CN102174371B - Process method and device for coupling acetone-butyl alcohol fermentation and separation - Google Patents

Process method and device for coupling acetone-butyl alcohol fermentation and separation Download PDF

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CN102174371B
CN102174371B CN2011100390367A CN201110039036A CN102174371B CN 102174371 B CN102174371 B CN 102174371B CN 2011100390367 A CN2011100390367 A CN 2011100390367A CN 201110039036 A CN201110039036 A CN 201110039036A CN 102174371 B CN102174371 B CN 102174371B
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acetone
extraction
extraction tower
extraction agent
well heater
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CN102174371A (en
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金付强
胡素琴
王波
许海朋
张�杰
王建梅
杨改
蔡飞鹏
张晓东
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Energy Research Institute of Shandong Academy of Sciences
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Abstract

The invention discloses a device for coupling acetone-butyl alcohol fermentation and separation. The device consists of a fermentation tank, an extraction tower, a heater and a condenser, wherein the extraction tower is arranged at the upper part of the fermentation tank and is communicated with the fermentation tank; the heater is arranged at the upper part of the extraction tower; and the condenser is communicated with the top part of the extraction tower. Acetone-butyl alcohol fermentation liquor in a conventional fermentation tank is added into the fermentation tank of the coupling device or is directly used for performing acetone-butyl alcohol fermentation in the fermentation tank of the coupling device; an extracting agent with a high boiling point is filled in the extraction tower; the acetone, the butyl alcohol and the ethanol generated through the fermentation are extracted into the extracting agent, and move upwards under the driving of the concentration difference and density difference between the generated acetone, butyl alcohol and ethanol and the extracting agent; and the heater is used for heating the extracting agent at the inner upper part of the extraction tower so that the acetone, the butyl alcohol and the ethanol dissolved in the extracting agent are distilled out continuously. According to the method provided by the invention, not only can the product inhibition of the acetone-butyl alcohol fermentation be effectively eliminated, the product yield and the raw material utilization ratio of the acetone-butyl alcohol fermentation be improved, but also the production energy consumption and cost can be effectively reduced.

Description

Acetone separates coupled process method and device
Technical field
The present invention relates to a kind of acetone and separate the coupled process method, particularly fermentation and a kind of fermentation separation coupling method of extractive distillation stripping technique coupled.
Background technology
Acetone and butanols are important chemical material, industrial solvent and fuel, can be by chemical synthesis and fermentative Production.Production of acetone and butanol fermentation is starch, pulp waste, molasses and wild plants as raw materials, since the fermentation process is subject to severe product inhibition, so that the reaction after the fermentation broth contains only about 1.8% (mass fraction) ethanol, acetone and n-butanol (product known as ABE), the rest is fermented solids and water [Chen Tao-sound.? fermentation of acetone and butanol production technology [M].? Beijing:? chemical Industry Press,? 1991].Traditional method of purification is to make fermented liquid at first put forward dense fermentation solid thing and the portion water removed through the roughing out column distillation, is contained the material of ethanol 4%, acetone 10%, propyl carbinol 26% and water 60% approximately, and the energy consumption of this process is very big.
At present, document (Steven Roffler, Harvey W. Blanch; Charles R. Wilke. Extractive Fermentation of Acetone and Butanol:Process Design and Economic Evaluation [J]. Biotechnology Progress, 1987,3 (3): 131 – 140.) in relevant for the report that adopts liquid-liquid extraction to combine with acetone; This method can effectively be eliminated the restraining effect of product; Improved productive rate and raw material availability, very big progress has been arranged, but the method for separate fermentation product is to adopt traditional distillating method after extraction than traditional zymotic method; The extraction liquid that is about to contain tunning joins in the still kettle; Obtain containing the material of ethanol, acetone, propyl carbinol and water and reclaiming extraction agent through still kettle being heated distill, this method need be heated to high temperature with employed whole extraction agents, also need extraction agent be cooled off afterwards; Complex equipments, energy expenditure is big.
Summary of the invention
The purpose of this invention is to provide a kind of acetone and separate coupling process method and device, it has overcome the high shortcoming of tunning separating energy consumption in the existing extractive fermentation coupling process.
The technical scheme that the present invention adopted is: a kind of acetone separation coupling device; It by fermentor tank, be arranged on fermentor tank top and the extraction tower that connects with it, be installed on the well heater on extraction tower top and the condensing surface that is communicated with the extraction tower top is formed; Can in this device, realize fermentation simultaneously, extract and distill three processes; Wherein the extraction tower outer wall is provided with opening for feed; Be provided with feed valve before the opening for feed, extraction tower bottom outer wall is provided with discharge port, is provided with bleeder valve behind the discharge port; The fermentor tank outer wall is provided with opening for feed, is provided with feed valve before the opening for feed, and the fermentor tank bottom is provided with discharge port, and the discharge port bottom is provided with bleeder valve.
The height H of said extraction tower tBe 0.4～20 m, preferred 1.5～15 m.
The height H of said well heater hBe 0.05～5 m, and H h=0.01 H t～0.3 H tThe distance H of the upper limb of well heater and extraction tower cat head pBe 0.05～5 m, and H p=0.01 H t～0.4 H t, and liquid boiling carries out with vaporization is overflowed smoothly can guarantee to distill the time, and the liquid spittle is not taken out of by steam.
The said well heater that is installed on extraction tower top can be the electrically heated cover, is installed on the extraction tower external wall of upper portion.
The foregoing coupling device of a kind of use is accomplished acetone and is separated the coupled process method, and it may further comprise the steps:
(a) in conventional fermentor tank, carry out acetone, afterwards fermented liquid is joined in the fermentor tank of foregoing coupling device, perhaps directly in the fermentor tank of foregoing coupling device, carry out acetone;
(b) high boiling extraction agent is housed in extraction tower;
(c) acetone, butanols and the ethanol of fermentation generation are extracted in the extraction agent, and upwards migration;
(d) well heater through being installed on extraction tower top heats the extraction agent of extraction tower internal upper part, and the acetone, butanols and the ethanol that are dissolved in the extraction agent are constantly distilled away, after condenser condenses, collects to such an extent that contain acetone, butanols and alcoholic acid solution.
