CN106478368B - Produce the energy-saving rectifying process and device of high grade edible spirit - Google Patents
Produce the energy-saving rectifying process and device of high grade edible spirit Download PDFInfo
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- CN106478368B CN106478368B CN201710004713.9A CN201710004713A CN106478368B CN 106478368 B CN106478368 B CN 106478368B CN 201710004713 A CN201710004713 A CN 201710004713A CN 106478368 B CN106478368 B CN 106478368B
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
- C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
- C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
- C07C29/80—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by distillation
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
Abstract
The present invention relates to a kind of energy-saving rectifying process for producing high grade edible spirit and devices, it is a kind of energy saver and process for producing high grade edible spirit by distillation process from fermentation liquid.Entire ethanol refinery device includes at least five towers and its corollary equipment compositions such as prefractionator T101, water scrubber T102, the first smart tower T103, the smart tower T105 of eparating methanol tower T104 and second.The shortcomings that the present invention overcomes prior arts is thermally integrated process using the quadruple effect of single column heat supply breakthroughly on the Process ba- sis of common multitower heating, in addition other heat exchange, the application of power-saving technology significantly reduce operation energy consumption in system.It overcomes the shortcomings that prior art, operation energy consumption is down to 1.7 tons of steam/ton high grade edible spirit, top grade ethanol refinery process operation energy consumption than being widely used at present reduces by 40% or more, has significant practicability and huge economic benefit, has a extensive future.
Description
Technical field
The present invention relates to a kind of energy-saving rectifying process for producing high grade edible spirit and devices, it is a kind of from fermentation
The energy saver and process of high grade edible spirit are produced in mash by distillation process.
Background technique
The problems such as with the in short supply of the energy resources such as petroleum, coal, environmental pollution, greenhouse effects, gets worse, alcohol
Etc. industries energy conservation, consumption reduction have become Business survival and improve competitiveness key, increasingly by the attention of various aspects.
At present from the process of fermentation liquid production high grade edible spirit, the general method for using multitower rectifying process.It is " newly organized
Alcohol technology " in (publication of in July, 2004 Beijing Chemical Industry Press university teaching publishing centre) book, for it is domestic
You Duojia Alcohol Plant uses five tower differential distillation techniques, has done more detailed summary and introduction.Typically topping still is negative
Under the conditions of pressure, with the positive pressure fume (secondary steam) of the top of the distillation column, the recycle stock of heating topping still reboiler is removed；Water scrubber
It is atmospheric operation, tower top wine vapour (secondary steam) is gone to the methanol tower reboiler heat supply of negative-pressure operation.It is utilized again in this way
The thermal energy of the tower top fume (secondary steam) of two tower of rectifying column and water scrubber.Although this process has used some differential pressure sections
Energy measure, but its steam consumption for producing top grade alcohol per ton is still up to 3.0~4.2t/t finished product alcohol, constrains alcohol industry
The economy of production.
Chinese patent CN200510035598.9 provides a kind of " alcohol quinque-towel differential pressure distilling arrangement and technique ": using five
Column differential-pressure distillation device produces high grade edible spirit, and Distallation systm includes topping still, rectifying column, water scrubber, methanol column and recycling
Tower, Distallation systm institute calorific requirement are added by the tower reactor of rectifying column and recovery tower respectively；Rectifying tower top gaseous phase is divided into two strands, respectively
It is heated to the reboiler of topping still and water scrubber；Water scrubber top gaseous phase is heated to methanol column tower reactor reboiler.Its core is one
Kind triple-effect differential pressure distillation technique, this method energy consumption of rectification is in 2.3~2.6t steam/t alcohol, although more energy saving than traditional handicraft,
But steam consumption or relatively high.
Chinese patent CN200710030550.8 provide it is a kind of " five-tower two-grade difference pressure distillation equipment for senior edible ethanol and
Its technique ": using five towers such as topping still, water scrubber, rectifying column, methanol column and recovery tower, Distallation systm institute calorific requirement respectively by
The tower reactor of rectifying column and recovery tower is added；Rectifying tower top gaseous phase successively gives the reboiler of methanol column and water scrubber to heat；Washing
The top gaseous phase of tower and methanol column gives the reboiler of topping still to heat respectively；Recovery tower tower reactor heats steam using tower bottom of rectifying tower
Secondary steam or the live steam heating that lime set flashes off, recovery tower top gaseous phase is for heating topping still charging.Its core
It is a kind of triple-effect differential pressure distillation technique, the only sequence variation of triple-effect differential pressure, the energy consumption and CN of this method rectifying
Process disclosed in 200510035598.9 is suitable, and about 2.3 tons of the steam consumption quantity of alcohol product per ton, steam consumption or phase
To higher.
Chinese patent CN201410357357.5 discloses a kind of " alcohol distillation of molasses raw material top grade and waste liquid concentration thermal coupling
Attach together set and technique ": using four column differential-pressure distillation devices produce high grade edible spirit, Distallation systm include topping still, water scrubber,
Methanol column and rectifying column, Distallation systm institute calorific requirement are added by tower bottom of rectifying tower；Rectifying tower top gaseous phase successively give methanol column and
The reboiler of water scrubber heats；The top gaseous phase of water scrubber and methanol column gives the reboiler of topping still to heat respectively.Its core is still
It is a kind of triple-effect differential pressure distillation technique, compared with the process that CN200710030550.8 is provided, triple effect steams this process
It is almost the same to evaporate process, recovery tower is only omitted.The energy consumption and 200510035598.9 disclosure of CN of this process rectifying
Process it is suitable, steam consumption or relatively high.
