to each other with second topping still reboiler shell-side inlet through pipeline; The outlet of the second topping still reboiler shell-side links to each other with methanol column return tank inlet through pipeline; Methanol column return tank outlet at bottom links to each other with methanol column reflux pump inlet end through pipeline, and methanol column reflux pump exit end links to each other with methanol column top refluxing opening through pipeline.
Water wash column reboiler and methanol column reboiler are equivalent to first condensing surface and second condensing surface that rectifying tower cat head wine vapour passes through successively respectively; Working pressure through regulating and controlling water wash column and methanol column; Guarantee that washing Tata still temperature is more or less the same with methyl alcohol Tata still temperature; Thereby help the properly distributed of rectifying tower cat head wine vapour, can practice thrift cooling water amount, also be easy to the steady running of technology.
The outlet of methanol column reboiler shell-side is through the cold inlet side in pipe connection rectifying tower end; The cold outlet side pipe connection rectifying tower return tank inlet in rectifying tower end; Be provided with that rectifying tower end is cold can fully to guarantee condensation effect; The wine vapour that conveniently regulates and distributes rectifying tower top distributes, and further improves the stability of device.
The topping still bottom links to each other with useless wine with dregs pump intake end, the first topping still pump entry end and the second topping still pump entry end respectively through pipeline; The first topping still circulating-pump outlet end links to each other with the second topping still reboiler pipe side entrance with the first topping still reboiler respectively through pipeline with the second topping still circulating-pump outlet end, and the first topping still reboiler links to each other with topping still tower still inlet respectively through pipeline with the second topping still reboiler pipe side outlet.The useless mash of topping still bottom is divided into three strands, can regulate reboiler institute heat requirement through regulating each burst amount, further reduces cooling water amount.
The outlet of the first topping still reboiler shell-side is connected with the cold inlet side in water wash column end through pipeline, and the cold outlet side pipe connection water wash column return tank inlet in water wash column end can fully guarantee condensation effect, convenient operational stability of regulating the washing Tata.
The outlet of the second topping still reboiler shell-side is cold inlet side through pipe connection methanol column end, and the cold outlet side pipe connection methanol column return tank inlet in methanol column end can fully guarantee condensation effect, convenient operational stability of regulating methanol column.
Rectifying tower reboiler steam condensation-water drain end is connected with the flash tank inlet end through pipeline, and the flash distillation tank deck is connected with recovery Tata still through pipeline, reduces the influence to technology stability of flash steam feeding water wash column or topping still, is convenient to automation technolo control.
Another technical solution of the present invention is: a kind of high grade edible spirit five tower secondary differential distillation production technique; From the maturing fermentation mash that fermentation workshop section comes, through getting into topping still after the first ripening wine with dregs preheater and the second ripe wine with dregs preheater preheating, the thick wine vapour at topping still top is successively through after the first ripe wine with dregs preheater and the topping still condenser condenses successively; The thick wine liquid that imports thick wine jar is through crude wine preheater; The rectifying tower tower bottom that comes with rectifying tower waste water pump pump divides that the waste water preheating is laggard goes into water wash column, and the thick wine liquid that gets into water wash column is after waste water washing at the bottom of the rectifying Tata, and most of light constituent impurity is discharged by the water wash column top; The light wine after removal of impurities that the water wash column bottom is come pumps into the light wine preheater by the light wine pump; By getting into rectifying tower after the waste water preheating that comes at the bottom of the rectifying tower, water wash column cat head wine vapour is after the first topping still reboiler condensation, and phlegma gets into the water wash column return tank; Pump into water wash column through the water wash column reflux pump and reflux, condensing does not feed the vacuum cleaning tower; The light wine that gets into rectifying tower concentrates wine liquid by the rectifier extraction and sends into methanol column after rectifying concentrates; Rectifying tower top wine vapour is successively through water wash column reboiler and the condensation of methanol column reboiler; Phlegma gets into the rectifying tower return tank, pumps into the rectifying tower top by the rectifying tower reflux pump again and refluxes; , the concentrated wine that rectifying tower comes excludes most of methyl alcohol after getting into methanol column; Wine liquid is seen the battery limit (BL) off by the finished product volume pump after after discharge pump pumps into the cooling of finished product water cooler, getting into the finished product jar again at the bottom of the tower; Methanol column cat head wine vapour is successively through the second topping still reboiler condensation; Phlegma gets into the methanol column return tank, pumps into the methanol column top by the methanol column reflux pump again and refluxes.