The liquid level that in extraction tower, adds extraction agent is higher than the well heater lower edge that is installed on extraction tower top, and with distance=0.8 H of this well heater edge h～1.2 H hWhat liquid boiling and vaporization were overflowed when the distance of extraction agent liquid level and extraction tower cat head can guarantee to distill carries out smoothly, and the liquid spittle is not taken out of by steam.
The characteristic of this process method is the density of the density of extraction agent less than acetone liquid, and greater than the density of butanols, preferred 0.83～0.97 kg/m 3So that make extraction agent can be in the top of acetone liquid, and the concentration difference between tunning acetone, butanols and ethanol and the extraction agent and density difference can be used as acetone, butanols and ethanol motive for migration source upwards in extraction agent.
The characteristic of this process method is that the boiling point of extraction agent is 140～800 ℃.
The characteristic of this process method is that extraction agent can be selected from one or both or the two or more mixtures in OE, oleic acid, Unimac 5680, triricinoleiden, methyl ricinoleate, ethyl ricinoleate, butyl butyrate, certain herbaceous plants with big flowers two dibutyl phthalates, certain herbaceous plants with big flowers diacid di-isooctyl, sym-trimethylbenzene, decyl alcohol, lauryl alcohol, tetradecyl alcohol, oleyl alcohol, the isooctadecanol.
In the existing acetone extraction coupling technique, the method for separate fermentation product is to adopt traditional distillating method after extraction, needs employed whole extraction agents are heated to high temperature, also need extraction agent be cooled off afterwards, and complex equipments, energy expenditure is big.
With respect to existing acetone extraction coupling technique; The invention has the beneficial effects as follows: the characteristic of this process method is in a device, to realize acetone, product extraction and distill three processes; Wherein fermenting process and still-process can carry out continuously; Also may be carried out batchwise; Though and fermentation is to carry out at a lower temperature, distillation is under comparatively high temps, to carry out, because the heater heats distillatory heat that is installed on extraction tower top makes the degree of fermented liquid temperature rising can not influence carrying out smoothly of device bottom acetone process.
1. energy-conservation.Adopt the fermentation-extraction-water distilling apparatus among the present invention to carry out acetone, product extraction and distill three processes; Heating unit during distillation is installed on extraction tower top; Only need few part extraction agent is heated; And need whole extraction agents be heated to high temperature, the extraction agent process of cooling after also having avoided can effectively reduce energy expenditure.
2. device is simplified.Fermentation-extraction-still-process among the present invention can be accomplished in a device, and does not need the extraction agent cooling apparatus.
Description of drawings
Below in conjunction with accompanying drawing the present invention is done further explanation.Fig. 1 is fermentation of the present invention-extraction-water distilling apparatus and schematic flow sheet.Among Fig. 1, the 101-condensing surface; 102,109-well heater; The 103-extraction tower; 104,106-feed valve; 105,107-opening for feed; The 108-fermentor tank; 110,112-discharge port; 111,113-bleeder valve; W 101The water inlet of-water of condensation; W 102The water outlet of-water of condensation; D 101-distillation condensed product; F i-liquid liquid interface; F s-liquid level of solution; H t-extraction tower height; H hThe height of-well heater 102; H pThe distance of the upper limb of-well heater 102 and extraction tower cat head; H vThe distance of-extraction agent liquid level and extraction tower cat head; H eThe height of-extraction agent.
Fig. 2 is fermentation of the present invention-extraction-water distilling apparatus and schematic flow sheet; Be with the difference of device shown in Figure 1: the extraction tower 103 among Fig. 1 is made up of a cylinder; And the extraction tower 103 among Fig. 2 is made up of a truncated cone-shaped tube and a cylinder that connects with it, and wherein the height of truncated cone-shaped tube is H c
Fig. 3 is the liquid-liquid extraction of prior art and device and the schematic flow sheet that acetone is coupled.Among Fig. 3,301,310,317,322,324, the 332-pump; 302,305,325-feed valve; 303,304,311,314,319,326-opening for feed; The 306-fermentor tank; 307,328-well heater; 308,312,315,320,329-discharge port; 309,316,321,330-bleeder valve; The 313-extractor; 318-extraction agent storage tank; The 323-condensing surface; The 327-still kettle; The 331-water cooler; W 301The water inlet of-water of condensation; W 302The water outlet of-water of condensation; W 303The water inlet of-water coolant; W 304The water outlet of-water coolant; D 301-distillation condensed product.
Embodiment
In following embodiment, used clostridium acetobutylicum (Clostridium acetobutylicum) Chinese common micro-organisms culture presevation administrative center (1.244) provides.
Corn mash culture medium preparation method and actication of culture method and the equal reference literature (Yang Ying of method for preserving that activation, preservation bacterial classification and fermentation are adopted; Zhang Longyun, Shi Zhongping. add tensio-active agent and improve butanols extractive fermentation performance [J]. biological processing, 2008; 6 (4): 25-30); That is: gelatinization 60 min after activation, preservation bacterial classification and fermentation all adopt corn mash substratum, commercially available Semen Maydis 40 orders to sieve are cooled to room temperature.The corn mash massfraction that actication of culture and preservation are used is 5%, the pH nature; It is 6%～7% that the corn mash massfraction is used in fermentation, and pH transfers to 9.0,121 ℃ of sterilization 60 min.