Chinese patent CN201510850323.4 provides a kind of " for producing double smart tower quadruple effect top grade alcohol steamings of alcohol
Evaporate method and apparatus ": entire ethanol refinery device includes prefractionator, a smart tower, two smart towers, water scrubber, eparating methanol tower and recovery tower,
Distallation systm institute calorific requirement is added by the tower reactor of a smart tower and recovery tower respectively；One smart column overhead gas phase adds to two smart tower reboilers
Heat；Two smart column overhead gas phases are divided into two strands, respectively to eparating methanol tower reboiler and washing tower reboiler I heating；Recycle column overhead
Gas phase gives washing tower reboiler II heating；Eparating methanol tower top gaseous phase is heated to prefractionator reboiler I, and water scrubber top gaseous phase is to wine with dregs
Tower reboiler II heating.Its core is a kind of quadruple effect differential distillation technique, this method production energy consumption in 1.8t steam/t alcohol,
Energy-saving effect is relatively good, but the method process is complicated.Using prefractionator as the 4th effect in this distilling apparatus, prefractionator kettle material is base
This nonalcoholic waste water containing wine with dregs, this route necessarily lead to the increasing of differential pressure amplitude, the operating pressure meeting of the 1st effect (a smart tower)
It is higher, it is up to 1.0MPa or more.It is well known that the alcohol distillation operating pressure the low more is conducive to the removal of other impurities, and
And too high operating pressure, also necessarily lead to the raising of operation temperature, it is also unfavorable to the safety of distillation procedure.
Chinese patent CN201010547354.X provides a kind of " using three rectification-tower heat-integration alcohol rectification energy-saving technique sides
Method ": a kind of energy-saving process method producing alcohol by distillation process from fermentation liquid, entire ethanol refinery system are at least wrapped
Include three tower such as first rectifying column, Second distillation column and third distillation column and its corollary equipment composition, first rectifying column, the second rectifying
It is thermally integrated between three tower of tower and third distillation column.Its core is a kind of triple-effect differential pressure distillation technique, and this method is due to entire work
Lack water scrubber and eparating methanol tower in process and equipment, therefore the alcohol product impurity content obtained is relatively high, is only used for producing
Alcohol fuel and general grade edible ethanol, application field are limited.
Summary of the invention
The purpose of the present invention is to provide a kind of energy-saving rectifying process for producing high grade edible spirit and devices, it is
A kind of energy saver and process producing high grade edible spirit by distillation process from fermentation liquid.Entire ethanol refinery
Device includes at least five towers and its corollary equipment compositions such as prefractionator, water scrubber, the first smart tower, eparating methanol tower and the second smart tower.This
The shortcomings that invention overcomes prior art, on the Process ba- sis of common multitower heating, breakthroughly using single column heat supply
Quadruple effect is thermally integrated process, significantly reduces operation energy consumption, and the steam consumption of high grade edible spirit per ton is reduced to 1.7 tons, this
Invention has significant practicability and economic benefit.
A kind of energy-saving rectifying process producing high grade edible spirit provided by the invention includes the following steps:
1) five towers such as prefractionator, water scrubber, the first smart tower, eparating methanol tower and the second smart tower are included at least；
2) rectifier unit institute calorific requirement is all added by the second smart tower tower reactor；
3) the second smart tower and prefractionator are thermally integrated operation, and prefractionator tower reactor institute's calorific requirement is provided by the second smart column overhead gas phase；
4) prefractionator and water scrubber are thermally integrated operation, and water scrubber tower reactor institute's calorific requirement is provided by prefractionator top gaseous phase；
5) water scrubber and the first smart tower and eparating methanol tower are thermally integrated operation, water scrubber top gaseous phase be respectively the first smart tower with
Eparating methanol tower tower reactor provides institute's calorific requirement.
Described second smart tower is the first effect, and prefractionator is the second effect, and water scrubber is third effect, and the first smart tower and eparating methanol tower are
Quadruple effect, above-mentioned five tower constitute a kind of energy saver of quadruple effect heat-integration alcohol rectifying.
By process provided by the invention, the maturing fermentation mash come from fermentation procedure first passes through the first smart tower condenser
It is preheated with the first smart column overhead fume, then through the useless wine with dregs preheating of prefractionator tower reactor of mash preheater, then into prefractionator top.
The prefractionator and water scrubber are thermally integrated operation, and for prefractionator tower top fume into water scrubber tower reactor reboiler shell side, fume is cold
Material after solidifying is into light wine tank.After completing gas-liquid separation in light wine tank, gas phase and liquid phase are respectively into water scrubber tower middle part.
The water scrubber and the first smart tower and eparating methanol tower are thermally integrated operation, the smart tower tower of washing column overhead fume advanced first
Kettle reboiler shell side, the condensed material of fume is into water scrubber return tank.After completing gas-liquid separation in water scrubber return tank, gas
Phase logistics is again into eparating methanol tower reboiler shell side.After logistics condensate gas-liquid separation, gas phase removes water scrubber tail cooler, and liquid phase is into returning
Flow tank.Water scrubber tail cooler outlet fixed gas removes exhaust treatment system, and water scrubber tail cooler lime set is divided into two strands, one is used as and adopts
Out into aldehyde wine, another part is into water scrubber return tank.Water scrubber return tank outlet liquid phase is divided into two strands, a part of and circulation wash water
Column overhead is washed together as the water inlet of water scrubber phegma, another part is produced into aldehyde wine.The first smart tower is removed in the discharging of water scrubber tower reactor
Lower part.
Described first smart column overhead gas phase first exchanges heat through the first smart tower condenser and fermentation liquid, and not solidifying gas phase is again through first
Smart tower tail cooler condensation, fixed gas go vacuum system, and the first smart tower condenser, the first smart tower tail cooler lime set are returned into the first smart tower
Flow tank.Wherein the part lime set of the first smart tower tail cooler is as industrial alcohol discharger.First smart tower return tank exports liquid phase
As the first smart tower phegma into the first smart column overhead.
