CN113072424A - Energy-saving device and process for producing fuel ethanol by purifying fermentation liquor - Google Patents
Energy-saving device and process for producing fuel ethanol by purifying fermentation liquor Download PDFInfo
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- CN113072424A CN113072424A CN202110294625.3A CN202110294625A CN113072424A CN 113072424 A CN113072424 A CN 113072424A CN 202110294625 A CN202110294625 A CN 202110294625A CN 113072424 A CN113072424 A CN 113072424A
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Abstract
The invention discloses an energy-saving device and a process for producing fuel ethanol by purifying fermentation liquor. Aiming at the fact that the existing process for producing fuel ethanol by purifying fermentation liquor has a space for reducing energy consumption, the three-tower differential pressure distillation technology is selected, and by means of side line extraction, full utilization of heat of material streams in a system and the like, the steam consumption can be greatly reduced while the product quality is ensured, so that the steam consumption of the biofuel ethanol reaches below 1.4 ton/ton, the process is optimized, the purification process is more energy-saving, and the economic benefit is improved while the purposes of energy conservation and environmental protection are achieved.
Description
Technical Field
The invention relates to the technical field of preparation of biofuel ethanol, in particular to an energy-saving device and process for producing fuel ethanol by purifying fermentation liquor.
Background
The fuel ethanol is a clean energy source, and is a novel energy source which is internationally recognized and can reduce environmental pollution and replace petroleum fuel. In the production process of the bioethanol, rectification and refining, namely the distillation and dehydration unit process, plays a significant role in controlling the product quality, yield and public engineering consumption in the whole production process, and can be called as a key technology of the bioethanol production process. The distillation and dehydration unit consumes the most energy in the whole fuel ethanol production process, accounting for 60-70% of the total energy consumption, and efficient distillation technology needs to be developed. The content of ethanol in mature mash is only 10-15% (volume), the rest contains impurities such as water, alcohols, acids, lipids and the like, the distilled crude ethanol still contains various volatile impurities, the boiling points of partial impurities are close, and further separation and purification are difficult.
Chinese patent CN201110029536.2 discloses an energy-saving process for preparing absolute ethyl alcohol from biological ethyl alcohol aqueous solution, wherein three rectifying towers with stepwise pressure reduction are adopted to provide a heat source for the next rectifying tower by utilizing the heat contained in the self material of the previous rectifying tower, the insufficient part is supplemented by an air source heat pump system, the waste heat which is not utilized in the material discharged by the rectifying towers is utilized to preheat the ethyl alcohol aqueous solution raw material to form a thermal coupling network, so that the energy consumption of the absolute ethyl alcohol produced by unit mass is reduced by 30-48% compared with the traditional process, but the arrangement of a compressor increases the power consumption, and the power consumption is increased by utilizing the frozen salt water provided by a freezing system as a refrigerant. Chinese patent CN201810719237.3 discloses a system for producing fuel ethanol by double-coarse double-fine four-tower four-effect energy-saving distillation and a use method thereof, comprising a negative pressure mash tower/degassing section, an atmospheric mash tower, a medium pressure fine tower and a high pressure fine tower, wherein one tower is used for steam admission, the four towers work, the consumption in the distillation process is reduced, the mash treatment temperature is controlled to be lower, but the equipment and the operation cost of one tower are increased. Chinese patent CN201920237176.7 discloses an energy-saving process apparatus for producing fuel ethanol from low-concentration fermentation broth, wherein the whole rectification system comprises four towers, such as a first rectification tower, a second rectification tower, a third rectification tower, a fourth rectification tower, and a dehydration unit and other supporting equipment, the energy consumption of operation is greatly reduced by heat integration between the four towers and application of other heat exchange and energy-saving technologies in the system, the energy consumption of operation is only 1.8 tons of steam/ton of fuel ethanol product, but the number of towers is large, and the energy consumption of operation has further space for optimization.
The above patents have the defects of higher power consumption of equipment, more towers, higher equipment cost and the like, and certain space is also provided for improving the energy consumption.
Disclosure of Invention
Aiming at the technical problems in the prior art, the invention provides an energy-saving device and process for producing fuel ethanol by purifying fermentation liquor, which adopt a three-tower differential pressure thermal coupling rectification dehydration technology, ensure the product quality and greatly reduce the steam consumption by means of side line extraction, furthest utilizing the potential energy of each stream and the like, so that the ethanol rectification recovery rate is more than 99.5 percent, and the steam consumption reaches below 1.4 tons/ton of fuel ethanol.
