CN115636728B - Treatment method of cellulose ethanol fermentation mash and preparation method of cellulose fuel ethanol - Google Patents
Treatment method of cellulose ethanol fermentation mash and preparation method of cellulose fuel ethanol Download PDFInfo
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- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 title claims abstract description 240
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- 238000000034 method Methods 0.000 title claims abstract description 38
- 239000000446 fuel Substances 0.000 title claims abstract description 21
- 238000002360 preparation method Methods 0.000 title claims abstract description 9
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- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 58
- 238000000926 separation method Methods 0.000 claims abstract description 46
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- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 11
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Classifications
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
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- Preparation Of Compounds By Using Micro-Organisms (AREA)
Abstract
The invention discloses a treatment method of cellulose ethanol fermentation mash and a preparation method of cellulose fuel ethanol. The treatment method comprises the steps of adopting a mash tower to treat cellulose ethanol fermentation mash; the bottom of the mash tower is provided with a reboiler, the lower part is provided with a material inlet, the inside is provided with a multi-stage tower plate, and the top of the tower is provided with a membrane separation dehydrator; the processing method comprises the following steps: 1) Feeding the cellulose ethanol fermentation mash into the lower part of a mash tower through a material inlet; 2) Heating the cellulose ethanol fermentation mash by a reboiler at the bottom of the mash tower, and gradually rising the vapor-liquid mixture to pass through a tower plate; 3) A mixture side offtake of water and ethanol; 4) The gas phase material comprising water and CO 2 is separated by a membrane separation dehydrator at the top of the mash tower. By applying the technical scheme of the invention, most of water is removed by the membrane separation dehydrator, so that the concentration of ethanol is multiplied, and ethanol fermentation mash is separated into water, high-concentration ethanol and solid residues, thereby reducing the energy consumption of rectification.
Description
Technical Field
The invention relates to the technical field of chemical industry, in particular to a treatment method of cellulose ethanol fermentation mash and a preparation method of cellulose fuel ethanol.
Background
The energy is the motive power for producing world material data, and biomass energy is used as a novel biological energy source, and has the advantages of reproducibility, low pollution and the like. The fuel ethanol is used as an alternative energy source, can be applied to the traffic industry, creates employment opportunities, improves urban air quality and reduces emission of greenhouse gases.
The current fuel ethanol production technology mainly comprises a first generation technology and a second generation technology. The first generation of fuel ethanol technology is to produce ethanol from sugar and starch crops as raw materials. The main production procedures comprise: liquefaction, saccharification, fermentation, distillation and dehydration. The second generation fuel ethanol is produced by using lignocellulose (crop straw and the like) as a raw material (mainly comprising cellulose, hemicellulose and lignin), namely, the cellulose ethanol. The main production procedures comprise: raw material pretreatment, cellulose and hemicellulase hydrolysis saccharification, fermentation ethanol production and distillation dehydration. Compared with the first generation technology, the second generation fuel ethanol technology firstly carries out pretreatment, namely delignification is carried out, the looseness of the raw materials is increased, the contact between cellulose and cellulose is increased, and the enzymolysis efficiency is improved; after the raw materials are decomposed into fermentable sugars, the fermentable sugars are fermented, distilled and dehydrated. The second generation of cellulose ethanol has the raw material advantage of 'no competition with grain and no competition with land', and is the future development direction of biofuel ethanol.