Into eparating methanol tower top, eparating methanol tower top gaseous phase 43 is returned for described first smart tower top side line Extract phase logistics
First smart tower liquid side line position.The high grade edible spirit of purity qualification is obtained from eparating methanol tower tower reactor.
Described first smart tower tower reactor discharging is first preheated through gaseous effluent cooler and waste water, then through the second smart tower feed preheater
With the second smart tower of smart tower tower reactor discharging heat exchange laggard second.
Described second smart tower and prefractionator are thermally integrated operation, using the heat of the second smart column overhead gas phase, through steam generator
With the combination unit of knockout drum, waste water is generated into secondary steam, for heat needed for providing prefractionator.Specific implementation process
Are as follows: the second smart column overhead gas phase removes prefractionator reboiler shell side, and the condensed material of logistics is into the second smart tower return tank.In the second essence
After completing gas-liquid separation in tower return tank, not solidifying gas phase removes the first smart column overhead gaseous stream pipeline, and the second smart tower return tank goes out
Oral fluid is mutually used as the second smart tower phegma into tower top.Second smart tower tower reactor discharging is after cooling useless through the second smart tower feed preheater
For water into knockout drum, waste water a part in knockout drum removes prefractionator reboiler, produces with the second smart column overhead gas phase heat exchange
Raw secondary steam is into prefractionator tower reactor, heat source needed for separating as prefractionator；Another part waste water in knockout drum is cold through waste water
But device is cooling, and logistics after cooling is divided into two strands, one goes washing column overhead as circulation wash water, and another part is arranged as waste water
Rectifier unit out.
The second smart tower tower reactor is heated using live steam, from the second smart tower middle part or lower part lateral line withdrawal function fusel oil,
Second smart tower top lateral line withdrawal function azeotropic alcohol removes eparating methanol tower tower top.
By process provided by the invention, the second smart tower can use so-called steaming with the heat exchange mode that prefractionator is thermally integrated
Vapour generator --- the combination unit of prefractionator reboiler and knockout drum generates secondary steam to prefractionator tower reactor and provides heat；
Or as shown in figure 4, heat is provided to prefractionator tower reactor using the heat exchanger of pump forced circulation.Prefractionator kettle liquid is through mash circulating pump liter
It is pressed into steam generator tube side, is returned to prefractionator tower reactor after the gas-phase heating from the second smart column overhead, provided needed for prefractionator
Heat.It is preferred that using steam generator, generating secondary steam as prefractionator heat source, solid content in prefractionator kettle material is effectively avoided
To the blocking of prefractionator tower reactor reboiler, solid content is avoided to guarantee the long-period stable operation of reboiler to the abrasion of reboiler.It steams
Water used in vapour generator, it is preferential that external offer fresh water had not both been needed using the second smart tower tower reactor waste discharge in this way, and
The alcohol in the second smart tower tower reactor waste water can be recycled.Steam generator can also generate steam using fresh water.
By process provided by the invention, water scrubber is thermally integrated mode of operation and can be with the first smart tower and eparating methanol tower
The first smart tower tower reactor reboiler heating is first given in series connection, i.e. water scrubber top gaseous phase, and remaining gas phase gives eparating methanol tower tower reactor to boil again again
Device heating；Parallel way can also be used, i.e. water scrubber top gaseous phase is divided into two strands, one gas phase is boiled again to the first smart tower tower reactor
Device heating, another burst of gas phase are heated to eparating methanol tower tower reactor reboiler.
By process provided by the invention (as shown in Figure 1), eparating methanol tower top gaseous phase is directly entered in the first smart tower
The auxiliary devices such as cooling equipment and return tank are saved to reduce investment outlay in top；Edible alcohol product is produced from eparating methanol tower tower reactor.
As shown in Fig. 2, pressing process provided by the invention, separating methanol top gaseous phase can not also return to the first smart tower, eparating methanol tower
Top sets the auxiliary devices such as rectifying section and condenser.
By process provided by the invention (as shown in Figure 3), the first smart tower and eparating methanol tower merge into a single whole, using every
Plate tower structure.Combination in Fig. 3 on the left of the first smart tower dividing plates above section and lower partition is equivalent to the first essence tower in Fig. 1；
The first smart tower lower partition right part is equivalent to the eparating methanol tower in Fig. 1 in Fig. 3.
By process provided by the invention, each tower operating pressure (unless otherwise specified, all pressure in the present invention
Referring both to absolute pressure) range is as follows:
The tower top operating pressure of prefractionator is 0.1~0.3MPa；
The tower top operating pressure of water scrubber is 0.05~0.2MPa；
The tower top operating pressure of first smart tower is 0.01~0.1MPa；
The tower top operating pressure of eparating methanol tower is 0.01~0.1MPa；
The tower top operating pressure of second smart tower is 0.3~0.9MPa.
By process provided by the invention, the second smart tower tower reactor can use direct steam heating；Or pass through reboiler
Between be connected in the second smart tower tower reactor heat be provided.If by reboiler indirect heating, heat medium can use steam or thermally conductive
Oil.
It, can be in prefractionator, water scrubber, the first smart tower, eparating methanol tower and the second smart tower by process provided by the invention
Increase a recovery tower on the basis of five towers, for handle the aldehyde wine of water scrubber overhead extraction, the second smart tower side take-off it is miscellaneous
The alcoholic material such as alcohol oil, to improve alcohol product yield.The aldehyde wine of water scrubber overhead extraction, the second smart tower side take-off
The alcoholic material such as fusel oil enters in the middle part of recovery tower, from recovery tower recovered overhead alcohol therein and returns to water scrubber；From
Recovery tower tower reactor waste discharge.Generally, the outlet of side line fusel need to be arranged in recovery tower, and fusel oil washing, phase splitting device is arranged,
For removing fusel oil.