The invention provides an energy-saving device for producing fuel ethanol by purifying fermentation liquor, which comprises: a rough distillation tower, a first rectification tower, a second rectification tower, a No. 1 molecular sieve adsorption bed, a No. 2 molecular sieve adsorption bed, a rough tower top heat exchanger, a mash preheater, a rough distillation tower cooler, a rough distillation tower kettle reboiler, a first rectification tower preheater, a second rectification tower preheater, a first rectification tower kettle reboiler, an ethanol vapor superheater, a regenerated gas condenser, a fusel oil cooler, a second rectification tower preheater, a rough distillation tower reflux tank, a second rectification tower reflux tank, a first rectification tower reflux tank, a fusel oil extraction tank, a light wine recovery tank and a condensate tank, a filter and a crude wine filter;
the gas port at the top of the crude distillation tower is respectively connected with the hot material inlet of the heat exchanger at the top of the crude distillation tower and the hot material inlet of the cooler of the crude distillation tower, the reflux port of the crude distillation tower is connected with the discharge port of the reflux tank of the crude distillation tower, the hot material outlet of the heat exchanger at the top of the crude distillation tower and the hot material outlet of the cooler of the crude distillation tower are both connected with the feed inlet of the reflux tank of the crude distillation tower, the cold material outlet of the coarse tower top heat exchanger is connected with the cold material inlet of the mash preheater, the cold material outlet of the mash preheater is connected with the tower side feed inlet of the coarse distillation tower, a first side collecting port of the coarse distillation tower is connected with a feed inlet of a light wine recovery tank, a second side collecting port of the coarse distillation tower is respectively connected with a cold material inlet of a second preheater of the second rectifying tower and a cold material inlet of a first preheater of the second rectifying tower, the cold material outlet of the second preheater of the second rectifying tower and the cold material outlet of the first preheater of the second rectifying tower are both connected with the tower side feed inlet of the second rectifying tower;
the gas port at the top of the second rectifying tower is respectively connected with a hot material inlet of a reboiler at the bottom of the coarse rectifying tower and a cold material inlet of an ethanol steam superheater, a cold material outlet of the ethanol steam superheater is respectively connected with a feed inlet of a 1# molecular sieve adsorption bed and a feed inlet of a 2# molecular sieve adsorption bed, a hot material outlet of the reboiler at the bottom of the coarse rectifying tower is connected with a feed inlet of a reflux tank of the second rectifying tower, a discharge outlet of the reflux tank of the second rectifying tower is connected with a reflux port of the second rectifying tower, a material extraction outlet of the bottom of the second rectifying tower is connected with a hot material inlet of a first preheater of the second rectifying tower, a side extraction port of the second rectifying tower is connected with a feed inlet of a filter, and a filtrate discharge outlet of the filter is connected with a side feed inlet of the first rectifying;
the top gas port of the first rectifying tower is connected with a hot material inlet of a reboiler of a second rectifying tower, a hot material outlet of the reboiler of the second rectifying tower is connected with a feed inlet of a reflux tank of the first rectifying tower, a discharge port of the reflux tank of the first rectifying tower is respectively connected with a reflux port of the first rectifying tower and a top feed inlet of the second rectifying tower, a tower bottom material extraction port of the first rectifying tower is connected with a hot material inlet of a first preheater of the first rectifying tower, a side extraction port of the first rectifying tower is connected with a hot material inlet of a fusel oil cooler, a hot material outlet of the fusel oil cooler is connected with a feed inlet of a fusel oil extraction tank, and a discharge port at the bottom of the fusel oil extraction tank is connected with a feed inlet of a light wine recovery tank;
the first discharge port of the 1# molecular sieve adsorption bed and the first discharge port of the 2# molecular sieve adsorption bed are both connected with a hot material inlet of a mash preheater, the second discharge port of the 1# molecular sieve adsorption bed and the second discharge port of the 2# molecular sieve adsorption bed are both connected with a hot material inlet of a regenerated gas condenser, a hot material outlet of the regenerated gas condenser is connected with a feed inlet of a weak liquor recovery tank, a discharge port of the weak liquor recovery tank is connected with a feed inlet of a crude liquor filter, a filtrate discharge port of the crude liquor filter is respectively connected with a cold material inlet of a first preheater of a first rectification tower and a cold material inlet of a second preheater of a first rectification tower, and a cold material outlet of the first preheater of the first rectification tower and a cold material outlet of the second preheater of the first rectification tower are both connected with a tower side feed inlet of the first rectification tower;
the hot material outlet of the distillation first tower kettle reboiler and the hot material outlet of the ethanol steam superheater are both connected with the feed inlet of the condensate tank, the discharge port of the condensate tank is connected with the hot material inlet of the distillation first tower second preheater, and the hot material outlet of the distillation first tower second preheater is connected with the hot material inlet of the distillation second tower second preheater.
The invention also discloses an energy-saving process based on the energy-saving device, which comprises the following steps:
s1, preheating fermentation liquor, then feeding the preheated fermentation liquor into a rough distillation tower, condensing overhead gas, discharging non-condensable gas, then completely refluxing, sending waste mash at the bottom of the tower to centrifugal separation, collecting two materials at a lateral line, feeding one material into a second rectification tower, and feeding the other material into a weak liquor recovery tank;
s2, rectifying the material entering the second rectifying tower, sending waste mash extracted from the bottom of the second rectifying tower to centrifugal separation, filtering out solid from a side line, then feeding filtrate into the first rectifying tower, condensing and discharging noncondensable gas from the top of the first rectifying tower, refluxing the condensed gas, and continuously heating the top gas to form superheated steam to enter a molecular sieve adsorption bed;
s3, preheating the filtrate obtained by filtering the filtrate obtained by the side of the rectifying tower and the filtrate obtained by filtering solids in a light liquor recovery tank, mixing the preheated filtrate and entering a rectifying tower I, condensing the top gas of the rectifying tower I, returning one reflux and the other reflux to the rectifying tower II, returning the water obtained from the bottom of the rectifying tower to a powder slurry liquefaction unit, condensing the fusel solution obtained from the side line, separating a fusel oil byproduct and a de-fusel liquid from a fusel oil extraction tank, and sending the de-fusel liquid to the light liquor recovery tank;
and S4, dehydrating the steam in a molecular sieve adsorption bed, condensing the ethanol steam at the tower top to obtain a fuel ethanol product, and condensing the separated low-concentration ethanol steam and then sending the condensed low-concentration ethanol steam into a light wine recovery tank.
Preferably, in S1, the heat source for preheating the fermentation liquid is crude distillation tower top gas and molecular sieve adsorbent bed top gas; the heat source of the reboiler at the bottom of the coarse distillation tower is rectifying second tower overhead gas, the tower top pressure of the coarse distillation tower is-0.1 to-0.01 MPaG, the tower bottom temperature is 70 to 90 ℃, and the tower top extraction temperature is 40 to 60 ℃.
Preferably, in S2, a part of the feed preheating heat source of the second rectification column is the bottom effluent of the second rectification column, the reboiler heat source of the second rectification column is the top gas of the first rectification column, the temperature of the bottom of the first rectification column is 100-130 ℃, and the temperature of the top effluent is 80-120 ℃.