The content of butanols, ethanol, acetone adopts the gc internal mark method determination in the gained cut, adopts GC112A type gas chromatograph (being furnished with hydrogen flame detector), and Shanghai Precision Scientific Apparatus Co., Ltd produces.Use N2000 type chromatographic working station (Zhejiang University's intelligence reaches information ltd) analytical data, chromatographic column is ALPHA-Col type PEG (polyoxyethylene glycol) capillary column (Australian SGE Int'l Pty. Ltd.).Nitrogen be carrier gas (14 milliliters/min), hydrogen and air are respectively 38 milliliters/min and 252 milliliters/min.Adopt three rank programmed temperature methods (40 ℃, 1.0 min → 3 ℃/min of temperature rise rate, warm 70 ℃ eventually, 1.0 min → 5 ℃/min of temperature rise rate, warm 140 ℃ eventually, 1.0 min → 15 ℃/min of temperature rise rate, 200 ℃ of whole temperature, 15 min) to carry out assay determination.The sampler temperature is 220 ℃, and the monitor temperature is 220 ℃.Use internal mark method determination, internal standard substance is an isopropylcarbinol, and sample size is 0.1 microlitre.Water-content in the cut calculates by [100% (butanol content+ethanol content+acetone content)].
Embodiment 1
Fermentation-extraction-water distilling apparatus: specific operation process is: at first in conventional fermentor tank, carry out acetone; Afterwards fermented liquid is joined in the fermentor tank 108 through opening for feed 107, perhaps directly fermentation raw material is joined through opening for feed 107 and carry out acetone in the fermentor tank 108; In extraction tower 103, add high boiling extraction agent through opening for feed 105; Acetone, butanols and ethanol that fermentation produces are extracted in the extraction agent, and upwards migration; The low-temperature receiver of open cold condenser 101, the extraction agent of 102 pairs of extraction tower internal upper parts of heater heats, and the acetone, butanols and the ethanol that are dissolved in the extraction agent are constantly vaporized, and after condensing surface 101 condensations, collect.Fermented liquid after fermentation-extraction-distillation is accomplished can be discharged by discharge port 110; Can discharge by discharge port 212 when extraction agent need be changed, add new extraction agent through opening for feed 105.
Device shown in the accompanying drawing 1; By fermentor tank 108, be arranged on fermentor tank 108 tops and the extraction tower 103 that connects with it, be installed on the well heater 102 on extraction tower 103 tops and the condensing surface 101 that is communicated with the extraction tower top is formed, and well heater 109, feed valve 104,106; Opening for feed 105,107; Discharge port 110,112, bleeder valve 111,113, water of condensation water inlet W 101, water of condensation water outlet W 102, distillation condensed product D 101Fermentor tank 108 volumes are 5 liters, inner barrel diameter 0.15 m; Extraction tower 103 height H tBe 1.4 m, tower internal diameter 0.15 m; Well heater 102 is the electrically heated cover, is positioned on extraction tower 103 external wall of upper portion chuck height H hBe 0.25 m, its power is 1.5 kilowatts, the distance H of its upper limb and extraction tower cat head pBe 0.3 m.
Fermentation-extraction-still-process: adopt the said device of present embodiment; Inoculum size by 5% inserts activatory bacterium liquid in 7% corn mash substratum; TV is 5 liters; Join in the fermentor tank 108 through opening for feed 107, in extraction tower 103, add OE through opening for feed 105 then and exceed well heater 102 lower edges 0.25 m, the height H of extraction agent as extraction agent to extraction agent liquid level eBe 1.2 m, the distance H of extraction agent liquid level and extraction tower cat head vBe 0.3 m; Leave standstill under 37 ℃ and cultivated 72 hours, acetone, butanols and ethanol that fermentation produces are extracted in the extraction agent, and upwards migration; The water of condensation of open cold condenser 101; The extraction agent temperature that the extraction agent of 102 pairs of extraction tower internal upper parts of heater heats and pass through to regulate heater voltage control extraction tower internal upper part is at 120～130 ℃; Working pressure is a normal atmosphere; The acetone, butanols and the ethanol that are dissolved in the extraction agent are constantly vaporized, and after condensing surface 101 condensations, collect, and replenish in extraction tower 103 through opening for feed 105 simultaneously to add OE (extraction agent) to keep the distance H of extraction agent liquid level and extraction tower cat head vBe 0.3 m; Pick up counting when having cut to distillate, close the heating of well heater 102 after 4 hours, close the water of condensation of condensing surface 101 again after 2.0 hours.Obtain cut 0.212 kg; Butanol content is 31.2% (mass percent), and acetone content is 11.3% (mass percent), and ethanol content is 3.90% (mass percent); Water-content is 53.6% (mass percent), and well heater 102 stops to heat 1.40 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 1.40/0.212=6.60 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 3.06 kilowatt-hours/kg of 9.66 kilowatt-hours/kg); And the butanols in the present embodiment gained cut, acetone and alcoholic acid total content are not less than butanols, acetone and alcoholic acid total content in embodiment 20 (Comparative Examples) the gained cut.
Present embodiment lacks than the equipment that embodiment 20 (Comparative Examples) needs, and does not need the extraction agent cooling apparatus, and embodiment 20 (Comparative Examples) need be provided with extraction agent equipment (water cooler 331).
Embodiment 2
Fermentation-extraction-water distilling apparatus: the device shown in the accompanying drawing 1, wherein fermentor tank 108 volumes are 0.8 liter, inner barrel diameter 0.08 m; Extraction tower 103 height H tBe 0.4 m, tower internal diameter 0.08 m; Well heater 102 is the electrically heated cover, is positioned on extraction tower 103 external wall of upper portion chuck height H hBe 0.05 m, its power is 0.8 kilowatt, the distance H of its upper limb and extraction tower cat head pBe 0.05 m.