The energy saver of production high grade edible spirit provided by the invention includes at least having prefractionator, water scrubber, the first essence
The production high grade edible spirit device noumenon of five tower of smart tower of tower, eparating methanol tower and second, and following pipeline is set by above-mentioned five tower
Link together: prefractionator top gaseous phase is connected through pipeline with the reboiler shell side inlet of water scrubber；Water scrubber top gaseous phase warp
Pipeline is connected with the reboiler shell side inlet of the first smart tower；The reboiler shell-side outlet material of first smart tower flows back into water scrubber
Tank, water scrubber return tank outlet gas phase are connected through pipeline with the reboiler shell side inlet of eparating methanol tower；Second smart column overhead gas
Mutually it is connected through pipeline with the reboiler shell side inlet of prefractionator.
By process provided by the invention, fermentation liquid enters back into prefractionator after need to preheating, the preheating method is: hair
Ferment mash and the first smart column overhead gas phase exchange heat, fermentation liquid and prefractionator tower reactor give up wine with dregs heat exchange, fermentation liquid and steam condensate or
Other high temperature fluids in second smart tower tower reactor waste discharge heat exchange or fermentation liquid and rectifier unit exchange heat, either
Any combination of above-mentioned heat exchange mode.
By process provided by the invention, only it need to be passed through primary steam in the second smart tower tower reactor, overcome traditional handicraft
Multitower uses primary steam, distills the shortcomings that energy consumption is high.By process provided by the invention, prefractionator top gaseous phase is to water scrubber
Tower reactor reboiler heating, logistics can coagulate entirely all to be entered in water scrubber with partial condensation, the lime set of logistics and not solidifying gas phase
Portion.
As shown in Figure 1, pressing process provided by the invention, the first smart tower and the second smart column overhead are respectively equipped with separating methanol
Section, removes the light components impurity such as the further methanol removal of eparating methanol tower tower top in separating methanol pars infrasegmentalis side take-off azeotropic alcohol,
The high grade edible spirit of eparating methanol tower tower reactor acquisition purity qualification.
By process provided by the invention, fusel oil is produced from the side line position near the second smart tower charging；If setting
Recovery tower, then final fusel oil is drawn from recovery tower side-stream, and rectifier unit is discharged after cooling, washing.
By process provided by the invention, the edible alcohol product can preheat to fermentation liquid or to miscellaneous
The light wine preheating that the extraction of alcohol oil returns, recycles wherein heat, reduces cooling-water consumption.
By process provided by the invention, each reboiler and heat exchanger can be shell-and-tube heat exchanger, board-like
The various heat exchangers such as heat exchanger, spiral heat exchanger, falling-film reboiler.Which kind of do not constituted pair using the heat exchanger pattern of pattern
The restriction of spirit of that invention.
The process provided by the invention that top grade ethanol refinery is carried out using multitower heat integration device, is suitable for wood
Potato, starch or saccharic or their combination are raw material, production national standard top grade savor the general grade edible alcohol of edible alcohol, national standard and
The alcohol product of various other specifications.It is volume ratio that fermentation liquid alcohol content range, which is generally 5~12%(alcohol concentration),
Process provided by the invention is applicable to the ethanol refinery process of various concentration fermentation liquids, not by above-mentioned fermentation liquid wine
The limitation of smart content range.
By process provided by the invention, it cannot be only used for production high grade edible spirit, it is superfine to can be used for production
Edible alcohol.
The present invention relates to a kind of energy-saving rectifying process for producing high grade edible spirit and devices, it is a kind of from fermentation
The energy saver and process of high grade edible spirit are produced in mash by distillation process.Entire ethanol refinery device at least wraps
Include five towers and its corollary equipment compositions such as prefractionator, water scrubber, the first smart tower, eparating methanol tower and the second smart tower.The present invention overcomes
The shortcomings that prior art, is thermally integrated using the quadruple effect of single column heat supply breakthroughly on the Process ba- sis of common multitower heating
Process, in addition other heat exchange, the application of power-saving technology significantly reduce operation energy consumption in system.It overcomes existing skill
The shortcomings that art, operation energy consumption are down to 1.7 tons of steam/ton high grade edible spirit, than the top grade ethanol refinery work being widely used at present
Process operation energy consumption reduces by 40% or more, has significant practicability and huge economic benefit, has a extensive future.
Detailed description of the invention
Fig. 1 is that a kind of energy-saving rectifying process of typical production high grade edible spirit provided by the invention and device show
It is intended to.
Fig. 2 is a kind of differentiation process schematic diagram of Fig. 1, and separating methanol top gaseous phase shown in FIG. 1 does not return to the first essence
Tower, eparating methanol tower top set the auxiliary devices such as rectifying section and condenser；Water scrubber top gaseous phase is divided into two strands, respectively to the first essence
Tower and eparating methanol tower reboiler provide institute's calorific requirement；Second smart tower provides institute's calorific requirement by the second smart tower reboiler.
Fig. 3 is that the another of Fig. 1 develops process schematic diagram, and increases recovery tower, improves alcohol product yield.Figure
First smart tower and eparating methanol tower shown in 1 merge into a single whole, using partition tower structure.In Fig. 3 more than first smart tower T103 partition
The first smart tower that the combination of T103L is equivalent in Fig. 1 on the left of part and lower partition；First smart tower T103 lower partition in Fig. 3
The part right side T103R is equivalent to the eparating methanol tower in Fig. 1.