Rectifying tower top wine vapour is cold with fixed attention through water wash column reboiler, methanol column reboiler and rectifying tower end successively, and phlegma gets into the rectifying tower return tank, pumps into the rectifying tower top by the rectifying tower reflux pump again and refluxes; The useless mash of topping still bottom is partly discharged outside the battery limit (BL), and part gets into topping still tower still through the first topping still reboiler and the second topping still reboiler respectively.
After the first topping still reboiler and last cold the coagulating of water wash column, phlegma gets into the water wash column return tank to water wash column cat head wine vapour, pumps into water wash column through the water wash column reflux pump and refluxes successively, and condensing feeds the vacuum cleaning tower; Methanol column cat head wine vapour is cold with fixed attention through the second topping still reboiler and methanol column end successively, and phlegma gets into the methanol column return tank, pumps into the methanol column top by the methanol column reflux pump again and refluxes.
As a kind of prioritization scheme, each column overhead working pressure, cat head and column bottom temperature are respectively:
Topping still cat head absolute pressure 0.3～0.6kg/cm
2, 50～70 ℃ of tower top temperatures, 70～90 ℃ of column bottom temperatures;
Water wash column cat head absolute pressure 0.7～1.0kg/cm
2, 90～105 ℃ of tower top temperatures, 90～110 ℃ of column bottom temperatures;
Rectifying tower cat head absolute pressure 2.5～3.5kg/cm
2, 102～112 ℃ of tower top temperatures, 127～142 ℃ of column bottom temperatures;
Methanol column cat head absolute pressure 1.5～2.5kg/cm
2, 85～105 ℃ of tower top temperatures, 90～110 ℃ of column bottom temperatures;
Regenerating column cat head absolute pressure 1.0～1.1kg/cm
2, 78～85 ℃ of tower top temperatures, column bottom temperature is 102～115 ℃.
Advantage of the present invention is: adopt secondary differential pressure thermal coupling technology to realize the mutual coupling utilization of energy; Guaranteed the stability of technological operation; Be convenient to the online remote centralized control through robot control system(RCS) is set, can also practice thrift steam consumption and cooling-water consumption, environmental protection and energy saving.
Description of drawings
Accompanying drawing 1 is a technical process schematic diagram of the present invention;
1. first ripening wine with dregs preheater, the 2. second ripe wine with dregs preheater, 3. topping still condensing surface, 4. vacuum cleaning tower, 5. vacuum pump, 6. topping still, 7. useless wine with dregs pump; 8. the first topping still reboiler, the 9. first topping still recycle pump, the 10. second topping still reboiler, 11. second topping still recycle pumps, 12. thick wine jars, 13. thick wine pumps; 14. crude wine preheater, 15. water wash columns, 16. water wash column ends are cold, 17. water wash column return tanks, 18. water wash column reflux pumps, 19. light wine pumps; 20. the light wine preheater, 21. rectifying tower, 22. water wash column reboilers, 23. methanol column reboilers, 24. rectifying tower ends are cold, 25. rectifying tower return tanks; 26. the rectifying tower reflux pump, 27. rectifying tower reboilers, 28. rectifying tower waste water pumps, 29. methanol columns, 30. methanol column ends are cold, 31. methanol column return tanks; 32. the methanol column reflux pump, 33. discharge pumps, 34. finished product water coolers, 35. finished product jars, 36. finished product volume pumps, 37. assorted wine jars; 38. assorted wine pump, 39. assorted wine preheaters, 40. regenerating columns, 41. regenerating column ends are cold, 42. regenerating column return tanks, 43. regenerating column reflux pumps; 44. the regenerating column waste water pump, 45. potato spirit water coolers, 46. potato spirit separators, 47. potato spirit basins, 48. fusel oil pumps, 49. flash tanks.