Fermentation-extraction-still-process: adopt the said device of present embodiment; Inoculum size by 5% inserts activatory bacterium liquid in 7% corn mash substratum; TV is 0.8 liter; Join in the fermentor tank 108 through opening for feed 107, in extraction tower 103, add oleic acid through opening for feed 105 then and exceed well heater 102 lower edges 0.04 m, the height H of extraction agent as extraction agent to extraction agent liquid level eBe 0.37 m, the distance H of extraction agent liquid level and extraction tower cat head vBe 0.06 m; Leave standstill under 37 ℃ and cultivated 72 hours, acetone, butanols and ethanol that fermentation produces are extracted in the extraction agent, and upwards migration; The water of condensation of open cold condenser 101; The extraction agent temperature that the extraction agent of 102 pairs of extraction tower internal upper parts of heater heats and pass through to regulate heater voltage control extraction tower internal upper part is at 120～130 ℃; Working pressure is a normal atmosphere; The acetone, butanols and the ethanol that are dissolved in the extraction agent are constantly vaporized, and after condensing surface 101 condensations, collect, and replenish in extraction tower 103 through opening for feed 105 simultaneously to add oleic acid (extraction agent) to keep the distance H of extraction agent liquid level and extraction tower cat head vBe 0.06 m; Pick up counting when having cut to distillate, close the heating of well heater 102 after 3 hours, close the water of condensation of condensing surface 101 again after 2.0 hours.Obtain cut 0.032 kg; Butanol content is 31.4% (mass percent), and acetone content is 11.4% (mass percent), and ethanol content is 4.0% (mass percent); Water-content is 53.2% (mass percent), and well heater 102 stops to heat 0.305 kilowatt-hour of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 0.305/0.032=9.53 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 0.13 kilowatt-hour/kg of 9.66 kilowatt-hours/kg).
Embodiment 3
Fermentation-extraction-water distilling apparatus: the device shown in the accompanying drawing 1, wherein fermentor tank 108 volumes are 5 liters, inner barrel diameter 0.15 m; Extraction tower 103 height H tBe 1.5 m, tower internal diameter 0.15 m; Well heater 102 is the electrically heated cover, is positioned on extraction tower 103 external wall of upper portion chuck height H hBe 0.25 m, its power is 3 kilowatts, the distance H of its upper limb and extraction tower cat head pBe 0.3 m.
Fermentation-extraction-still-process: the inoculum size by 5% inserts activatory bacterium liquid in 7% corn mash substratum, and TV is 50 liters, under 37 ℃, leaves standstill earlier to cultivate 72 hours; Adopt the said device of present embodiment; 5 liters of fermented liquids are joined in the fermentor tank 108 through opening for feed 107; In extraction tower 103, add Unimac 5680 through opening for feed 105 then and exceed well heater 102 lower edges 0.25 m, the height H of extraction agent as extraction agent to extraction agent liquid level eBe 1.3 m, the distance H of extraction agent liquid level and extraction tower cat head vBe 0.3 m; Acetone in the fermented liquid, butanols and ethanol are extracted in the extraction agent, and upwards migration; The water of condensation of open cold condenser 101 after 2 hours; The extraction agent temperature that the extraction agent of 102 pairs of extraction tower internal upper parts of heater heats and pass through to regulate heater voltage control extraction tower internal upper part is at 120～130 ℃; Working pressure is a normal atmosphere; The acetone, butanols and the ethanol that are dissolved in the extraction agent are constantly vaporized; After condensing surface 101 condensations, collect, in extraction tower 103, replenish adding Unimac 5680 (extraction agent) to keep the distance H of extraction agent liquid level and extraction tower cat head through opening for feed 105 simultaneously vBe 0.3 m; After 2 hours the speed of remaining 45 liters of fermented liquids with 10 liters/hour is joined in the fermentor tank 108 through opening for feed 107; Constant from discharge port 110 discharge fermented liquids simultaneously with the fermentating liquid volume of keeping the fermentor tank 108; 4.5 reinforced finishing closed opening for feed 107 and discharge port 110 after hour; Pick up counting when having cut to distillate, close the heating of well heater 102 after 8 hours, close the water of condensation of condensing surface 101 again after 2.0 hours.Obtain cut 2.10 kg; Butanol content is 30.7% (mass percent), and acetone content is 11.2% (mass percent), and ethanol content is 3.90% (mass percent); Water-content is 54.2% (mass percent), and well heater 102 stops to heat 13.9 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 13.9/2.10=6.62 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 3.04 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 4
Fermentation-extraction-water distilling apparatus: the device shown in the accompanying drawing 1, wherein fermentor tank 108 volumes are 15 liters, inner barrel diameter 0.2 m; Extraction tower 103 height H tBe 3.0 m, tower internal diameter 0.2 m; Well heater 102 is the electrically heated cover, is positioned on extraction tower 103 external wall of upper portion chuck height H hBe 0.9 m, its power is 4 kilowatts, the distance H of its upper limb and extraction tower cat head pBe 1.2 m.