The traditional cellulose fuel ethanol rectification process is double-tower rectification, and the fresh steam consumption of the produced 1t fuel ethanol product in a rectification unit is 2.2 to 2.5t. The cellulose ethanol fermentation mash contains byproducts and impurities such as solid residues, water, CO 2, aldehydes, acids, fats, sulfates and the like, and in order to obtain qualified ethanol products and recycle byproducts, the traditional technology is as follows: ethanol fermentation mash is subjected to solid-liquid separation, rectification and molecular sieve adsorption to produce ethanol with the purity of 99.5% (volume fraction), water and solid residues. Distillation is carried out in two columns. The first, called the beer column, separates the dissolved CO 2 and most of the water. The second, called the rectifying column, is used to concentrate the ethanol to an azeotrope state. The ethanol product was concentrated to about 92.5% (volume fraction) after leaving the rectifying column, and then further dehydrated and concentrated to 99.5% (volume fraction) by adsorption through a gas phase molecular sieve. During regeneration of the absorption column, the low concentration (70% (volume fraction)) ethanol vapor produced is recycled back to the distillation column for recovery. The vapor at the top of the beer column and the aeration of the fermentor (mainly CO 2, also some ethanol) are sent to a water scrubber where the vast majority of the ethanol is recovered. The sewage from the water washer is returned to the mash. The bottom stream of the beer column contains unconverted soluble and insoluble materials. The insoluble materials are dehydrated by using a plate-and-frame filter press and then sent to a combustion furnace of a solid waste incineration and power generation section. The water after press filtration cannot be directly recycled because it contains high concentrations of organic salts, nutrients not utilized by the microorganisms and soluble inorganic parts of the biomass. Wherein the key step is to carry out crude distillation separation on the mash obtained by fermentation.
In the production process of the cellulose fuel ethanol, the mass fraction of fermentation mash is low (about 5% -6%), the energy consumption required by rectification is high, and the high energy consumption becomes an important reason for restricting the industrialization of the cellulose fuel ethanol. Due to higher energy consumption, the traditional double-tower rectification is gradually replaced by a three-tower rectification process. Scientific researchers at Beijing university Yang Jing and the like have studied "cellulose fuel ethanol three-tower rectification optimization technique" (Beijing university Yang Jing and the like, cellulose fuel ethanol three-tower rectification optimization [ J ]. Cellulose science and technology, 2016,24 (02): 60-64; 76.). Based on Aspen plus software, a calculation model of a cellulose ethanol three-tower rectification process is established, a material and energy balance result is obtained by adopting an NRTL activity coefficient model, a crude tower, an atmospheric tower and a pressurizing tower are respectively optimized, the influence rules of parameters such as the theoretical plate number of each tower, the feeding position, the reflux ratio and the like on the reboiler load of each tower are obtained, and the comprehensive energy consumption is minimized by optimizing each influence parameter. The three-tower rectification process of the cellulose fuel ethanol is that fermentation mature mash is heated to a bubble point by a mature mash 1# preheater and a mature mash 2# preheater to enter the upper part of a crude tower. Crude alcohol is extracted from the top of the tower, the crude alcohol is partially condensed by heat exchange between the mature mash No. 1 preheater and the raw material, the non-condensed gas phase is recovered in a washing tower, the condensed liquid and the side line liquid phase of the crude tower are used for extracting light alcohol, and the bottom liquid of the washing tower are combined, and then the mixture is heated to the bubble point by a feeding preheater of a normal pressure tower and enters the middle lower part of the normal pressure tower. And the produced liquid at the bottom of the crude tower is subjected to heat recovery through a mature mash No. 2 preheater and then is decontaminated into a water treatment system. The coarse tower is operated under negative pressure, mainly discharges noncondensable gas and a large amount of water, the tower top wine gas is condensed by a condenser, and the noncondensable gas is discharged after ethanol is recovered by a washing tower. And collecting condensate and tower bottom liquid of the washing tower, and then entering the atmospheric tower. The energy consumption of the rectifying unit is high, and the energy consumption of the rectifying unit accounts for 60-70% of the total energy consumption of the whole production. The low-energy-consumption rectification becomes a key technology and has great significance for reducing the production cost.
Disclosure of Invention
The invention aims to provide a treatment method of cellulose ethanol fermentation mash and a preparation method of cellulose fuel ethanol, which are used for solving the technical problem of high energy consumption in preparation and rectification of cellulose fuel ethanol in the prior art.
In order to achieve the above object, according to one aspect of the present invention, there is provided a method for treating cellulosic ethanol fermentation broth. The treatment method comprises the steps that cellulose ethanol fermentation mash is treated by a mash tower; the bottom of the mash tower is provided with a reboiler, the lower part is provided with a material inlet, the inside is provided with a multi-stage tower plate, and the top of the tower is provided with a membrane separation dehydrator; the processing method comprises the following steps: 1) Feeding the cellulose ethanol fermentation mash into the lower part of a mash tower through a material inlet; 2) Heating the cellulose ethanol fermentation mash by a reboiler at the bottom of the mash tower, and gradually rising the vapor-liquid mixture to pass through a tower plate; 3) A mixture side offtake of water and ethanol; 4) The gas phase material comprising water and CO 2 is separated by a membrane separation dehydrator at the top of the mash tower.