Preferably, in S3, a part of the heat source for preheating the filtered effluent of the weak liquor recovery tank is the distillate from the bottom of the rectification tower; the top pressure of the rectifying tower is 0.05-0.5MPaG, the temperature of the tower bottom is 140-.
Preferably, the heat source of the reboiler at the bottom of the rectifying tower is external steam, the heat source of the top gas of the rectifying tower is external steam, condensate of the two streams of steam is sent to a condensate tank, and the condensate flowing out of the condensate tank is used as the heat source and is used as a supplementary heat source for the filtrate flowing out of the weak liquor recovery tank and the feed of the rectifying tower.
Preferably, part of the cold source of the top gas of the crude distillation tower, the cold source of the mixed alcohol solution extracted from the side line of the rectification tower and the light wine steam cold source removed from the molecular sieve adsorption bed are external cooling water.
Compared with the prior art, the invention has the following beneficial effects: the method adopts a three-tower differential pressure distillation technology, and can greatly reduce steam consumption while ensuring product quality by means of side line extraction, full utilization of material stream heat in the system and the like, so that the steam consumption of the biofuel ethanol reaches below 1.4 ton/ton, the process is optimized, and the purification process is more energy-saving; in addition, the purposes of energy conservation and environmental protection are achieved, and meanwhile, the economic benefit is improved.
Drawings
Fig. 1 is a schematic structural diagram of an embodiment of the present invention.
Wherein, T1-crude distillation column, T2-first rectification column, T3-second rectification column, T4-1, 1# molecular sieve adsorption bed, T4-2, 2# molecular sieve adsorption bed, F1-filter, F2-crude wine filter, V1-crude distillation column reflux tank, V2-second distillation column reflux tank, V3-first distillation column reflux tank, V4-fusel oil extraction tank, V5-weak wine recovery tank, V6-condensate tank, E1-crude tower top heat exchanger, E2-mash preheater, E3-crude distillation column cooler, E4-crude distillation column kettle reboiler, E5-second distillation column first preheater, E6-second distillation column kettle reboiler, E7-first distillation column preheater, E8-second distillation column preheater, E9-first distillation column kettle reboiler, E10-ethanol vapor, E11-regeneration gas condenser, E12-superheater fusel oil cooler, E13-second distillation column preheater.
Detailed Description
In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the invention easy to understand, the invention is further explained below by combining the specific drawings.
Referring to fig. 1, the invention provides an energy-saving device and a process for producing fuel ethanol by purifying fermentation liquor, wherein the device comprises: a rough distillation tower T1, a first rectification tower T2, a second rectification tower T3, a 1# molecular sieve adsorption bed T4-1 and a 2# molecular sieve adsorption bed T4-2, a rough top heat exchanger E1, a mash preheater E2, a rough distillation tower cooler E3, a rough distillation tower kettle reboiler E4, a second rectification tower first preheater E5, a second rectification tower kettle reboiler E6, a first rectification tower first preheater E7, a first rectification tower second preheater E8, a first rectification tower kettle reboiler E9, ethanol vapor E10, a regeneration gas superheater E11, a fusel oil cooler E12, a second rectification tower preheater E13, a rough distillation tower reflux tank V1, a second rectification tower reflux tank V2, a first tower reflux tank V3, a fusel oil recovery tank V4, a light liquor recovery tank V4, a crude liquor tank V8672, a rough distillation tower reflux tank V8672 and a crude liquor filter 4.
The top gas port of the crude distillation tower T1 is respectively connected with the hot material inlet of a crude distillation tower top heat exchanger E1 and the hot material inlet of a crude distillation tower cooler E3, the reflux port of the crude distillation tower T1 is connected with the discharge port of a crude distillation tower reflux tank V1, the hot material outlet of the crude distillation tower top heat exchanger E1 and the hot material outlet of a crude distillation tower cooler E3 are both connected with the feed port of a crude distillation tower reflux tank V1, the cold material outlet of the crude distillation tower top heat exchanger E1 is connected with the cold material inlet of a mash liquid preheater E2, the cold material outlet of the mash liquid preheater E2 is connected with the tower side feed port of a crude distillation tower T1, the first side sampling port of the crude distillation tower T1 is connected with the feed port of a weak liquor recovery tank V5, the second side sampling port of the crude distillation tower T1 is respectively connected with the cold material inlet of a second preheater E13 and the first side preheater E6, and the cold material outlet of a second side sampling port of a rectification tower 3527 is connected with the cold material outlet of a second preheater E5 .
The tower top gas port of the second rectification tower T3 is respectively connected with a hot material inlet of a crude distillation tower kettle reboiler E4 and a cold material inlet of an ethanol steam superheater E10, a cold material outlet of the ethanol steam superheater E10 is respectively connected with a feed inlet of a 1# molecular sieve adsorption bed T4-1 and a feed inlet of a 2# molecular sieve adsorption bed T4-2, a hot material outlet of the crude distillation tower kettle reboiler E4 is connected with a feed inlet of a second rectification tower reflux tank V2, a discharge port of the second rectification tower reflux tank V2 is connected with a reflux port of a second rectification tower T3, a tower kettle material extraction outlet of the second rectification tower T3 is connected with a hot material inlet of a first rectification tower preheater E5, a side extraction port of the second rectification tower T3 is connected with a feed inlet of a filter F1, and a filtrate discharge port of the filter F1 is connected with a side inlet of the first rectification tower T2.