Fermentation-extraction-still-process: the inoculum size by 5% inserts activatory bacterium liquid in 7% corn mash substratum, and TV is 150 liters; Adopt the said device of present embodiment; 15 liters of corn mash substratum of activatory join in the fermentor tank 108 through opening for feed 107; In extraction tower 103, add triricinoleiden through opening for feed 105 then and exceed well heater 102 lower edges 0.9 m, the height H of extraction agent as extraction agent to extraction agent liquid level eBe 2.0 m, the distance H of extraction agent liquid level and extraction tower cat head vBe 1.2 m; Leave standstill under 37 ℃ and cultivated 72 hours, acetone, butanols and ethanol that fermentation produces are extracted in the extraction agent, and upwards migration; The water of condensation of open cold condenser 101; The extraction agent temperature that the extraction agent of 102 pairs of extraction tower internal upper parts of heater heats and pass through to regulate heater voltage control extraction tower internal upper part is at 120～130 ℃; Working pressure is a normal atmosphere; The acetone, butanols and the ethanol that are dissolved in the extraction agent are constantly vaporized, and after condensing surface 101 condensations, collect, and replenish in extraction tower 103 through opening for feed 105 simultaneously to add triricinoleiden (extraction agent) to keep the distance H of extraction agent liquid level and extraction tower cat head vBe 1.2 m; After 2 hours the speed of remaining 135 liters of corn mash substratum with 2.5 liters/hour is joined in the fermentor tank 108 through opening for feed 107; Constant from discharge port 110 discharge fermented liquids simultaneously with the fermentating liquid volume of keeping the fermentor tank 108; Reinforced finishing closed opening for feed 107 and discharge port 110 after 54 hours; Pick up counting when having cut to distillate, close the heating of well heater 102 after 60 hours, close the water of condensation of condensing surface 101 again after 2.0 hours.Obtain cut 6.23 kg; Butanol content is 31.0% (mass percent), and acetone content is 11.3% (mass percent), and ethanol content is 4.0% (mass percent); Water-content is 53.7% (mass percent), and well heater 102 stops to heat 48.6 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 48.6/6.23=7.80 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 1.86 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 5
Fermentation-extraction-water distilling apparatus: the device shown in the accompanying drawing 1, wherein fermentor tank 108 volumes are 95 liters, inner barrel diameter 0.35 m; Extraction tower 103 height H tBe 10 m, tower internal diameter 0.3 m; Well heater 102 is the electrically heated cover, is positioned on extraction tower 103 external wall of upper portion chuck height H hBe 2 m, its power is 8 kilowatts, the distance H of its upper limb and extraction tower cat head pBe 2.2 m.
Fermentation-extraction-still-process: the inoculum size by 5% inserts activatory bacterium liquid in 7% corn mash substratum, and TV is 95 liters, under 37 ℃, leaves standstill earlier to cultivate 72 hours; Adopt the said device of present embodiment; 95 liters of fermented liquids are joined in the fermentor tank 108 through opening for feed 107; In extraction tower 103, add methyl ricinoleate through opening for feed 105 then and exceed well heater 102 lower edges 2.1 m, the height H of extraction agent as extraction agent to extraction agent liquid level eBe 8.0 m, the distance H of extraction agent liquid level and extraction tower cat head vBe 2.1 m; Acetone in the fermented liquid, butanols and ethanol are extracted in the extraction agent, and upwards migration; The water of condensation of open cold condenser 101 after 2 hours; The extraction agent temperature that the extraction agent of 102 pairs of extraction tower internal upper parts of heater heats and pass through to regulate heater voltage control extraction tower internal upper part is at 120～130 ℃; Working pressure is a normal atmosphere; The acetone, butanols and the ethanol that are dissolved in the extraction agent are constantly vaporized; After condensing surface 101 condensations, collect, in extraction tower 103, replenish adding methyl ricinoleate (extraction agent) to keep the distance H of extraction agent liquid level and extraction tower cat head through opening for feed 105 simultaneously vBe 2.1 m; Pick up counting when having cut to distillate, close the heating of well heater 102 after 6 hours, close the water of condensation of condensing surface 101 again after 2.0 hours.Obtain cut 4.3 kg; Butanol content is 29.0% (mass percent), and acetone content is 11.0% (mass percent), and ethanol content is 4.0% (mass percent); Water-content is 56.0% (mass percent), and well heater 102 stops to heat 26.53 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 26.53/4.3=6.17 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 3.49 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 6
Fermentation-extraction-water distilling apparatus: the device shown in the accompanying drawing 1, wherein fermentor tank 108 volumes are 150 liters, inner barrel diameter 0.42 m; Extraction tower 103 height H tBe 15 m, tower internal diameter 0.4 m; Well heater 102 is the electrically heated cover, is positioned on extraction tower 103 external wall of upper portion chuck height H hBe 0.15 m, its power is 8 kilowatts, the distance H of its upper limb and extraction tower cat head pBe 0.15 m.
Fermentation-extraction-still-process: adopt the said device of present embodiment; Inoculum size by 5% inserts activatory bacterium liquid in 7% corn mash substratum; TV is 150 liters; Join in the fermentor tank 108 through opening for feed 107, in extraction tower 103, add ethyl ricinoleate through opening for feed 105 then and exceed well heater 102 lower edges 0.15 m, the height H of extraction agent as extraction agent to extraction agent liquid level eBe 14.9 m, the distance H of extraction agent liquid level and extraction tower cat head vBe 0.15 m; Leave standstill under 37 ℃ and cultivated 72 hours, acetone, butanols and ethanol that fermentation produces are extracted in the extraction agent, and upwards migration; The water of condensation of open cold condenser 101; The extraction agent temperature that the extraction agent of 102 pairs of extraction tower internal upper parts of heater heats and pass through to regulate heater voltage control extraction tower internal upper part is at 120～130 ℃; Working pressure is a normal atmosphere; The acetone, butanols and the ethanol that are dissolved in the extraction agent are constantly vaporized, and after condensing surface 101 condensations, collect, and replenish in extraction tower 103 through opening for feed 105 simultaneously to add ethyl ricinoleate (extraction agent) to keep the distance H of extraction agent liquid level and extraction tower cat head vBe 0.15 m; Pick up counting when having cut to distillate, close the heating of well heater 102 after 8 hours, close the water of condensation of condensing surface 101 again after 2.0 hours.Obtain cut 6.7 kg; Butanol content is 29.6% (mass percent), and acetone content is 11.1% (mass percent), and ethanol content is 3.90% (mass percent); Water-content is 55.4% (mass percent), and well heater 102 stops to heat 41.35 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 41.35/6.7=6.17 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 3.49 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 7
Fermentation-extraction-water distilling apparatus: the device shown in the accompanying drawing 1, wherein fermentor tank 108 volumes are 400 liters, inner barrel diameter 0.57 m; Extraction tower 103 height H tBe 20 m, tower internal diameter 0.5 m; Well heater 102 is the electrically heated cover, is positioned on extraction tower 103 external wall of upper portion chuck height H hBe 5 m, its power is 10 kilowatts, the distance H of its upper limb and extraction tower cat head pBe 5 m.