Further, the gas phase material separated by the membrane separation dehydrator at the top of the mash tower enters a condenser, wherein CO 2 is recovered as non-condensable gas, and the condensed water is recycled.
Further, the separation membrane in the membrane separation dehydrator is an inorganic membrane or an organic membrane.
Further, the inorganic membrane is a molecular sieve membrane.
Further, the mash tower is provided with 20-50 tower plates; feeding from the 2 nd to 10 th plates at the top of the tower.
Further, the top pressure of the mash tower is 1.5-2.5 atm.
Further, the mixture of water and ethanol is laterally extracted from the 11 th to 20 th trays.
According to another aspect of the present invention, a method for preparing cellulosic fuel ethanol is provided. The preparation method comprises the step of treating the cellulose ethanol fermentation mash, wherein the treatment of the cellulose ethanol fermentation mash is carried out by adopting any one of the treatment methods of the cellulose ethanol fermentation mash.
Further, the mixture of water and ethanol which are extracted from the side line enters a second rectifying tower for further rectification.
By applying the technical scheme of the invention, a rectification and membrane separation dehydration combined system is established, wherein a membrane separation dehydrator removes most of water, so that the concentration of ethanol is multiplied, and ethanol fermentation mash is separated into water, high-concentration ethanol and solid residues, thereby reducing the energy consumption of rectification. Compared with the traditional rectification and adsorption technology, the method can save energy by 15-30%; any third component is not introduced or generated in the process, so that the ethanol product and the environment are not polluted, and the method has the characteristics of energy conservation, environmental protection, simplicity in operation and the like.
Detailed Description
It should be noted that, without conflict, the embodiments of the present application and features of the embodiments may be combined with each other. The present application will be described in detail with reference to examples.
In order to solve the technical problems of low concentration of ethanol in fermentation mash and high distillation energy consumption in the prior art, the invention provides a method for treating cellulose ethanol fermentation mash by a rectification and membrane separation dehydration combination system, and the method can achieve the aim of reducing the rectification energy consumption after removing most of water by a membrane separation dehydrator and combining with a rectification tower.
According to an exemplary embodiment of the present application, a method for treating cellulosic ethanol fermentation broth is provided. The cellulosic ethanol fermentation mash is treated by a mash tower (also called a first rectifying tower in the application); the bottom of the mash tower is provided with a reboiler, the lower part is provided with a material inlet, the inside is provided with a multi-stage tower plate, and the top of the tower is provided with a membrane separation dehydrator; the processing method comprises the following steps: 1) Feeding the cellulose ethanol fermentation mash into the lower part of a mash tower through a material inlet; 2) Heating the cellulose ethanol fermentation mash by a reboiler at the bottom of the mash tower, and gradually rising the liquid mixture to pass through a tower plate; 3) A mixture side offtake of water and ethanol; 4) The vapor phase material comprising water and CO 2 is separated by a membrane separation dehydrator at the top of the beer column and most of the ethanol does not pass through.
By applying the technical scheme of the invention, a rectification and membrane separation dehydration combined system is established, wherein a membrane separation dehydrator removes most of water, so that the concentration of ethanol is multiplied, and ethanol fermentation mash is separated into water, high-concentration ethanol and solid residues, thereby reducing the energy consumption of rectification. Compared with the traditional rectification and adsorption technology, the method can save energy by 15-30%; any third component is not introduced or generated in the process, so that the ethanol product and the environment are not polluted, and the method has the characteristics of energy conservation, environmental protection, simplicity in operation and the like.
Preferably, the gas phase materials separated by the membrane separation dehydrator at the top of the mash tower enter a condenser, wherein CO 2 is recovered as non-condensable gas, and the condensed water is recycled, so that the effective utilization of resources is fully realized.