The tower top gas port of the first rectification tower T2 is connected with the hot material inlet of a second rectification tower reboiler E6, the hot material outlet of the second rectification tower reboiler E6 is connected with the feed inlet of a first rectification tower reflux tank V3, the discharge port of the first rectification tower reflux tank V3 is respectively connected with the reflux port of the first rectification tower T2 and the tower top feed inlet of a second rectification tower T3, the tower bottom material extraction port of the first rectification tower T2 is connected with the hot material inlet of a first rectification tower preheater E7, the side extraction port of the first rectification tower T2 is connected with the hot material inlet of a fusel oil cooler E12, the hot material outlet of the fusel oil cooler E12 is connected with the extraction feed inlet of a fusel oil extraction tank V4, and the bottom discharge port of the fusel oil tank V4 is connected with the feed inlet of a light wine recovery tank V5.
The first discharge port of the No. 1 molecular sieve adsorption bed T4-1 and the first discharge port of the No. 2 molecular sieve adsorption bed T4-2 are both connected with a hot material inlet of a mash preheater E2, the second discharge port of the No. 1 molecular sieve adsorption bed T4-1 and the second discharge port of the No. 2 molecular sieve adsorption bed T4-2 are both connected with a hot material inlet of a regeneration gas condenser E11, the hot material outlet of the regeneration gas condenser E11 is connected with the feed inlet of a weak liquor recovery tank V5, the discharge port of the weak liquor recovery tank V5 is connected with the feed port of a crude liquor filter F2, the filtrate discharge port of the crude liquor filter F2 is respectively connected with the cold charge inlet of a first preheater E7 of a first rectification tower and the connecting cold charge inlet of a second preheater E8 of the first rectification tower, and the cold charge outlet of the first rectifying tower preheater E7 and the connecting cold charge outlet of the second rectifying tower preheater E8 are both connected with the tower side feed inlet of the first rectifying tower T2.
The hot material outlet of the rectifying tower kettle reboiler E9 and the hot material outlet of the ethanol steam superheater E10 are both connected with the feed inlet of a condensate tank V6, the discharge port of the condensate tank V6 is connected with the hot material inlet of a rectifying tower second preheater E8, and the hot material outlet of the rectifying tower second preheater E8 is connected with the hot material inlet of a rectifying tower second preheater E13.
The process comprises the following steps:
s1 and fermentation liquor S1 are preheated by a crude tower top heat exchanger E1 and a mash preheater E2 to become S2 and enter a crude distillation tower T1, a part of tower top gas S4 enters a crude tower top heat exchanger E1 to be used as a part of heat source for preheating S1, a part of the tower top gas enters a crude distillation tower cooler E3 to be condensed, a cold source of the crude distillation tower cooler E3 is external cooling water, a condensed liquid obtained after condensation of the tower top gas S4 enters a crude distillation tower reflux tank V1, after non-condensable gas is discharged from a crude distillation tower reflux tank V1, the condensed liquid S5 is totally refluxed to the crude distillation tower T1, waste mash at the bottom of the crude distillation tower T1 is sent to be centrifugally separated, S3 and S6 materials are collected from a side line, S3 enters a light liquor recovery tank V5, and S6 enters a first secondary tower first preheater E6 and a second preheater E6 of a rectification tower to become S6 to be preheated to become S6.
S2 and S7 enter a second rectification tower T3 to be rectified, waste mash S11 extracted from the tower bottom supplies heat source to a first preheater E5 of the second rectification tower and then is sent to be centrifugally separated, S12 extracted from the side line of the second rectification tower T3 is filtered out by a filter F1 to obtain solid, filtrate becomes a part of S15 and then enters a first rectification tower T2, tower top gas is divided into two S8 and S9, S8 supplies heat source to a reboiler E4 of a tower kettle of a crude rectification tower and then is condensed and then enters a reflux tank V2 of the second rectification tower, non-condensable gas is discharged from the reflux tank V2 of the second rectification tower, condensate S10 is refluxed to the second rectification tower T3, S9 is heated by an ethanol steam superheater E10 to obtain superheated steam which becomes S23 and then enters a molecular sieve adsorption bed T4-1 or T4-2.
S3 and S15 enter a first rectification tower T2, overhead gas S16 provides a heat source for a second rectification tower kettle reboiler E6, the condensed overhead gas enters a first rectification tower reflux tank V3 after being condensed, condensed liquid in V3 is divided into S17 and S18 which flow out, S17 enters a second rectification tower T3, S18 reflows to the first rectification tower T2, water S19 produced at the bottom of the first rectification tower T2 provides a heat source for the first rectification tower E7 and is condensed to become S20 which is sent back to a powder slurry liquefaction unit, a fusel oil by-product S22 and a fusel oil by-product S27 are separated from the fusel oil extraction tank V4 after the fusel oil solution S21 produced at the side of the first rectification tower T2 is condensed by a fusel oil cooler E12, the S27 is sent to a light alcohol recovery tank V5, and a cold source of the fusel oil cooler E12 is external cooling water.
S4, ethanol overheating S23 enters a molecular sieve adsorption bed T4-1 or T4-2 and is dehydrated to form fuel ethanol S24, S24 provides a heat source for a mash preheater E2 and is condensed to form a fuel ethanol product which is sent to a product tank area, low-concentration ethanol S25 steam separated from the molecular sieve adsorption bed T4-1 or T4-2 is condensed to form S26 through a regeneration gas condenser E11 and is sent to a light wine recovery tank V5, a cold source of the regeneration gas condenser E11 is external cooling water, low-concentration ethanol solution S13 in the light wine recovery tank V5 flows out to enter a crude wine filter F2 and is filtered to form S14, and S14 is rectified to form a part of S15 after being respectively preheated by a first tower first preheater E7 and a first rectifying tower E8 and then enters a first tower T2.
S5, low-pressure steam provides heat sources for a rectifying first tower kettle reboiler E9 and an ethanol steam superheater E10, condensate is formed and enters a condensate tank V6, condensate flowing out of the condensate tank V6 provides heat sources for a rectifying first tower second preheater E8 and then provides heat sources for a rectifying second tower second preheater E13, and then the condensate is out of the way.