Embodiment
Embodiment: shown in accompanying drawing 1; Quinque-towel differential pressure distilling arrangement includes topping still 6, water wash column 15, rectifying tower 21, methanol column 29 and regenerating column 40; Wherein rectifying tower 21 top exits link to each other with water wash column reboiler 22 shell-sides inlet through pipeline; Water wash column reboiler 22 shell-sides are provided with two outlets; Wherein the shell-side vapor phase exit links to each other with methanol column reboiler 23 shell-sides inlet through pipeline; The outlet of shell-side liquid phase links to each other with rectifying tower return tank 25 inlets through pipeline, and the outlet of methanol column reboiler 23 shell-sides also links to each other with rectifying tower return tank 25 inlets through pipeline, and rectifying tower return tank 25 outlet at bottoms link to each other with rectifying tower reflux pump 26 inlet ends through pipeline; Rectifying tower reflux pump 26 exit end link to each other with rectifying tower 21 top refluxing openings through pipeline; Smart stream tower 21 outlet at bottoms link to each other with light wine preheater 20 1 side entrances through pipeline, and light wine preheater 20 1 side outlets link to each other with rectifying tower waste water pump 28 inlet ends through pipeline, and rectifying tower waste water pump 28 inlet ends link to each other with water wash column 15 top water inlets with crude wine preheater 14 1 side entrances respectively through pipeline; Rectifying tower reboiler 27 vapor condensation water outs through pipeline with link to each other with flash tank 49 inlet, flash tank 49 top exits link to each other with regenerating column 40 tower stills inlet through pipeline, outlet at bottom through pipeline towards going to the boiler tubing system; Water wash column 15 top exits link to each other with the first topping still reboiler, 8 shell-sides inlet through pipeline; The outlet of the first topping still reboiler, 8 shell-sides links to each other with water wash column return tank 17 inlets through pipeline; Water wash column return tank 17 top exits link to each other with vacuum system through pipeline; Water wash column return tank 17 bottoms link to each other with water wash column reflux pump 18 inlet ends through pipeline, and water wash column reflux pump 18 exit end link to each other with water wash column 15 top refluxing openings through pipeline, and water wash column 15 outlet at bottoms link to each other through pipeline light wine pump 19 inlet ends; Light wine pump 19 exit end link to each other with light wine preheater 20 2 side entrances through pipeline, and light wine preheater 20 2 side outlets link to each other with rectifying tower 21 centre entrances through pipeline; Methanol column 29 top exits link to each other with the second topping still reboiler, 10 shell-sides inlet through pipeline; The outlet of the second topping still reboiler, 10 shell-sides links to each other with methanol column return tank 31 inlets through pipeline; Methanol column return tank 31 outlet at bottoms link to each other with methanol column reflux pump 32 inlet ends through pipeline; Methanol column reflux pump 32 exit end link to each other with methanol column 29 top refluxing openings through pipeline, and methanol column 29 outlet at bottoms link to each other with discharge pump 33 inlet ends through pipeline.
Topping still 6 top exits link to each other with first ripening wine with dregs preheater 1 shell-side inlet through pipeline; First ripening wine with dregs preheater 1 shell-side lower part outlet end links to each other with thick wine jar 12 inlets through pipeline; The outlet of first ripening wine with dregs preheater 1 shell-side top links to each other with topping still condensing surface 3 inlets through pipeline; The outlet of condensing surface 3 tops links to each other with vacuum system through pipeline; Condensing surface 3 lower part outlets also link to each other with thick wine jar 12 inlets through pipeline; Topping still 6 bottoms link to each other with useless wine with dregs pump 7 inlet ends, the first topping still recycle pump, 9 inlet ends and the second topping still recycle pump, 11 inlet ends respectively through pipeline; The first topping still recycle pump, 9 exit end link to each other with the second topping still reboiler, 10 pipe side entrances with the first topping still reboiler 8 respectively through pipeline with the second topping still recycle pump, 11 exit end, and the first topping still reboiler 8 links to each other with topping still 6 tower stills inlet respectively through pipeline with the second topping still reboiler, 10 pipe side outlets; Regenerating column 40 top exits link to each other with the second ripe wine with dregs preheater 2 shell-sides inlet through pipeline; The second ripe wine with dregs preheater 2 shell-sides outlet links to each other with regenerating column return tank 42 inlets through pipeline; Regenerating column return tank 42 outlet at bottoms link to each other with regenerating column reflux pump 43 inlet ends through pipeline; Regenerating column reflux pump 43 exit end link to each other with regenerating column 40 top refluxing openings through pipeline; Regenerating column 40 outlet at bottoms link to each other with assorted wine preheater 39 1 side entrances through pipeline, and assorted wine preheater 39 1 side outlets are continuous through the pipeline inlet end that links to each other with regenerating column waste water pump 44, regenerating column waste water pump 44 exit end with go out the battery limit (BL) tubing system and link to each other.