The membrane is an inorganic or high molecular material with special selective separation function, and can separate fluid into two non-communicated parts so that one or more substances can permeate and other substances can be separated. The membrane can be separated in the molecular range, and the process is a physical process, does not change phases and does not need addition of auxiliary agents. The inorganic film mainly includes a ceramic film and a metal film. The organic film is made of high molecular material, such as cellulose acetate, aromatic polyamide, polyether sulfone, polyfluoro polymer, etc. In the present invention, the separation membrane in the membrane separation dehydrator may be an inorganic membrane or an organic membrane.
The membranes required for the membrane separation dehydrator in the present invention are required to have high permeation flux, high water selectivity and stability, and preferably molecular sieve membranes. Molecular sieve membranes are a class of inorganic membrane materials with a regular micro-channel structure. The molecular sieve membrane is a novel separation membrane material with a molecular sieve function by taking porous ceramic tubes such as alumina and the like as a support, has compact, uniform and continuous molecular sieve membrane layers, has the characteristics of uniform pore diameter and hydrophilicity, has excellent selectivity on azeotropes formed by water and ethanol, and can lead water to pass preferentially. Under the pushing of the vapor partial pressure difference of the ethanol, the separation among the components is realized by utilizing the difference of the dissolution (adsorption) -diffusion rates of the ethanol and the water in the pore channels of the membrane and the difference of the molecular sizes, and the water is preferentially permeated.
According to an exemplary embodiment of the invention, the mash tower has 20-50 trays; feeding from the 2 nd to 10 th plates at the top of the tower. Preferably, the head pressure of the beer column is 1.5 to 2.5 atmospheres. Preferably, the mixture of water and ethanol is sidedraw from trays 11 to 20.
According to an exemplary embodiment of the present invention, the overhead CO 2 (75% to 90% by mass), ethanol (0.1% to 0.5% by mass), and water (10% to 24% by mass).
After passing through the condenser, all CO 2 and most of water are removed, most of ethanol (more than 99 percent) and water vapor form mixed gas phase with the concentration of 45 to 65 percent by mass, and the mixed gas phase is discharged from the side line of the 11 th to 20 th actual tower plates and enters the second rectifying tower through a pump.
According to an exemplary embodiment of the present invention, a method for preparing cellulosic fuel ethanol is provided. The preparation method comprises the step of treating the cellulose ethanol fermentation mash, wherein the treatment of the cellulose ethanol fermentation mash is carried out by adopting any one of the treatment methods of the cellulose ethanol fermentation mash. Preferably, the mixture of water and ethanol at the side draw is fed into a second rectifying tower for further rectification.
The advantageous effects of the present invention will be further described below with reference to examples.
Example 1
Rectification and membrane separation dehydration combined system
The cellulose ethanol fermentation mash 130t/h, wherein the solid is 15t/h and the ethanol is 8t/h, is pumped into the lower part of a mash tower, and is provided with 30 tower plates, and is fed from a 4 th tower plate at the top of the tower, and the pressure at the top of the tower is 1.8 atm. Heating the material by a reboiler at the bottom of the mash tower, and gradually rising the vapor-liquid mixture to pass through a tower plate; a membrane separation dehydrator is arranged at the top of the mash tower, a molecular sieve membrane is arranged in the membrane separation dehydrator, water and CO 2 pass through preferentially, vapor phase materials CO 2 (82.5% by mass fraction), ethanol (0.2% by mass fraction) and water (16% by mass fraction) enter a condenser after passing through the membrane separation dehydrator, and CO 2 is recycled as non-condensable gas, and the condensed water is recycled. Ethanol forms a mixed gas phase with water vapor at a concentration of 55% (mass fraction), and is discharged from the side line of the 12 th actual column plate. The energy consumption of the reboiler of the mash tower is 4.501 X10 7 kJ/h. The mixed gas of the ethanol and the water vapor extracted from the side line enters a second rectifying tower, the ethanol recovery rate is 98%, and the mass fraction of the ethanol in the final rectifying product is 94%. The reboiler energy consumption of the second rectification column was 8.017 X10 7 kJ/h.