The technical solution of the present invention is described in detail below with reference to specific examples and drawings, but the scope of the present invention is not limited to the examples.
Example 1
An energy-saving process for producing fuel ethanol by purifying fermentation liquor, which takes 10 ten thousand tons of fuel ethanol per year of industrial device as an example to further explain the technology of the invention. Referring to FIG. 1, the mass flow rate of the fermentation broth S1 is 104 t/h, wherein the mass concentration of ethanol is 12.09%. Has the following composition:
the operating conditions of the crude distillation column T1 were as follows: the tower top temperature: 52 ℃; pressure at the top of the column: -0.07 MPaG; temperature at the bottom of the column: 83 ℃; containing 35 theoretical plates, total reflux. The mass flow of fermentation liquor S1 is 104T/h, the fermentation liquor S1 is preheated by a crude tower top heat exchanger E1 and a mash preheater E2 to become S2, the S2 enters a crude distillation tower T1 from a 15 th tray, a part of overhead gas S4 enters a crude tower top heat exchanger E1 to be used as a part of heat source for preheating S1, a part of the overhead gas enters a crude distillation tower cooler E3 to be condensed, a cold source of E3 is external cooling water, a condensate after condensation of the overhead gas S4 enters a crude distillation tower reflux tank V1, a condensate S5 is totally refluxed to the crude distillation tower T1 after non-condensable gas is discharged from the crude distillation tower reflux tank V1, S5 and S5 are all refluxed to the crude distillation tower T1, the mass flow of S5 is 12T/h, waste mash at the bottom of the crude distillation tower T5 is sent to be centrifugally separated, two streams of S5 and S5 are respectively collected at the positions of side lines of a theoretical plate 14 and a 16 side line, the rectification tower T5 and S5 and enters a second preheater E5 to become a second preheater S5, the mass flow rate of S6 is 70 t/h, and the mass concentration of S6 ethanol is 12.3%.
The operating conditions of the rectification second column T3 are as follows: the tower top temperature: 92 ℃; pressure at the top of the column: 0.07 MPaG; temperature at the bottom of the column: 119 ℃; containing 55 theoretical plates, molar reflux ratio 1.1. S7 has mass flow of 70T/h, S7 ethanol has mass concentration of 12.3%, S7 enters a second rectifying tower T3 from a 35 th tray and is rectified, waste mash S11 extracted from the tower bottom provides a heat source for a first preheater E5 of the second rectifying tower and is sent to centrifugal separation, the second rectifying tower T3 extracts S12 from a side line of a first tray 37 and passes through a filter F1 to filter out solid, filtrate becomes a part of S15 and enters a first rectifying tower T2, S12 has mass flow of 11T/h, S12 has ethanol mass concentration of 9.8%, gas at the top is divided into two parts of S8 and S9, S8 has mass flow of 18.5T/h, S8 has ethanol mass concentration of 92.38%, S8 provides a heat source for a crude tower kettle E8 and enters a second rectifying tower reflux tank V8 after condensation, the condensate enters a superheater 8 of the second rectifying tower reflux tank V8 after discharging noncondensed gas, the S8 returns to a superheated steam absorption bed S8 or a superheated steam absorption sieve 8 to S8, the mass flow rate of S9 is 16.8t/h, and the mass concentration of S9 ethanol is 92.38%.
The operating conditions of the rectification column T2 are as follows: the tower top temperature: 126 ℃; pressure at the top of the column: 0.42 MPaG; temperature at the bottom of the column: 156 ℃; containing 41 theoretical plates, the molar reflux ratio was 3.2. S15 enters a first rectification tower T2 from a 25 th plate, S15 mass flow is 24.2T/h, S15 ethanol mass concentration is 33.42%, a top gas S16 provides a heat source for a second rectification tower kettle reboiler E6 and is condensed and then enters a first rectification tower reflux tank V3, condensate in the first rectification tower reflux tank V3 is divided into two parts of S17 and S18 to flow out, S17 enters a second rectification tower T3 from the top of the tower, S3 mass flow is 9T/h, S3 ethanol mass concentration is 91.92%, S3 returns to the first rectification tower T3, S3 mass flow is 28T/h, S3 ethanol mass concentration is 91.92%, produced water at the bottom of the first rectification tower T3 provides a heat source for the first rectification tower E3 to be condensed and is sent to a powder slurry liquefaction unit, the first rectification tower T3 produces a fusel oil solution, and a side alcohol extraction solution is separated from the S3 and a side alcohol extraction liquid S3 by-side cooling tank S3 to obtain a byproduct S3. The mass flow of S21 is 1 t/h, the mass concentration of S21 ethanol is 11%, S27 is sent to a light wine recovery tank V5, and the cold source of the fusel oil cooler E12 is external cooling water.
Ethanol overheating S23 enters a molecular sieve adsorption bed T4-1 or T4-2 and is dehydrated to form fuel ethanol S24, the molecular sieve adsorption bed T4-1 and T4-2 are operated in parallel, while one adsorption bed adsorbs water to produce fuel ethanol, the other adsorption bed desorbs low-concentration weak liquor steam to regenerate a molecular sieve, the mass flow rate of S24 is 12.6T/h, the mass concentration of S24 ethanol is 99.96%, S24 provides a heat source for mash preheater E2 and is condensed to form a fuel ethanol product which is sent to a product tank area, the low-concentration ethanol S25 steam separated from the molecular sieve adsorption bed T4-1 or T4-2 is condensed to form S26 which is sent to a weak liquor recovery tank V5 by a regeneration gas condenser E11, a cold source of the regeneration gas condenser E9 is external cooling water, the low-concentration ethanol solution S13 in the weak liquor recovery tank V5 flows out to enter a crude liquor F2 to be filtered to form S14, and the S14 passes through a first rectification tower and a first rectification tower 7E 15 to form a first rectification tower S8 and a second rectification tower S15 Enters a rectification tower T2.