Fig. 4 is the another embodiment schematic diagram that the second essence tower T105 and prefractionator T101 are thermally integrated, and prefractionator T101 tower reactor is adopted
Heat is provided to prefractionator T101 tower reactor with the heat exchanger of pump forced circulation.By mash circulating pump P101 by T101 tower reactor mash 59
It is sent into E104 tube side, for the gas phase 32 from T105 tower top into E104 shell side, the mash 60 after being heated returns to T101 tower reactor, above-mentioned
Process realizes heat transfer process of the T105 to T101.
Specific embodiment
Specific embodiments of the present invention be explained in detail with reference to the accompanying drawings it is as follows, but for illustrative purposes only rather than limitation the present invention.
Embodiment 1:
As shown in Figure 1, first passing through the first essence tower condenser E101 with the first essence from the maturing fermentation mash 1 that fermentation procedure comes
Tower T103 tower top fume 22 preheats, then preheats through the mash preheater E103 useless wine with dregs 6 of prefractionator T101 tower reactor, then pushes up into T101
Portion.
Prefractionator T101 and water scrubber T102 are thermally integrated operation, and T101 tower top fume 5 is into water scrubber T102 tower reactor reboiler
E105 shell side, the condensed material 8 of fume 5 is into light wine tank V102.After completing gas-liquid separation in V102, gas phase 9 and liquid phase 10
Respectively into T102 tower middle part.
The essence of water scrubber T102 and first tower T103 and eparating methanol tower T104 is thermally integrated operation, and T102 tower top fume 12 is advanced
T103 tower reactor reboiler E106 shell side, the condensed material 13 of fume 12 is into water scrubber return tank V103.Gas is completed in V103
After liquid separation, gaseous stream 14 is again into T104 reboiler E107 shell side.After 14 condensate of logistics, 15 gas-liquid separation, gas phase 16 removes water
Wash tower tail cooler E108, liquid phase is into V103.The outlet E108 fixed gas 17 removes exhaust treatment system, and it is two strands that E108 lime set 45, which is divided to,
One is 47 as producing into aldehyde wine 18, and another part 46 is into V103.It is two strands that the outlet V103 liquid phase 48, which is divided to, a part 19 and circulation
Together as T102 phegma into T102 tower top, another part is produced into aldehyde wine 18 wash water 11.T103 is removed in T102 tower reactor discharging 21
Lower part.
E106 outlet streams 13 can not also advanced V103, but gas-liquid mixed phase, together into E107.Gas is completed in E107
Liquid separation.
T103 top gaseous phase 22 first exchanges heat through E101 and fermentation liquid 1, and not solidifying gas phase 23 is again through the first smart tower tail cooler
E102 condensation, fixed gas 24 go vacuum system, and E101, E102 lime set are into the first smart tower return tank V104.The wherein part of E102
Lime set is as 25 discharger of industrial alcohol.V104 exports liquid phase as the first smart tower phegma into T103 tower top.
The top T103 side line Extract phase logistics 27 returns to T103 liquid phase side line position into the top T104, T104 top gaseous phase 43
It sets.The high grade edible spirit 44 of purity qualification is obtained from T104 tower reactor.
T103 tower reactor discharging 28 is first preheated through gaseous effluent cooler E109 and waste water 40, then through the second smart tower feed preheater
The smart 38 laggard T105 of heat exchange of tower tower reactor discharging of E110 and second.
Second essence tower T105 and prefractionator T101 are thermally integrated operation, using the heat of T105 top gaseous phase 32, through steam generation
Waste water 39 is generated secondary steam 4, for heat needed for providing T101 by device (combination unit of E104 and V101).It is specific real
Apply process are as follows: T105 top gaseous phase 32 removes T101 reboiler E104 shell side, and the condensed material 33 of logistics 32 is returned into the second smart tower
Flow tank V105.After completing gas-liquid separation in V105, not solidifying gas phase 34 goes T103 top gaseous phase logistic pipeline, and V105 exports liquid phase
35 are used as the second smart tower phegma into T105 tower top.Second smart tower tower reactor discharging 38 divides through E110 39 air inlet liquid of waste water after cooling
From tank V101, waste water a part in V101 removes E104, exchanges heat with T105 top gaseous phase 32 and generates secondary steam 4 into T101 tower
Kettle, heat source needed for being separated as T101；Another part waste water 40 in V101 is cooling through E109.The logistics 41 after cooling of logistics 40
It is divided into two strands, one removes T102 tower top as circulation wash water 11, and rectifier unit is discharged as waste water 42 in another part.
Second smart tower T105 tower reactor is heated using live steam 31, from the middle part T105 or lower part lateral line withdrawal function fusel oil 37,
The top T105 lateral line withdrawal function azeotropic alcohol 36 removes T104 tower top.
Following present a kind of typical operation conditions of each tower in embodiment 1:
Prefractionator T101 tower top operating pressure 0.16MPa, tower top operation temperature are 105 DEG C, 117 DEG C of tower reactor operation temperature；
Water scrubber T102 tower top operating pressure 0.11MPa, 90 DEG C of tower top operation temperature, 93 DEG C of tower reactor operation temperature；
First essence tower T103 tower top operating pressure 0.035MPa, 53 DEG C of tower top operation temperature, 70 DEG C of tower reactor operation temperature；
Eparating methanol tower T104 tower top operating pressure 0.036MPa, 54 DEG C of tower top operation temperature, 56 DEG C of tower reactor operation temperature；
Second essence tower T105 tower top operating pressure 0.56MPa, 128 DEG C of tower top operation temperature, 157 DEG C of tower reactor operation temperature.