Example 2 (comparative example)
Conventional rectification system
The cellulose ethanol fermentation mash 130t/h, wherein the solid is 15t/h and the ethanol is 8t/h, is pumped into the lower part of a mash tower, the tower is provided with 30 tower plates, the 4 th tower plate is fed from the top of the tower, and the pressure of the top of the tower is 1.8 atm. The materials are heated by a reboiler at the bottom of a mash tower, the vapor-liquid mixture is gradually increased to pass through a tower plate, the tower top distillate CO 2 (mass fraction 83%), ethanol (mass fraction 11.7%) and water (mass fraction 4%) enter a condenser, CO 2 is recycled as non-condensable gas, and the condensed water is recycled. Ethanol and water vapor form mixed gas phase at the concentration of 20.2% (mass fraction), and the mixed gas phase is discharged from the side line of the 12 th actual tower plate. The energy consumption of the reboiler of the mash tower is 5.338 X10 7 kJ/h. The mixed gas of the ethanol and the water vapor extracted from the side line enters a second rectifying tower, the ethanol recovery rate is 98%, and the mass fraction of the ethanol in the final rectifying product is 94%. The reboiler energy consumption of the second rectification column was 8.865 X10 7 kJ/h.
Example 3
Rectification and membrane separation dehydration combined system
The cellulose ethanol fermented mash is pumped into the lower part of a mash tower by a pump, 20 tower plates are arranged, the material is fed from the 2 nd tower plate at the top of the tower, and the pressure at the top of the tower is 1.5 atm. Heating the material by a reboiler at the bottom of the mash tower, and gradually rising the vapor-liquid mixture to pass through a tower plate; a membrane separation dehydrator is arranged at the top of a mash tower, an organic membrane of cellulose acetate is filled in the membrane separation dehydrator, water and CO 2 preferentially pass through the membrane separation dehydrator, after vapor phase materials pass through the membrane separation dehydrator, vapor phase materials CO 2 (mass fraction 75.7%), ethanol (mass fraction 0.3%) and water (mass fraction 24%) enter a condenser again, CO 2 is recycled as non-condensable gas, and the condensed water is recycled. Ethanol and water vapor form mixed gas phase at the concentration of 48% (mass fraction), and the mixed gas phase is discharged from the side line of the 11 th actual tower plate.
Example 4
Rectification and membrane separation dehydration combined system
The cellulosic ethanol fermented mash is pumped into the lower part of the mash tower by a pump, 50 trays are arranged, the 10 th tray at the top of the tower is fed, and the pressure at the top of the tower is 2.5 atm. Heating the material by a reboiler at the bottom of the mash tower, and gradually rising the vapor-liquid mixture to pass through a tower plate; a membrane separation dehydrator is arranged at the top of the mash tower, a molecular sieve membrane is arranged in the membrane separation dehydrator, water and CO 2 pass through preferentially, vapor phase materials CO 2 (89.9% by mass fraction), ethanol (0.1% by mass fraction) and water (10% by mass fraction) enter a condenser after passing through the membrane separation dehydrator, and CO 2 is recycled as non-condensable gas, and the condensed water is recycled. Ethanol forms a mixed gas phase with water vapor at a concentration of 65% (mass fraction), and is discharged from a side line at a20 th actual tray. From the above description, it can be seen that the above embodiments of the present invention achieve the following technical effects:
1) Compared with the ethanol concentration of the side stream discharged from the tower plate by adopting the combined rectification and membrane separation dehydration system (example 1) and the ethanol concentration in the mixed gas phase of the ethanol discharged from the side stream and the water vapor in example 2 (comparative example), the ethanol concentration in example 2 (comparative example) is 20.2%, the ethanol concentration in example 1 is 55% (mass fraction), the improvement is 1.72 times, and the rectification effect is obviously improved.
2) Example 1 the energy consumption of the beer column reboiler was 4.501 X10 7 kJ/h; example 2 the reboiler energy consumption of the beer column was 5.338 X10- 7 kJ/h, and the combined rectification and membrane separation dehydration system reduced the energy consumption of the beer column by 15.68% compared to conventional rectification systems.
3) The reboiler energy consumption of the second rectifying tower in the embodiment 1 is 8.865 X10- 7 kJ/h, the reboiler energy consumption of the second rectifying tower in the embodiment 2 is 8.017X 10- 7 kJ/h, and compared with a conventional rectifying system, the combined rectifying and membrane separation dehydration system has the advantage that the energy consumption of the second rectifying tower is reduced by 9.57%.