Low-pressure steam provides heat sources for a rectifying first tower kettle reboiler E9, an ethanol steam superheater E10 and a molecular sieve adsorption bed superheater, then condensate is formed and enters a condensate tank V6, and the condensate flowing out of the condensate tank V6 provides heat sources for a rectifying first tower second preheater E8 and then provides heat sources for a rectifying second tower second preheater E13, and then the condensate enters the boundary. The heat exchange amounts of a rectifying tower kettle reboiler E9, an ethanol steam superheater E10 and a molecular sieve adsorption bed superheater are 9277 kW, 264 kW and 40 kW respectively, 17.2 t/h is needed in conversion into steam, and 1.37 t of steam is needed in each ton of fuel ethanol products. The rest heat exchange is carried out by utilizing the heat of the material flow strand in the system or steam condensate.
Example 2
An energy-saving process for producing fuel ethanol by purifying fermentation liquor takes 30 ten thousand tons of fuel ethanol per year of industrial device as an example to further explain the technology of the invention. Referring to FIG. 1, the mass flow rate of S1 was 208 t/h, wherein the ethanol concentration was 15.0% by mass. Has the following composition:
the operating conditions of the crude distillation column T1 were as follows: the tower top temperature: 52 ℃; pressure at the top of the column: -0.07 MPaG; temperature at the bottom of the column: 83 ℃; containing 35 theoretical plates, total reflux. The mass flow of fermentation liquor S1 is 313T/h, the fermentation liquor S1 is preheated by a crude tower top heat exchanger E1 and a mash preheater E2 to become S2, the S2 enters a crude distillation tower T1 from a 15 th tray, a part of overhead gas S4 enters a crude tower top heat exchanger E1 to be used as a part of heat source for preheating S1, a part of the overhead gas enters a crude distillation tower cooler E3 to be condensed, a cold source of E3 is external cooling water, a condensate after condensation of the overhead gas S4 enters a crude distillation tower reflux tank V1, a condensate S5 is totally refluxed to the crude distillation tower T1 after discharge of non-condensable gas from the crude distillation tower reflux tank V1, the S5 is completely refluxed to the crude distillation tower T1, the mass flow of S5 is 36T/h, waste mash at the bottom of the crude distillation tower T5 is sent to centrifugal separation, S5 and S5 are respectively collected at the positions of a side line 14 and 16 trays and enter a second rectification tower E5 to become a second preheater, S5 and a second preheater E5, the mass flow rate of S6 is 211 t/h, and the mass concentration of S6 ethanol is 16.2%.
The operating conditions of the rectification second column T3 are as follows: the tower top temperature: 92 ℃; pressure at the top of the column: 0.07 MPaG; temperature at the bottom of the column: 119 ℃; containing 55 theoretical plates, molar reflux ratio 1.1. S7 mass flow is 211T/h, S7 ethanol mass concentration is 16.2%, S7 enters a second rectification tower T3 from a 35 th tray and is rectified, waste mash S11 extracted from the tower bottom provides a heat source for a first preheater E5 of the second rectification tower and is sent to centrifugal separation, the second rectification tower T3 extracts S12 from a side line of a first plate 37 and passes through a filter F1 to filter out solid, filtrate becomes a part of S15 and enters a first rectification tower T2, S12 mass flow is 34T/h, S12 ethanol mass concentration is 17.4%, top gas is divided into two S12 and S12, S12 mass flow is 67.3T/h, S12 ethanol mass concentration is 12%, S12 provides a heat source for a crude distillation tower bottom E12 and enters a second rectification tower reflux tank V12 after condensation, S12 returns to a superheated steam adsorption tower T12 after non-condensable gas is discharged from the second rectification tower reflux tank V12, S12 returns to a superheated steam adsorption tower 12 and is heated to a molecular sieve 12 or a superheated steam adsorption tower 12 to obtain S12-12, the mass flow rate of S9 is 60.9 t/h, and the mass concentration of S9 ethanol is 92.37%.
The operating conditions of the rectification column T2 are as follows: the tower top temperature: 126 ℃; pressure at the top of the column: 0.42 MPaG; temperature at the bottom of the column: 156 ℃; containing 41 theoretical plates, molar reflux ratio 2.8. S15 enters a first rectification tower T2 from a 27 th plate, the mass flow of S15 is 74.9T/h, the mass concentration of S15 ethanol is 39.07%, overhead gas S16 provides a heat source for a second rectification tower reboiler E6, the condensed gas enters a first rectification tower reflux tank V3 after being condensed, the condensed liquid in the first rectification tower reflux tank V3 is divided into two parts of S17 and S18 to flow out, S17 enters a second rectification tower T3 from the top of the tower, the mass flow of S17 is 30.5T/h, the mass concentration of S17 ethanol is 91.81%, S18 returns to the first rectification tower T2, the mass flow of S2 is 85.3T/h, the mass concentration of S2 ethanol is 91.81%, the bottom water S2 of the first rectification tower T2 provides a heat source for the first rectification tower E2 to be condensed and then is sent to a powder slurry liquefaction unit, the first rectification tower T2 recovers a side-liquid and a side alcohol condensate is separated from a mixed oil condensate tank S2 after the S2 side-draw oil condensate is separated from a S2 by a plate S2. The mass flow of S21 is 3 t/h, the mass concentration of S21 ethanol is 42.67%, S27 is sent to a weak liquor recovery tank V5, and the cold source of the fusel oil cooler E12 is external cooling water.