Fermentation-extraction-still-process: adopt the said device of present embodiment; Inoculum size by 5% inserts activatory bacterium liquid in 7% corn mash substratum; TV is 400 liters; Join in the fermentor tank 108 through opening for feed 107, in extraction tower 103, add butyl butyrate through opening for feed 105 then and exceed well heater 102 lower edges 6.0 m, the height H of extraction agent as extraction agent to extraction agent liquid level eBe 16.2 m, the distance H of extraction agent liquid level and extraction tower cat head vBe 4.0 m; Leave standstill under 37 ℃ and cultivated 72 hours, acetone, butanols and ethanol that fermentation produces are extracted in the extraction agent, and upwards migration; The water of condensation of open cold condenser 101; The extraction agent temperature that the extraction agent of 102 pairs of extraction tower internal upper parts of heater heats and pass through to regulate heater voltage control extraction tower internal upper part is at 120～130 ℃; Working pressure is a normal atmosphere; The acetone, butanols and the ethanol that are dissolved in the extraction agent are constantly vaporized, and after condensing surface 101 condensations, collect, and replenish in extraction tower 103 through opening for feed 105 simultaneously to add butyl butyrate (extraction agent) to keep the distance H of extraction agent liquid level and extraction tower cat head vBe 4.0 m; Pick up counting when having cut to distillate, close the heating of well heater 102 after 20 hours, close the water of condensation of condensing surface 101 again after 2.0 hours.Obtain cut 18.4 kg; Butanol content is 28.5% (mass percent), and acetone content is 11.1% (mass percent), and ethanol content is 3.98% (mass percent); Water-content is 56.42% (mass percent), and well heater 102 stops to heat 113.35 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 113.35/18.4=6.16 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 3.50 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 8
Fermentation-extraction-water distilling apparatus: the device shown in the accompanying drawing 1, wherein fermentor tank 108 volumes are 5 liters, inner barrel diameter 0.15 m; Extraction tower 103 height H tBe 1.6 m, tower internal diameter 0.15 m; Well heater 102 is the electrically heated cover, is positioned on extraction tower 103 external wall of upper portion chuck height H hBe 0.4 m, its power is 2 kilowatts, the distance H of its upper limb and extraction tower cat head pBe 0.4 m.
Fermentation-extraction-still-process: adopt the said device of present embodiment; Inoculum size by 5% inserts activatory bacterium liquid in 7% corn mash substratum; TV is 5 liters; Join in the fermentor tank 108 through opening for feed 107, in extraction tower 103, add certain herbaceous plants with big flowers two dibutyl phthalates through opening for feed 105 then and exceed well heater 102 lower edges 0.4 m, the height H of extraction agent as extraction agent to extraction agent liquid level eBe 1.25 m, the distance H of extraction agent liquid level and extraction tower cat head vBe 0.4 m; Leave standstill under 37 ℃ and cultivated 72 hours, acetone, butanols and ethanol that fermentation produces are extracted in the extraction agent, and upwards migration; The water of condensation of open cold condenser 101; The extraction agent temperature that the extraction agent of 102 pairs of extraction tower internal upper parts of heater heats and pass through to regulate heater voltage control extraction tower internal upper part is at 120～130 ℃; Working pressure is a normal atmosphere; The acetone, butanols and the ethanol that are dissolved in the extraction agent are constantly vaporized, and after condensing surface 101 condensations, collect, and replenish in extraction tower 103 through opening for feed 105 simultaneously to add certain herbaceous plants with big flowers two dibutyl phthalates (extraction agent) to keep the distance H of extraction agent liquid level and extraction tower cat head vBe 0.4 m; Pick up counting when having cut to distillate, close the heating of well heater 102 after 3 hours, close the water of condensation of condensing surface 101 again after 2.0 hours.Obtain cut 0.225 kg; Butanol content is 27.3% (mass percent), and acetone content is 11.3% (mass percent), and ethanol content is 4.0% (mass percent); Water-content is 57.4% (mass percent), and well heater 102 stops to heat 1.87 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 1.87/0.225=8.31 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 1.35 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 9
Except that adopting certain herbaceous plants with big flowers diacid di-isooctyl is the extraction agent; Other obtains cut 0.24 kg with embodiment 8, and butanol content is 27.8% (mass percent); Acetone content is 11.3% (mass percent); Ethanol content is 3.98% (mass percent), and water-content is 56.92% (mass percent), and well heater 102 stops to heat 1.86 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 1.86/0.24=7.75 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 1.91 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 10
Except that adopting sym-trimethylbenzene is the extraction agent; Other obtains cut 0.231 kg with embodiment 8, and butanol content is 27.9% (mass percent); Acetone content is 11.8% (mass percent); Ethanol content is 3.95% (mass percent), and water-content is 56.35% (mass percent), and well heater 102 stops to heat 1.76 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 1.76/0.231=7.62 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 2.04 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 11
Except that adopting decyl alcohol is the extraction agent; Other obtains cut 0.221 kg with embodiment 8, and butanol content is 28.5% (mass percent); Acetone content is 11.2% (mass percent); Ethanol content is 4.0% (mass percent), and water-content is 56.3% (mass percent), and well heater 102 stops to heat 1.91 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 1.91/0.221=8.64 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 1.02 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 12
Except that adopting lauryl alcohol is the extraction agent; Other obtains cut 0.220 kg with embodiment 8, and butanol content is 28.0% (mass percent); Acetone content is 11.2% (mass percent); Ethanol content is 3.92% (mass percent), and water-content is 56.88% (mass percent), and well heater 102 stops to heat 1.89 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 1.89/0.220=8.59 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 1.07 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 13