From the washing light wine of vacuum cleaning tower 4, from the assorted wine of water wash column return tank 17, import assorted wine jar 37 from the assorted wine of rectifying tower return tank 25 and the extraction of rectifying tower stage casing; Pump into light wine preheater 39 sides by assorted wine pump 38 then and after preheating, send into regenerating column; The assorted wine that potato spirit is rich in the place's extraction of several laminates more than regenerating column 40 feed plates is sent into potato spirit water cooler 45 cooling backs and is got into potato spirit separators 46 and isolate potato spirit, and the assorted wine of isolating behind the potato spirit gets into assorted wine jar 37 by the pipeline of potato spirit separator 46 bottoms.
The process flow of material is to being: the maturing fermentation mash that the workshop section of fermenting certainly comes; After 1 and second ripe wine with dregs preheater 2 preheatings of first ripening wine with dregs preheater, get into topping still 6; Thick wine vapour by topping still 6 tops is condensed into through first ripening wine with dregs preheater 1 and condensing surface 3 and slightly gets into thick wine jar 12 after drinking; Thick wine pumps into crude wine preheater 14 by thick wine pump 13 and goes into water wash column 15 through preheating is laggard; Light wine flows out from water wash column 15 bottoms after washing; Pump into light wine preheater 20 by light wine pump 19 and after preheating, get into rectifying tower 21, it is refining to get into methanol column 29 after the concentrated wine liquid after rectifying concentrates is adopted the extraction of wine mouth by rectifying tower 21 tops, and the high grade edible spirit after methanol column 29 is made with extra care is drawn by methanol column 29 bottoms after cooling and pumped into the finished product jar.
Producing 13.5 ten thousand tons of high grade edible spirit devices per year with northeast grain distillery is example, further specifies technological process of the present invention:
Before transforming, application number is 200510035598.9 " alcohol quinque-towel differential pressure distilling arrangement and technology thereof ", the working pressure of its each column overhead, temperature are:
Topping still 6 absolute pressure 0.35kg/cm
2, 55 ℃ of tower top temperatures, 82 ℃ of column bottom temperatures;
Rectifying tower 21 absolute pressure 2.30kg/cm
2, 100 ℃ of tower top temperatures, 128.5 ℃ of column bottom temperatures;
Regenerating column 40 absolute pressure 1.00kg/cm
2, 79 ℃ of tower top temperatures, 106 ℃ of column bottom temperatures.
Improved device is five tower secondary difference pressure distillation equipments of the present invention, and its each column overhead working pressure, cat head and column bottom temperature are respectively:
Topping still 6 cat head absolute pressures 0.3～0.6kg/cm
2, 50～70 ℃ of tower top temperatures, 70～90 ℃ of column bottom temperatures;
Rectifying tower 21 cat head absolute pressures 2.5～3.5kg/cm
2, 102～112 ℃ of tower top temperatures, 127～142 ℃ of column bottom temperatures;
Regenerating column 40 cat head absolute pressures 1.0～1.1kg/cm
2, 78～85 ℃ of tower top temperatures, column bottom temperature is 102～115 ℃.