Ethanol overheating S23 enters a molecular sieve adsorption bed T4-1 or T4-2 and is dehydrated to form fuel ethanol S24, the molecular sieve adsorption bed T4-1 and T4-2 are operated in parallel, while one adsorption bed adsorbs water to produce fuel ethanol, the other adsorption bed desorbs low-concentration weak liquor steam to regenerate a molecular sieve, the mass flow rate of S24 is 46.4T/h, the mass concentration of S24 ethanol is 99.96%, S24 provides a heat source for mash preheater E2 and is condensed to form a fuel ethanol product which is sent to a product tank area, the low-concentration ethanol S25 steam separated from the molecular sieve adsorption bed T4-1 or T4-2 is condensed to form S26 which is sent to a weak liquor recovery tank V5 by a regeneration gas condenser E11, a cold source of the regeneration gas condenser E9 is external cooling water, the low-concentration ethanol solution S13 in the weak liquor recovery tank V5 flows out to enter a crude liquor F2 to be filtered to form S14, and the S14 passes through a first rectification tower and a first rectification tower 7 and a second rectification tower S15 Enters a rectification tower T2.
Low-pressure steam provides heat sources for a rectifying first tower kettle reboiler E9, an ethanol steam superheater E10 and a molecular sieve adsorption bed superheater, then condensate is formed and enters a condensate tank V6, and the condensate flowing out of the condensate tank V6 provides heat sources for a rectifying first tower second preheater E8 and then provides heat sources for a rectifying second tower second preheater E13, and then the condensate enters the boundary. The heat exchange amounts of a rectifying tower kettle reboiler E9, an ethanol steam superheater E10 and a molecular sieve adsorption bed superheater are 29324 kW, 959 kW and 150 kW respectively, and as the circulation amount is increased, the heat exchange amounts of 4019 kW are required to be supplemented for other heat exchange besides heat exchange by using material flow stock heat or steam condensate in the system, the conversion into steam requires 61.8 t/h, and each ton of fuel ethanol product requires 1.33 tons of steam.
The above description is only an embodiment of the present invention, and not intended to limit the scope of the present invention, and all equivalent structures made by using the contents of the present specification and the drawings can be directly or indirectly applied to other related technical fields, and are within the scope of the present invention.
Claims (7)
1. An energy-saving device for producing fuel ethanol by purifying fermentation liquor is characterized by comprising: a crude distillation tower (T1), a first rectification tower (T2), a second rectification tower (T3), a # 1 molecular sieve adsorption bed (T4-1) and a # 2 molecular sieve adsorption bed (T4-2), a crude overhead heat exchanger (E1), a mash liquid preheater (E2), a crude distillation tower cooler (E3), a crude distillation tower kettle reboiler (E4), a first rectification tower preheater (E5), a second rectification tower kettle reboiler (E6), a first rectification tower preheater (E7), a first rectification tower second preheater (E8), a first rectification tower kettle reboiler (E9), an ethanol vapor superheater (E10), a regenerated gas condenser (E11), a fusel oil cooler (E12), a second rectification tower preheater (E13), a crude distillation tower reflux tank (V1), a second rectification tower reflux tank (V2), a first rectification tower reflux tank (V2), a fusel oil extraction tank (V4), a light distillate recovery tank (V8653) and a V8427, A filter (F1) and a crude wine filter (F2);
the top gas port of the crude distillation tower (T1) is respectively connected with a hot material inlet of a crude distillation tower top heat exchanger (E1) and a hot material inlet of a crude distillation tower cooler (E3), the reflux port of the crude distillation tower (T1) is connected with a discharge port of a crude distillation tower reflux tank (V1), a hot material outlet of the crude distillation tower top heat exchanger (E1) and a hot material outlet of a crude distillation tower cooler (E3) are both connected with a feed port of a crude distillation tower reflux tank (V1), a cold material outlet of the crude distillation tower top heat exchanger (E1) is connected with a cold material inlet of a mash preheater (E2), a cold material outlet of the mash preheater (E2) is connected with a side tower feed port of the crude distillation tower (T1), a first side collecting port of the crude distillation tower (T1) is connected with a feed port of a light liquor recovery tank (V5), a second side collecting port of the crude distillation tower (T1) is respectively connected with a first cold material inlet of a second rectifying tower (E3985) and a second collecting tower inlet of the crude distillation tower (E3985), the cold charge outlet of the second preheater (E13) of the second rectifying tower and the cold charge outlet of the first preheater (E5) of the second rectifying tower are both connected with the tower side feed inlet of the second rectifying tower (T3);
the top gas port of the rectifying tower (T3) is respectively connected with the hot material inlet of a reboiler (E4) at the bottom of the crude distillation tower and the cold material inlet of an ethanol vapor superheater (E10), the cold charge outlet of the ethanol vapor superheater (E10) is respectively connected with the feed inlet of a 1# molecular sieve adsorption bed (T4-1) and the feed inlet of a 2# molecular sieve adsorption bed (T4-2), the hot material outlet of the crude distillation tower kettle reboiler (E4) is connected with the feed inlet of a second rectification tower reflux tank (V2), the discharge hole of the rectification second tower reflux tank (V2) is connected with the reflux hole of the rectification second tower (T3), a tower bottom material extraction outlet of the second rectifying tower (T3) is connected with a hot material inlet of a first preheater (E5) of the second rectifying tower, the side extraction port of the rectifying second tower (T3) is connected with the feed port of a filter (F1), the filtrate discharge port of the filter (F1) is connected with the side feed port of the first rectification tower (T2);