Except that adopting tetradecyl alcohol is the extraction agent; Other obtains cut 0.224 kg with embodiment 8, and butanol content is 27.9% (mass percent); Acetone content is 11.4% (mass percent); Ethanol content is 3.91% (mass percent), and water-content is 56.79% (mass percent), and well heater 102 stops to heat 1.81 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 1.81/0.224=8.08 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 1.58 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 14
Except that adopting oleyl alcohol is the extraction agent; Other obtains cut 0.220 kg with embodiment 8, and butanol content is 29.3% (mass percent); Acetone content is 11.8% (mass percent); Ethanol content is 3.98% (mass percent), and water-content is 54.92% (mass percent), and well heater 102 stops to heat 1.89 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 1.89/0.220=8.59 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 1.07 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 15
Except that adopting isooctadecanol is the extraction agent; Other obtains cut 0.215 kg with embodiment 8, and butanol content is 28.9% (mass percent); Acetone content is 11.5% (mass percent); Ethanol content is 3.90% (mass percent), and water-content is 55.7% (mass percent), and well heater 102 stops to heat 1.85 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 1.85/0.215=8.60 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 1.06 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 16
Except that adopting the mixture that contains 50% (mass percent) decyl alcohol, 50% (mass percent) tetradecyl alcohol is the extraction agent; Other obtains cut 0.233 kg with embodiment 8, and butanol content is 28.6% (mass percent); Acetone content is 11.3% (mass percent); Ethanol content is 3.99% (mass percent), and water-content is 56.11% (mass percent), and well heater 102 stops to heat 1.92 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 1.92/0.233=8.24 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 1.42 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 17
Except that adopting the mixture that contains 30% (mass percent) tetradecyl alcohol, 30% (mass percent) isooctadecanol, 40% (mass percent) ethyl ricinoleate is the extraction agent; Other obtains cut 0.220 kg with embodiment 8, and butanol content is 28.3% (mass percent); Acetone content is 11.5% (mass percent); Ethanol content is 3.98% (mass percent), and water-content is 56.22% (mass percent), and well heater 102 stops to heat 1.91 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 1.91/0.220=8.68 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 0.98 kilowatt-hour/kg of 9.66 kilowatt-hours/kg).
Embodiment 18
Except that adopting the mixture that contains 25% (mass percent) ethyl ricinoleate, 25% (mass percent) OE, 25% (mass percent) certain herbaceous plants with big flowers, two dibutyl phthalates, 25% (mass percent) isooctadecanol is the extraction agent; Other is with embodiment 8; Obtain cut 0.225 kg; Butanol content is 27.4% (mass percent), and acetone content is 11.8% (mass percent), and ethanol content is 3.95% (mass percent); Water-content is 56.85% (mass percent), and well heater 102 stops to heat 1.83 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 1.83/0.225=8.13 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 1.53 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 19
Fermentation-extraction-water distilling apparatus: the device shown in the accompanying drawing 2, wherein fermentor tank 108 volumes are 150 liters, inner barrel diameter 0.42 m; Extraction tower 103 is formed its height H by a truncated cone-shaped tube and a cylinder that connects with it tBe 8 m, the high H of truncated cone-shaped tube wherein cBe 7.1 m, internal diameter 0.4 m that goes to the bottom, upper base internal diameter 0.2 m; Well heater 102 is the electrically heated cover, is positioned on extraction tower 103 external wall of upper portion chuck height H hBe 0.4 m, its power is 4 kilowatts, the distance H of its upper limb and extraction tower cat head pBe 0.5 m.
Fermentation-extraction-still-process: adopt the said device of present embodiment; Inoculum size by 5% inserts activatory bacterium liquid in 7% corn mash substratum; TV is 150 liters; Join in the fermentor tank 108 through opening for feed 107, in extraction tower 103, add ethyl ricinoleate through opening for feed 105 then and exceed well heater 102 lower edges 0.4 m, the height H of extraction agent as extraction agent to extraction agent liquid level eBe 7.6 m, the distance H of extraction agent liquid level and extraction tower cat head vBe 0.5 m; Leave standstill under 37 ℃ and cultivated 72 hours, acetone, butanols and ethanol that fermentation produces are extracted in the extraction agent, and upwards migration; The water of condensation of open cold condenser 101; The extraction agent temperature that the extraction agent of 102 pairs of extraction tower internal upper parts of heater heats and pass through to regulate heater voltage control extraction tower internal upper part is at 120～130 ℃; Working pressure is a normal atmosphere; The acetone, butanols and the ethanol that are dissolved in the extraction agent are constantly vaporized, and after condensing surface 101 condensations, collect, and replenish in extraction tower 103 through opening for feed 105 simultaneously to add ethyl ricinoleate (extraction agent) to keep the distance H of extraction agent liquid level and extraction tower cat head vBe 0.5 m; Pick up counting when having cut to distillate, close the heating of well heater 102 after 10 hours, close the water of condensation of condensing surface 101 again after 2.0 hours.Obtain cut 5.72 kg; Butanol content is 29.7% (mass percent), and acetone content is 11.1% (mass percent), and ethanol content is 3.90% (mass percent); Water-content is 55.3% (mass percent), and well heater 102 stops to heat 32.55 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut well heater 102 is 32.55/5.72=5.69 kilowatt-hour/kg, than the power consumption of per unit mass cut heating jacket 328 among the embodiment 20 (Comparative Examples) (low 3.97 kilowatt-hours/kg of 9.66 kilowatt-hours/kg).