215.8 tons/hour of come from fermentation workshop section 30 ℃ maturing fermentation wine with dregs that contain wine 10.5% (v/v);, first ripening wine with dregs preheater 1 is preheating to 62 ℃ by the second ripe wine with dregs preheater 2 again after being preheating to 52 ℃; Get into by topping still 6 tops then; Come out from topping still 6 tops 66 ℃ contain thick wine vapour about wine 58% (v/v) after first ripening wine with dregs preheater 1 and 3 condensations of topping still condensing surface; By sending into water wash column 15 after crude wine preheater 14 preheatings, the 95 ℃ of light wine that contain about wine 15% (v/v) after washing that come out from water wash column 15 bottoms are sent into rectifying tower 21 after 20 preheatings of light wine preheater again, and after rectifying concentrates 108 ℃ contain the concentrated wine of wine 96% or more and send into methanol column 29 after by rectifying tower 21 top extraction and make with extra care; After the refining liquor liquid that after refining 98 ℃ contain wine 96% is discharged by methanol column 29 bottoms; Be cooled to 30 ℃, promptly obtain 18.9 tons/hour of finished product high grade edible spirits, the ton product steam consumption of this technology is about 2.3 tons.
The present invention is second stage condensation through the methanol column reboiler because rectifying tower top wine vapour is first step condensation through the water wash column reboiler in order then, and aftercooler to the end again reaches and helps impurities removal, the effect of stable operation.Thereby make quality product, further improve.
The quality product of device production edible ethanol is as shown in the table before and after transforming:
| Index name | Unit | Chinese Industrial Standards (CIS) (GB10343-2002) | The quality product (application number 200510035598.9) that five tower differential distillation technologies and equipment thereof are produced | The quality product that five tower secondary differential distillation technologies of the present invention and equipment thereof are produced | |
| Superfine | Top grade | (1) | (2) | ||
| Colourity<= | Number | 10 | 10 | 8 | 8 |
| Ethanol content >= | ％(v/v) | 96.0 | 95.5 | 95.5 | 95.5 |
| Sulfuric acid test<= | Number | 5 | 10 | 10 | 10 |
| Oxidization time >= | min | 40 | 30 | 31 | 31 |
| Total aldehyde (in acetaldehyde)<= | mg/l | 1 | 3 | / | / |
| Methyl alcohol<= | mg/l | 2 | 50 | 34 | 15 |
| N-propyl alcohol<= | mg/l | 2 | 35 | 5 | 2 |
| Isopropylcarbinol+primary isoamyl alcohol<= | mg/l | 1 | 2 | Do not have | Do not have |
| Total acid (with acetometer)<= | mg/l | 7 | 10 | 10 | 10 |
| Total ester (in ETHYLE ACETATE)<= | mg/l | 10 | 18 | / | / |
| Non-volatile matter<= | mg/l | 10 | 20 | / | / |
| Heavy metal (in Pb)<= | mg/l | 1 | / | / | |
| Prussiate (in HCN)<= | mg/l | 5* | / | / | |
| Annotate: with the cassava is the requirement of raw material, and the alcohol of processing with other raw material does not have this requirement. | |||||
Can find out from last table,, adopt technology of the present invention to descend greater than 50% than old technology for methyl alcohol very important in industry, n-propyl alcohol index.Wherein n-propyl alcohol also reaches the standard of superfine alcohol.
Above-listed detailed description is to the specifying of possible embodiments of the present invention, and this embodiment is not in order to limiting claim of the present invention, and the equivalence that all the present invention of disengaging do is implemented or change, all should be contained in the claim of this case.
Claims (10)
1. five-tower two-grade difference pressure distillation equipment for senior edible ethanol; Comprise topping still (6), water wash column (15), rectifying tower (21), methanol column (29) and regenerating column (40); It is characterized in that: wherein rectifying tower (21) top links to each other with water wash column reboiler (22) shell-side inlet through pipeline; Water wash column reboiler (22) shell-side is provided with two outlets; Wherein the shell-side vapor phase exit links to each other with methanol column reboiler (23) shell-side inlet through pipeline; The outlet of shell-side liquid phase links to each other with rectifying tower return tank (25) inlet through pipeline, and the outlet of methanol column reboiler (23) shell-side links to each other with rectifying tower return tank (25) inlet through pipeline, and rectifying tower return tank (25) end links to each other with rectifying tower reflux pump (26) inlet through pipeline; Rectifying tower reflux pump (26) exit end links to each other with rectifying tower (21) top refluxing opening through pipeline; Water wash column (15) top links to each other through pipeline and first topping still reboiler (8) shell-side inlet, and the outlet of first topping still reboiler (8) shell-side enters the mouth with water wash column return tank (17) through pipeline and links to each other, water wash column return tank (17) top through pipe connection in vacuum cleaning tower (4); Water wash column return tank (17) bottom links to each other with water wash column reflux pump (18) inlet end through pipeline, and water wash column reflux pump (18) exit end links to each other with water wash column (15) top refluxing opening through pipeline; Methanol column (29) top links to each other with second topping still reboiler (10) shell-side inlet through pipeline; The outlet of second topping still reboiler (10) shell-side links to each other with methanol column return tank (31) inlet through pipeline; Methanol column return tank (31) outlet at bottom links to each other with methanol column reflux pump (32) inlet end through pipeline, and methanol column reflux pump (32) exit end links to each other with methanol column (29) top refluxing opening through pipeline.