the top gas port of the rectifying tower I (T2) is connected with the hot material inlet of a rectifying tower II reboiler (E6), the hot material outlet of the rectifying tower II reboiler (E6) is connected with the feed inlet of a rectifying tower I reflux tank (V3), the discharge port of the rectifying tower I reflux tank (V3) is respectively connected with the reflux port of a rectifying tower I (T2) and the top feed port of a rectifying tower II (T3), the bottom material discharge port of the rectifying tower I (T2) is connected with the hot material inlet of a rectifying tower I preheater (E7), the side draw port of the rectifying tower I (T2) is connected with the hot material inlet of a fusel oil cooler (E12), the hot material outlet of the fusel oil cooler (E12) is connected with the feed inlet of a fusel oil extraction tank (V4), and the discharge port of the bottom of the fusel oil extraction tank (V4) is connected with the feed inlet of a light wine recovery tank (V5);
the first discharge port of the 1# molecular sieve adsorption bed (T4-1) and the first discharge port of the 2# molecular sieve adsorption bed (T4-2) are connected with a hot material inlet of a mash preheater (E2), the second discharge port of the 1# molecular sieve adsorption bed (T4-1) and the second discharge port of the 2# molecular sieve adsorption bed (T4-2) are connected with a hot material inlet of a regeneration gas condenser (E11), a hot material outlet of the regeneration gas condenser (E11) is connected with a feed port of a light wine recovery tank (V5), a discharge port of the light wine recovery tank (V5) is connected with a feed port of a crude wine filter (F2), a filtrate discharge port of the crude wine filter (F2) is respectively connected with a cold material inlet of a first preheater (E7) of a rectification tower and a cold material inlet of a second preheater (E8) of the rectification tower, and a cold material outlet of the first preheater (E7) of the rectification tower and a cold material outlet of the second preheater (E3874) of the rectification tower are respectively connected with a cold material inlet of the second preheater (E8) of the rectification tower The tower side feed inlets of the rectification tower I (T2) are connected;
the hot material outlet of the rectifying tower kettle reboiler (E9) and the hot material outlet of the ethanol steam superheater (E10) are connected with the feed inlet of a condensate tank (V6), the discharge port of the condensate tank (V6) is connected with the hot material inlet of a rectifying tower second preheater (E8), and the hot material outlet of the rectifying tower second preheater (E8) is connected with the hot material inlet of a rectifying tower second preheater (E13).
2. An energy-saving process based on the energy-saving device of claim 1, characterized by comprising the following steps:
s1, preheating fermentation liquor, feeding the preheated fermentation liquor into a rough distillation tower (T1), condensing overhead gas, discharging non-condensable gas, then completely refluxing, sending waste mash at the bottom of the tower to centrifugal separation, collecting two materials at a lateral line, feeding one material into a rectification second tower (T3) and feeding the other material into a light wine recovery tank (V5);
s2, after the material entering a second rectifying tower (T3) is rectified, waste mash extracted from the bottom of the second rectifying tower (T3) is sent to be centrifugally separated, the side line is extracted, solid is filtered out, then filtrate enters a first rectifying tower (T2), a first tower top gas is condensed, non-condensable gas is discharged and then flows back, and a first tower top gas is continuously heated into superheated steam to enter a molecular sieve adsorption bed;
s3, preheating the filtrate obtained by filtering the filtrate obtained by the side of the rectifying tower and the filtrate obtained by filtering solids in a light liquor recovery tank, mixing the preheated filtrate and entering a rectifying tower I (T2), condensing the gas at the top of the rectifying tower I (T2) to obtain reflux, returning the reflux to the rectifying tower II (T3), returning the produced water at the bottom of the rectifying tower to a powder slurry liquefaction unit, condensing the fusel solution obtained at the side of the rectifying tower, separating a fusel oil byproduct and a fusel liquid from a fusel oil extraction tank (V4), and sending the fusel liquid to a light liquor recovery tank (V5);
and S4, dehydrating the steam in a molecular sieve adsorption bed, condensing the ethanol steam at the top of the tower to obtain a fuel ethanol product, and condensing the separated low-concentration ethanol steam and then sending the condensed low-concentration ethanol steam into a light wine recovery tank (V5).
3. The energy saving process of claim 2, wherein in S1, the heat source for preheating the fermentation liquid is the top gas of a crude distillation column (T1) and the top gas of a molecular sieve adsorption bed; the heat source of the reboiler (E4) at the bottom of the crude distillation tower is top gas of a rectification secondary tower (T3), the top gas of the crude distillation tower (T1) is-0.1 to-0.01 MPaG, the temperature of the bottom of the tower is 70 to 90 ℃, and the temperature of the top of the tower is 40 to 60 ℃.
4. The energy-saving process as claimed in claim 2, wherein in S2, part of the preheating heat source of the feed of the second rectifying tower (T3) is the bottom liquid of the second rectifying tower (T3), the heat source of the reboiler (E6) of the second rectifying tower is the top gas of the first rectifying tower (T2), the temperature of the tower bottom is 100-130 ℃, and the temperature of the top liquid is 80-120 ℃.
5. The energy-saving process according to claim 2, wherein in S3, a part of a heat source for preheating the effluent of the weak liquor recovery tank (V5) after filtration is a bottom liquid of a rectification tower (T2); the top pressure of the rectifying tower (T2) is 0.05-0.5MPaG, the temperature of the tower bottom is 140-170 ℃, and the extraction temperature of the tower top is 110-140 ℃.
6. The energy saving process as claimed in claim 2, wherein the heat source of the reboiler (E9) of the rectifying tower-one tower is external steam, the heat source of the overhead gas of the rectifying tower (T3) is external steam, the condensate of the two streams is sent to the condensate tank (V6), the condensate flowing out of the condensate tank (V6) is used as the heat source to be used as the supplementary heat source of the effluent of the light liquor recovery tank (V5) and the feed of the rectifying tower (T3).
7. The energy-saving process as claimed in claim 2, wherein the partial cold source of the top gas of the crude distillation column (T1), the cold source of the fusel solution taken out from the side line of the rectification column (T2) and the cold source of the light wine vapor taken out from the molecular sieve adsorption bed are all external cooling water.
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