Embodiment 20 (Comparative Examples)
The device and the flow process that adopt the liquid-liquid extraction reported in the present document and acetone to be coupled, the device shown in accompanying drawing 3, wherein 301,310,317,322,324, the 332-pump; 302,305,325-feed valve; 303,304,311,314,319,326-opening for feed; The 306-fermentor tank; 307,328-heating jacket; 308,312,315,320,329-discharge port; 309,316,321,330-bleeder valve; The 313-extractor; 318-extraction agent storage tank; The 323-condensing surface; The 327-still kettle; The 331-water cooler; W 301The water inlet of-water of condensation; W 302The water outlet of-water of condensation; W 303The water inlet of-water coolant; W 304The water outlet of-water coolant; D 301-distillation condensed product; Fermentor tank 306 volumes are 5 liters, inner barrel diameter 0.15 m; Extractor 313 volumes are 20 liters, inner barrel diameter 0.30 m; Extraction agent storage tank 318 volumes are 25 liters; Still kettle 327 volumes are 10 liters, inner barrel diameter 0.25 m; Heating jacket 328 adopts Electric heating, and its power is 2.0 kilowatts.
Fermentation, extraction, still-process: adopt the said device of this comparative example, the inoculum size by 5% inserts activatory bacterium liquid in 7% corn mash substratum, and TV is 5 liters; Join in the fermentor tank 306 through opening for feed 303, leave standstill under 37 ℃ and cultivated 72 hours, be transferred to afterwards in the extractor 313; Add 10 liters of OEs as extraction agent, stir 30 min, leave standstill 60 min; The fermented liquid of lower floor is transferred in the fermentor tank 306; The extraction agent on upper strata is transferred in the still kettle 327, and the extraction agent temperature that the water of condensation of open cold condenser 323,328 pairs of extraction agents of unlatching heating jacket heat and pass through to regulate heater voltage control extraction tower internal upper part is at 120～130 ℃; Working pressure is a normal atmosphere, and the acetone, butanols and the ethanol that are dissolved in the extraction agent are vaporized after collect after condensing surface 323 condensations; Pick up counting when having cut to distillate, close the heating of heating jacket 328 after 3 hours, close the water of condensation of condensing surface 323 again after 2.0 hours.Open the water of condensation of water cooler 331, extraction agent is transferred to after condensation in the extraction agent storage tank 318.Obtain cut 0.178 kg; Butanol content is 30.5% (mass percent), and acetone content is 11.2% (mass percent), and ethanol content is 3.80% (mass percent); Water-content is 54.5% (mass percent), and heating jacket 328 stops to heat 1.72 kilowatt-hours of power consumption altogether from beginning to be heated to.
In the present embodiment, the power consumption of per unit mass cut heating jacket 328 is 1.72/0.178=9.66 kilowatt-hour/kg.

Claims (8)

1. acetone separation coupling device; It by fermentor tank, be arranged on fermentor tank top and the extraction tower that connects with it, be installed on the well heater on extraction tower top and the condensing surface that is communicated with the extraction tower top is formed; In this device, realize fermentation simultaneously, extract and distill three processes, wherein the extraction tower outer wall is provided with opening for feed, is provided with feed valve before the opening for feed; Extraction tower bottom outer wall is provided with discharge port, is provided with bleeder valve behind the discharge port; And the fermentor tank outer wall is provided with opening for feed, is provided with feed valve before the opening for feed, and the fermentor tank bottom is provided with discharge port, and the discharge port bottom is provided with bleeder valve; The height H of extraction tower tBe 0.4～20 m; The height H of said well heater hBe 0.05～5 m, and H h=0.01 H t～0.3 H tThe distance H of the upper limb of said well heater and extraction tower cat head pBe 0.05～5 m, and H p=0.01 H t～0.4 H t
2. device according to claim 1 is characterized in that the height H of extraction tower tBe 1.5～15 m.
3. device according to claim 1 and 2 is characterized in that said well heater is the electrically heated cover, is installed on the extraction tower external wall of upper portion.
4. one kind is used acetone separation coupling device as claimed in claim 1 to accomplish acetone separation coupled process method, it is characterized in that it may further comprise the steps:
(a) in the fermentor tank of acetone separation coupling device as claimed in claim 1, carry out acetone; Perhaps earlier in conventional fermentor tank, carry out acetone, afterwards fermented liquid is joined in the acetone separation coupling device as claimed in claim 1;
(b) extraction agent is housed in extraction tower;
(c) acetone, butanols and the ethanol of fermentation generation are extracted in the extraction agent, and upwards migration;
(d) well heater through being installed on extraction tower top heats the extraction agent of extraction tower internal upper part, and the acetone, butanols and the ethanol that are dissolved in the extraction agent are constantly distilled away, after condenser condenses, collects to such an extent that contain acetone, butanols and alcoholic acid solution.
5. acetone according to claim 4 separates the coupled process method, it is characterized in that the liquid level that in extraction tower, adds extraction agent is higher than the well heater lower edge, and with the distance of this well heater lower edge be 0.8 H h～1.2 H hH hHeight for well heater; And extraction agent liquid level and extraction tower cat head remain on when distillation liquid boiling to carry out with vaporization is overflowed smoothly, and the liquid spittle distance of not taken out of by steam.
6. acetone according to claim 4 separates the coupled process method, and the boiling point that it is characterized in that said extraction agent is 140～800 ℃.
7. acetone according to claim 4 separates the coupled process method, and the density that it is characterized in that said extraction agent is 0.83～0.97 kg/m 3
8. acetone according to claim 4 separates the coupled process method, it is characterized in that extraction agent is a kind of, two or more the mixture in OE, oleic acid, Unimac 5680, triricinoleiden, methyl ricinoleate, ethyl ricinoleate, butyl butyrate, certain herbaceous plants with big flowers two dibutyl phthalates, certain herbaceous plants with big flowers diacid di-isooctyl, sym-trimethylbenzene, decyl alcohol, lauryl alcohol, tetradecyl alcohol, oleyl alcohol, the isooctadecanol.
CN2011100390367A 2011-02-16 2011-02-16 Process method and device for coupling acetone-butyl alcohol fermentation and separation Expired - Fee Related CN102174371B (en)

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