Relative to Chinese patent CN 201510850323.4 provide " for producing double smart tower quadruple effect top grades of alcohol
Alcohol distillation method and apparatus ", process provided by the invention is using the first smart tower and eparating methanol tower as the 4th effect, the first essence
Tower and two tower kettle material of eparating methanol tower are all the mixtures of second alcohol and water, and under the conditions of uniform pressure, vapourizing temperature is lower than pure
The boiling point of water, therefore process provided by the invention can significantly reduce the overall pressure differential that quadruple effect is thermally integrated, the 1st effect i.e. the second essence
The typical operating pressure of tower is only 0.56MPa, well below needed for the effect of Chinese patent CN 201510850323.4 the 1st
1.0MPa, operational safety greatly improve.Also, product is arranged process provided by the invention imitates eparating methanol tower the 4th
Tower reactor extraction, i.e., obtain alcohol product under the conditions of vacuumizing, it is well known that the alcohol distillation operating pressure the low more is conducive to
The removal of other impurities, therefore process provided by the invention is more advantageous to and obtains high-quality high grade edible spirit.
Using the energy-saving rectifying process and device of the production high grade edible spirit that the embodiment of the present invention 1 provides, production
Edible alcohol quality it is as shown in the table:
As can be seen from the above table, it for indexs such as very important methanol, oxidization times in edible alcohol industry, uses
Process provided by the invention is better than documents, and operation energy consumption is greatly reduced.
Embodiment 2:
As shown in Fig. 2, it is a kind of differentiation process of Fig. 1, process difference relatively shown in FIG. 1 is such as
Under:
It is two strands that water scrubber top gaseous phase 12, which is divided to, one gas phase 54 is to T103 tower reactor reboiler E106 heating, another strand of gas
Phase 55 is heated to T104 tower reactor reboiler E107.
Separating methanol top gaseous phase shown in FIG. 1 does not return to the first smart tower, sets rectifying section and condenser etc. at the top of eparating methanol tower
Auxiliary device.T104 top gaseous phase 49 is first condensed through eparating methanol tower condenser E111, and not solidifying gas phase 50 is cold through eparating methanol tower tail again
Device E112 condensation, fixed gas 51 go vacuum system, and E111, E112 lime set are into eparating methanol tower return tank V106.The wherein portion of E112
Liquid is segregated as 52 discharger of industrial alcohol.V106 exports liquid phase as eparating methanol tower phegma into T104 tower top.The side T105
Line azeotropic alcohol 36 is into the middle part of T104.T105 tower reactor provides heat by being connected in T105 tower reactor between the second smart tower reboiler E113.
Embodiment 3:
As shown in figure 3, it is that the another of Fig. 1 develops, process difference relatively shown in FIG. 1 is as follows:
First smart tower and eparating methanol tower merge into a single whole, using partition tower structure.T103 partition above section is under in Fig. 3
The first smart tower that the combination of T103L is equivalent in Fig. 1 on the left of portion's partition；The part T103R is suitable on the right side of T103 lower partition in Fig. 3
Eparating methanol tower in Fig. 1.Differentiation process shown in Fig. 3, number of devices is few, small accommodation area, and process flow is more simplified.
The present invention can choose in prefractionator T101, water scrubber T102, the first smart tower T103, the essence of eparating methanol tower T104 and second
Increase a recovery tower T106 on the basis of five tower of tower T105.Aldehyde wine 18 from water scrubber T102 tower top and from the second smart tower
The alcoholic material such as the fusel oil 37 of T105 side take-off, into the middle part T106, T106 recovered overhead alcohol 56 removes water scrubber
Middle part, T106 tower reactor waste discharge 57.Fusel oil side line after recovery tower charging neighbouring position extraction concentration, through cooling, water
After washing, rectifier unit is discharged in fusel oil 59.
It is using the energy-saving rectifying process and device, steam consumption quantity of production high grade edible spirit provided by the invention
1.7 tons of steam/ton top grade savors edible alcohol product.
The present invention and the top grade ethanol refinery technique being widely used at present have carried out operation energy consumption comparison, compare energy-saving effect
It is as follows:
The conventional multitower heating alcohol rectification process being widely used at present, produces azeotropic alcohol steam consumption about 3.0~4.2
Ton steam/ton top grade alcohol product:
(3.0-1.7)/3.0 × 100% ≈ 43%
The energy-saving rectifying process and device of production high grade edible spirit provided by the invention, than what is be widely used at present
Conventional multitower heats 40% or more alcohol rectification process energy conservation.
CN 200510035598.9 provides the process of quinque-towel differential pressure distilling arrangement production high grade edible spirit, raw
Production high grade edible spirit steam consumption quantity is 2.3 tons of steam/ton azeotropic alcohol product.
Using the energy-saving rectifying process and device and CN of production high grade edible spirit provided by the invention
200510035598.9 provided process operation energy consumption comparison is as follows:
(alcohol output is 25 ton/hours, and year operation hour is pressed 8000 hours) is calculated by 200,000 tons/year of alcohol devices, it can
Save 0.6 ton of steam of steam/ton azeotropic alcohol product (2.3-1.7=0.6):
0.6/2.3×100% ≈26%。
The energy-saving rectifying process and device of production high grade edible spirit provided by the invention, compare CN
200510035598.9 provided process saving energy 26%.About 120,000 tons of (0.6 ton/ton × 200,000 of steam can be saved every year
Ton/year=120,000 tons/year).
It is calculated by 150 yuan of steam per ton, can save steam expense every year: 120,000 tons/year × 150 yuan/ton=18,000,000
Member/year.
The energy-saving rectifying process and device of production high grade edible spirit provided by the invention have extremely significant economical
Benefit.It is illustrated in conjunction with the embodiments, the method that the personnel of related fields can provide according to the present invention completely is fitted
When change or changes and combinations, to realize the technology.It should be strongly noted that all these by work provided by the invention
Skill process carries out similar change or change and reconfigures, apparent to those skilled in the art, all by
It is considered as in spirit of the invention, range and content.