The above description is only of the preferred embodiments of the present invention and is not intended to limit the present invention, but various modifications and variations can be made to the present invention by those skilled in the art. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention should be included in the protection scope of the present invention.
Claims (8)
1. A method for treating cellulose ethanol fermentation mash, which is characterized in that the cellulose ethanol fermentation mash is treated by a mash tower; the bottom of the mash tower is provided with a reboiler, the lower part of the mash tower is provided with a material inlet, the inside of the mash tower is provided with a multistage column plate, and the top of the mash tower is provided with a membrane separation dehydrator;
the processing method comprises the following steps:
1) Feeding the cellulosic ethanol fermentation mash into the lower portion of the mash tower through the material inlet;
2) The cellulosic ethanol fermentation mash is heated by a reboiler at the bottom of the mash tower, and the vapor-liquid mixture is gradually increased to pass through the tower plate;
3) A mixture side offtake of water and ethanol;
4) Separating a gas phase material containing water and CO 2 through a membrane separation dehydrator at the top of the mash tower;
and (3) the gas phase material separated by the membrane separation dehydrator at the top of the mash tower enters a condenser, wherein CO 2 is recovered as non-condensable gas, and the condensed water is recycled.
2. The method according to claim 1, wherein the separation membrane in the membrane separation dehydrator is an inorganic membrane or an organic membrane.
3. The process of claim 2 wherein the inorganic membrane is a molecular sieve membrane.
4. The process of claim 1, wherein the mash tower has 20-50 trays; feeding from the 2 nd to 10 th plates at the top of the tower.
5. The method according to claim 4, wherein the head pressure of the beer column is 1.5 to 2.5 atm.
6. The process of claim 4, wherein the mixture of water and ethanol is sidedraw from trays 11 to 20.
7. A process for the preparation of cellulosic fuel ethanol comprising the treatment of cellulosic ethanol fermentation mash, characterized in that the treatment of cellulosic ethanol fermentation mash is carried out by the method of treatment of cellulosic ethanol fermentation mash according to any of claims 1-6.
8. The process of claim 7, wherein the mixture of water and ethanol from the side offtake is further rectified in a second rectification column.
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| CN202110820285.3A CN115636728B (en) | 2021-07-20 | 2021-07-20 | Treatment method of cellulose ethanol fermentation mash and preparation method of cellulose fuel ethanol |
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| CN115636728B true CN115636728B (en) | 2024-04-30 |
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| CN106928026A (en) * | 2015-12-30 | 2017-07-07 | 中粮营养健康研究院有限公司 | A kind of method of cellulosic ethanol distillation |
| CN110404285A (en) * | 2019-07-18 | 2019-11-05 | 肥城金塔酒精化工设备有限公司 | Four column distillations and UF membrane integrated system and its method for distilling ethyl alcohol |
| CN110483248A (en) * | 2019-08-06 | 2019-11-22 | 中海油天津化工研究设计院有限公司 | A kind of method of three towers, two film coupling and intensifying purification alcohol fuel |
| CN110698324A (en) * | 2019-11-20 | 2020-01-17 | 南京工业大学 | Device and novel process for producing fuel ethanol and electronic grade ethanol by rectification-membrane separation coupling method |
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Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
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| CN106928026A (en) * | 2015-12-30 | 2017-07-07 | 中粮营养健康研究院有限公司 | A kind of method of cellulosic ethanol distillation |
| CN110404285A (en) * | 2019-07-18 | 2019-11-05 | 肥城金塔酒精化工设备有限公司 | Four column distillations and UF membrane integrated system and its method for distilling ethyl alcohol |
| CN110483248A (en) * | 2019-08-06 | 2019-11-22 | 中海油天津化工研究设计院有限公司 | A kind of method of three towers, two film coupling and intensifying purification alcohol fuel |
| CN110698324A (en) * | 2019-11-20 | 2020-01-17 | 南京工业大学 | Device and novel process for producing fuel ethanol and electronic grade ethanol by rectification-membrane separation coupling method |
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