2. five-tower two-grade difference pressure distillation equipment for senior edible ethanol according to claim 1; It is characterized in that: the outlet of methanol column reboiler (23) shell-side is through pipe connection rectifying tower end cold (24) inlet side, and rectifying tower end cold (24) outlet side pipe connection rectifying tower return tanks (25) enter the mouth.
3. five-tower two-grade difference pressure distillation equipment for senior edible ethanol according to claim 1; It is characterized in that: topping still (6) bottom links to each other with useless wine with dregs pump (7) inlet end, first topping still recycle pump (9) inlet end and second topping still recycle pump (11) inlet end respectively through pipeline; First topping still recycle pump (9) exit end links to each other with the second topping still reboiler (10) pipe side entrance with the first topping still reboiler (8) respectively through pipeline with second topping still recycle pump (11) exit end, and the first topping still reboiler (8) links to each other with topping still (6) tower still inlet respectively through pipeline with the second topping still reboiler (10) pipe side outlet.
4. five-tower two-grade difference pressure distillation equipment for senior edible ethanol according to claim 3; It is characterized in that: inlet side is connected the outlet of first topping still reboiler (8) shell-side through pipeline and water wash column end cold (16), water wash column end cold (16) outlet side pipe connection water wash column return tanks (17) inlet.
5. five-tower two-grade difference pressure distillation equipment for senior edible ethanol according to claim 3; It is characterized in that: the outlet of second topping still reboiler (10) shell-side is inlet side through pipe connection methanol column end cold (30), methanol column end cold (30) outlet side pipe connection methanol column return tanks (31) inlet.
6. according to claim 1,2,3,4 or 5 described five-tower two-grade difference pressure distillation equipment for senior edible ethanol; It is characterized in that: rectifying tower reboiler (27) steam condensate exit end is connected with flash tank (49) inlet end through pipeline, and flash tank (49) top is connected with regenerating column (40) tower still through pipeline.
7. technology of utilizing the described five tower secondary difference pressure distillation equipments of claim 1 to produce high grade edible spirit; It is characterized in that: from the next maturing fermentation mash of fermentation workshop section; Get into topping still (6) after passing through the first ripening wine with dregs preheater (1) and second ripe wine with dregs preheater (2) preheating successively; The thick wine vapour at topping still (6) top is successively through after the first ripe wine with dregs preheater (1) and topping still condensing surface (3) condensation; Import thick wine jar (12), the thick wine liquid in the thick wine jar (12) is through crude wine preheater (14), and rectifying tower (21) tower bottom with rectifying tower waste water pump (28) pump divides that the waste water preheating is laggard goes into water wash column (15); The thick wine liquid that gets into water wash column (15) is after waste water washing at the bottom of rectifying tower (21) tower; Most of light constituent impurity is discharged by water wash column (15) top, and the light wine after removal of impurities that comes from water wash column (15) bottom pumps into light wine preheater (20) by light wine pump (19), by getting into rectifying tower (21) after rectifying tower (21) the waste water preheating at the end; Water wash column (15) cat head wine vapour is after first topping still reboiler (8) condensation; Phlegma gets into water wash column return tank (17), pumps into water wash column (15) through water wash column reflux pump (18) and refluxes, and condensing does not feed vacuum cleaning tower (4) by water wash column return tank (17); The light wine that gets into rectifying tower (21) concentrates wine liquid by rectifying tower (21) top extraction and sends into methanol column (29) after rectifying concentrates; Rectifying tower (21) top wine vapour is successively through water wash column reboiler (22) and methanol column reboiler (23) condensation; Phlegma gets into rectifying tower return tank (25), pumps into rectifying tower (21) top by rectifying tower reflux pump (26) again and refluxes; , the concentrated wine that rectifying tower (21) comes excludes most of methyl alcohol after getting into methanol column (29); Wine liquid is seen the battery limit (BL) off by finished product volume pump (36) after after discharge pump (33) pumps into finished product water cooler (34) cooling, getting into finished product jar (35) again at the bottom of the tower; Methanol column (29) cat head wine vapour is successively through second topping still reboiler (10) condensation; Phlegma gets into methanol column return tank (31), pumps into methanol column (29) top by methanol column reflux pump (32) again and refluxes.