Claims (10)
1. a kind of energy-saving rectifying process for producing high grade edible spirit, it is to be produced from fermentation liquid by distillation process
High grade edible spirit, it is characterised in that:
1) prefractionator (T101), water scrubber (T102), the first smart tower (T103), eparating methanol tower (T104) and the second smart tower are included at least
(T105) five tower；
2) rectifier unit institute calorific requirement is all added by the second smart tower (T105) tower reactor；
3) the second smart tower (T105) and prefractionator (T101) are thermally integrated operation, and prefractionator (T101) tower reactor institute's calorific requirement is by the second smart tower
(T105) top gaseous phase provides；
4) prefractionator (T101) and water scrubber (T102) are thermally integrated operation, and water scrubber (T102) tower reactor institute calorific requirement is by prefractionator
(T101) top gaseous phase provides；
5) water scrubber (T102) is thermally integrated operation, water scrubber (T102) tower top with the first smart tower (T103) and eparating methanol tower (T104)
Gas phase is respectively that the first smart tower (T103) and eparating methanol tower (T104) tower reactor provide institute's calorific requirement；
Described second smart tower (T105) is the first effect, and prefractionator (T101) is the second effect, and water scrubber (T102) is third effect, the first essence
Tower (T103) and eparating methanol tower (T104) are quadruple effect, and above-mentioned five tower constitutes a kind of quadruple effect and is thermally integrated process.
2. process described in accordance with the claim 1, it is characterised in that: the maturing fermentation mash (1) come from fermentation procedure is first
It is preheated by the first smart tower condenser (E101) with the first smart tower (T103) tower top fume (22), then through mash preheater (E103)
It is preheated with prefractionator (T101) tower reactor useless wine with dregs (6), then into prefractionator (T101) top；
The prefractionator (T101) and water scrubber (T102) are thermally integrated operation, and prefractionator (T101) tower top fume (5) is into water scrubber
(T102) tower reactor reboiler (E105) shell side, fume (5) condensed material (8) is into light wine tank (V102), in light wine tank
(V102) after completing gas-liquid separation in, gas phase (9) and liquid phase (10) are respectively into water scrubber (T102) tower middle part；
The water scrubber (T102) is thermally integrated operation, water scrubber (T102) tower with the first smart tower (T103) and eparating methanol tower (T104)
Push up fume (12) advanced first smart tower (T103) tower reactor reboiler (E106) shell side, fume (12) condensed material (13) water inlet
Tower (T102) return tank (V103) is washed, after completing gas-liquid separation in return tank (V103), gaseous stream (14) is again into separating methanol
Tower (T104) reboiler (E107) shell side, after logistics (14) condensate (15) gas-liquid separation, gas phase (16) removes water scrubber (T102)
Tail cooler (E108), liquid phase remove exhaust treatment system into return tank (V103), tail cooler (E108) outlet fixed gas (17), and tail is cold
Device (E108) lime set (45) is divided into two strands, one (47) as producing into aldehyde wine (18), another part (46) is into return tank
(V103)；Return tank (V103) outlet liquid phase (48) is divided into two strands, and a part is 19) with circulation wash water (11) together as water scrubber
(T102) into water scrubber (T102) tower top, another part is produced into aldehyde wine (18) phegma；The discharging of water scrubber (T102) tower reactor
(21) first smart lower part tower (T103) is gone to；
Described first smart tower (T103) top gaseous phase (22) first exchanges heat through the first smart tower condenser (E101) and fermentation liquid (1),
Not solidifying gas phase (23) are condensed through the first smart tower tail cooler (E102) again, and fixed gas (24) removes vacuum system, the first smart tower condenser
(E101), the first smart tower tail cooler (E102) lime set is into the first smart tower return tank (V104), wherein the first smart tower tail cooler
(E102) part lime set is as industrial alcohol (25) discharger；First smart tower return tank (V104) exports liquid phase as first
Smart tower (T103) phegma is into first smart tower (T103) tower top；
First smart tower (T103) the top side line Extract phase logistics (27) is at the top of eparating methanol tower (T104), eparating methanol tower
(T104) top gaseous phase (43) returns to first smart tower (T103) liquid side line position；Purity is obtained from eparating methanol tower (T104) tower reactor
Qualified high grade edible spirit (44)；
First smart tower (T103) the tower reactor discharging (28) first preheats through gaseous effluent cooler (E109) and waste water (40), then through the
Two smart tower feed preheaters (E110) and the second smart tower (T105) of smart tower (T105) tower reactor discharging (38) heat exchange laggard second；
Described second smart tower (T105) and prefractionator (T101) are thermally integrated operation, utilize the second smart tower (T105) top gaseous phase (32)
Waste water (39) are generated secondary steam by heat, the combination unit through steam generator (E104) Yu knockout drum (V101)
(4), for heat needed for providing prefractionator (T101), specific implementation process are as follows: the second smart tower (T105) top gaseous phase (32) is gone
Prefractionator (T101) reboiler (E104) shell side, logistics (32) condensed material (33) is into second smart tower (T105) return tank
(V105), after completing gas-liquid separation in return tank (V105), not solidifying gas phase (34) remove first smart tower (T103) top gaseous phase object
Flow tube line, return tank (V105) export liquid phase (35) and are used as the second smart tower (T105) phegma into second smart tower (T105) tower top；
Second smart tower (T105) tower reactor discharging (38) is through the second smart tower feed preheater (E110) waste water after cooling (39) air inlet liquid point
From tank (V101), waste water a part in knockout drum (V101) removes reboiler (E104), with second smart tower (T105) tower top
Gas phase (32) heat exchange generates secondary steam (4) into prefractionator (T101) tower reactor, heat source needed for separating as prefractionator (T101)；Gas-liquid point
It is cooling through gaseous effluent cooler (E109) from another part waste water (40) in tank (V101)；Logistics (40) logistics after cooling (41)
It is divided into two strands, one removes water scrubber (T102) tower top as circulation wash water (11), and rectifying is discharged as waste water (42) in another part
Device；
Described second smart tower (T105) tower reactor is heated using live steam (31), from the second smart tower (T105) middle part or lower part side line
It extracts out fusel oil (37), the second smart tower (T105) top lateral line withdrawal function azeotropic alcohol (36) removes eparating methanol tower (T104) tower top.