8. five tower secondary difference pressure distillation equipments according to claim 7 are produced the technology of high grade edible spirit; It is characterized in that: rectifying tower (21) top wine vapour is successively through water wash column reboiler (22), methanol column reboiler (23) and rectifying tower end cold (24) condensation; Phlegma gets into rectifying tower return tank (25), pumps into rectifying tower (21) top by rectifying tower reflux pump (26) again and refluxes; The useless mash of topping still (6) bottom is partly discharged outside the battery limit (BL), and part gets into topping still (6) tower still through the first topping still reboiler (8) and the second topping still reboiler (10) respectively.
9. five tower secondary difference pressure distillation equipments according to claim 7 are produced the technology of high grade edible spirit; It is characterized in that: water wash column (15) cat head wine vapour is successively after the first topping still reboiler (8) and water wash column end cold (16) condensation; Phlegma gets into water wash column return tank (17); Pump into water wash column (15) through water wash column reflux pump (18) and reflux, condensing does not feed vacuum cleaning tower (4) by water wash column return tank (17); Methanol column (29) cat head wine vapour is successively through the second topping still reboiler (10) and methanol column end cold (30) condensation, and phlegma gets into methanol column return tank (31), pumps into methanol column (29) top by methanol column reflux pump (32) again and refluxes.
10. the technology of producing high grade edible spirit according to claim 7,8 or 9 described five tower secondary difference pressure distillation equipments, it is characterized in that: each column overhead working pressure, cat head and column bottom temperature are respectively: topping still (6) cat head absolute pressure 0.3～0.6kg/cm
2, 50～70 ℃ of tower top temperatures, 70～90 ℃ of column bottom temperatures;
Water wash column (15) cat head absolute pressure 0.7～1.0kg/cm
2, 90～105 ℃ of tower top temperatures, 90～110 ℃ of column bottom temperatures;
Rectifying tower (21) cat head absolute pressure 2.5～3.5kg/cm
2, 102～112 ℃ of tower top temperatures, 127～142 ℃ of column bottom temperatures;
Methanol column (29) cat head absolute pressure 1.5～2.5kg/cm
2, 85～105 ℃ of tower top temperatures, 90～110 ℃ of column bottom temperatures;
Regenerating column (40) cat head absolute pressure 1.0～1.1kg/cm
2, 78～85 ℃ of tower top temperatures, column bottom temperature is 102～115 ℃.
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| CN101748037B (en) * | 2009-11-23 | 2013-12-11 | 广东中科天元新能源科技有限公司 | Special grade edible alcohol six-tower difference pressure distilling device and process thereof |
| CN101798265B (en) * | 2010-02-05 | 2013-09-18 | 天津大学 | Novel method for preparing vinyl acetate from bioethanol |
| CN101851149A (en) * | 2010-05-24 | 2010-10-06 | 中国轻工业西安设计工程有限责任公司 | Energy-saving method and energy-saving system for producing edible ethanol by five-tower three-stage differential distillation |
| CN102492597B (en) * | 2011-12-09 | 2013-04-03 | 杜永生 | System and method for removing impurity from liquor |
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| 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 |
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| CN112902686B (en) * | 2021-01-26 | 2022-08-16 | 河北易高生物能源有限公司 | Furfural primary distillation tower steam recycling method |
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