3. process described in accordance with the claim 1, it is characterised in that: the second smart tower (T105) is thermally integrated with prefractionator (T101)
Heat exchange mode provide heat to prefractionator (T101) tower reactor using the secondary steam (4) that the steam generator generates；Or
Heat is provided to prefractionator (T101) tower reactor using the heat exchanger of pump forced circulation.
4. process described in accordance with the claim 1, it is characterised in that: water scrubber (T102) and the first smart tower (T103) and take off
Methanol column (T104), which is thermally integrated mode of operation, can be series connection, i.e. water scrubber (T102) top gaseous phase first gives the first smart tower (T103)
Tower reactor reboiler (E106) heating, remaining gas phase give eparating methanol tower (T104) tower reactor reboiler (E107) to heat again；Or using simultaneously
Connection mode, i.e. water scrubber (T102) top gaseous phase is divided into two strands, one gas phase is to first smart tower (T103) tower reactor reboiler
(E106) it heats, another burst of gas phase is heated to eparating methanol tower (T104) tower reactor reboiler (E107).
5. process described in accordance with the claim 1, it is characterised in that: eparating methanol tower (T104) top gas does not return to the first essence mutually
Tower, eparating methanol tower (T104) top set rectifying section and condenser auxiliary device.
6. process described in accordance with the claim 1, it is characterised in that: the first smart tower (T103) and eparating methanol tower (T104) close
And be integrated, using partition tower structure, partition side is the first smart tower (T103), the partition other side is eparating methanol tower (T104).
7. process described in accordance with the claim 1, it is characterised in that each tower operating pressure range is as follows:
The tower top operating pressure of prefractionator (T101) is 0.1~0.3MPa；
The tower top operating pressure of water scrubber (T102) is 0.05~0.2MPa；
The tower top operating pressure of first smart tower (T103) is 0.01~0.1MPa；
The tower top operating pressure of eparating methanol tower (T104) is 0.01~0.1MPa；
The tower top operating pressure of second smart tower (T105) is 0.3~0.9MPa.
8. process described in accordance with the claim 1, it is characterised in that: second smart tower (T105) tower reactor is added using direct steam
Heat, or heat is provided by being connected in the second smart tower (T105) tower reactor between the second smart tower reboiler (E113).
9. process according to claim 1 or 2, it is characterised in that: in prefractionator (T101), water scrubber (T102),
Increase a recovery tower (T106) on the basis of one smart tower (T103), eparating methanol tower (T104) and second smart tower (T105) five tower,
For handling the fusel oil (37) of the aldehyde wine (18) of water scrubber (T102) overhead extraction, second smart tower (T105) side take-off containing wine
The material of essence, to improve alcohol product yield.
10. the device that the energy-saving process method of any production high grade edible spirit of claim 1-8 uses, feature exist
In at least with prefractionator (T101), water scrubber (T102), the first smart tower (T103), eparating methanol tower (T104) and the second smart tower
(T105) the production high grade edible spirit device noumenon of five towers, and following pipeline is set, above-mentioned five tower links together: prefractionator
(T101) top gaseous phase is connected through pipeline with reboiler (E105) shell side inlet of water scrubber (T102)；Water scrubber (T102) tower
Top gas is mutually connected through pipeline with reboiler (E106) shell side inlet of the first smart tower (T103)；First smart tower (T103's) boils again
Device (E106) shell-side outlet material exports gas phase through pipeline and eparating methanol tower into water scrubber return tank (V103), return tank V103
(T104) reboiler (E107) shell side inlet is connected；Second smart tower (T105) top gaseous phase is through pipeline and prefractionator (T101)
Reboiler (E104) shell side inlet is connected.
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| CN107954837A (en) * | 2017-11-22 | 2018-04-24 | 广东中科天元新能源科技有限公司 | Produce neutral alcohol, the device and its production technology of superneutrality alcohol |
| CN109939456A (en) * | 2019-04-08 | 2019-06-28 | 宁波中科远东催化工程技术有限公司 | A kind of distillation system and method for coal-ethylene glycol |
| CN111072454B (en) * | 2020-01-19 | 2024-02-27 | 肥城金塔机械科技有限公司 | System and process for producing fuel ethanol by double-coarse and double-fine distillation with low pressure method |
| CN113680088B (en) * | 2020-05-18 | 2023-06-02 | 北京诺维新材科技有限公司 | Multi-effect rectifying method, rectifying device and application thereof |
| CN114480067A (en) * | 2022-01-14 | 2022-05-13 | 肥城金塔机械科技有限公司 | Device for reducing methanol in kiwi fruit wine and preparation method |
| CN115057760A (en) * | 2022-06-08 | 2022-09-16 | 天津市新天进科技开发有限公司 | Process method and device for producing fuel ethanol and high-grade edible alcohol by adopting five-tower heat integration |
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| CN104151135A (en) * | 2014-07-24 | 2014-11-19 | 广东中科天元新能源科技有限公司 | Molassess raw material top-grade alcohol distillation and waste liquid concentration thermal coupling device and process |
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| CN104151135A (en) * | 2014-07-24 | 2014-11-19 | 广东中科天元新能源科技有限公司 | Molassess raw material top-grade alcohol distillation and waste liquid concentration thermal coupling device and process |
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