CN216404340U - Energy-saving device for producing fuel ethanol by using starch-based raw materials - Google Patents
Energy-saving device for producing fuel ethanol by using starch-based raw materials Download PDFInfo
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- CN216404340U CN216404340U CN202120587045.9U CN202120587045U CN216404340U CN 216404340 U CN216404340 U CN 216404340U CN 202120587045 U CN202120587045 U CN 202120587045U CN 216404340 U CN216404340 U CN 216404340U
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Abstract
The utility model discloses an energy-saving device for producing fuel ethanol by using starch-based raw materials, which comprises a pulping system, a liquefying system, a fermentation system and an ethanol rectification and dehydration system which are sequentially connected; the ethanol rectification dehydration system comprises a crude distillation tower, a first rectifying tower, a second rectifying tower and a molecular sieve adsorption tower; the crude distillation tower measuring line is respectively connected with a light wine tank and a secondary fine tower measuring line, and the tower kettle of the crude distillation tower is connected with a DDGS recovery system; the light wine tank is connected with a fine tower measuring line; the top of the first fine tower is connected with a second fine tower measuring line, the first fine tower measuring line is connected with an extraction tower, and the tower kettle of the extraction tower is connected with a light wine tank; the top of the second fine tower is connected with a molecular sieve adsorption tower, the measuring line of the second fine tower is connected with a light wine tank, and the kettle of the second fine tower is connected with a DDGS recovery system.
Description
Technical Field
The utility model relates to the technical field of fuel ethanol production, in particular to an energy-saving device for producing fuel ethanol by using starch-based raw materials.
Background
Ethanol is commonly called alcohol and can be classified into edible ethanol, industrial ethanol and fuel ethanol according to different purposes. Among them, fuel ethanol is a clean energy source, and is a new energy source which is internationally recognized and can reduce environmental pollution and replace petroleum fuel.
At present, the industrial production of fuel ethanol in China still takes corn, wheat and other grains as raw materials, and the production process mainly comprises five units of crushing, liquefying, fermenting, dehydrating and treating waste mash. The traditional device mainly has the problems of high steam consumption, large wastewater and carbon discharge amount, low ethanol concentration and the like, so that the production cost is high, and the popularization and the use of fuel ethanol are restricted. Therefore, the development of an efficient and energy-saving device for producing fuel ethanol is needed.
Disclosure of Invention
Aiming at the technical problems in the prior art, the utility model provides an energy-saving device for producing fuel ethanol by using starch-based raw materials, which is used for solving the problems of high steam consumption, large wastewater and carbon discharge amount, low ethanol concentration and the like of the conventional fuel ethanol production device.
The utility model provides an energy-saving device for producing fuel ethanol by using starch-based raw materials, which comprises a pulping system, a liquefying system, a fermentation system and an ethanol rectification and dehydration system which are sequentially connected;
the ethanol rectification dehydration system comprises a crude distillation tower, a first rectifying tower, a second rectifying tower and a molecular sieve adsorption tower;
the crude distillation tower measuring line is respectively connected with a light wine tank and a secondary fine tower measuring line, and the tower kettle of the crude distillation tower is connected with a DDGS recovery system;
the light wine tank is connected with a fine tower measuring line;
the top of the first fine tower is connected with a second fine tower measuring line, the first fine tower measuring line is connected with an extraction tower, and the tower kettle of the extraction tower is connected with a light wine tank;
the top of the second fine tower is connected with a molecular sieve adsorption tower, the measuring line of the second fine tower is connected with a light wine tank, and the kettle of the second fine tower is connected with a DDGS recovery system.
Preferably, the crude distillation column line is connected to the second fine column line through a second fine column preheater.
Preferably, the thin wine tank is connected with a fine tower measuring line through a fine tower preheater.
Preferably, the pulping system comprises a screw conveyor, the screw conveyor is connected with a powder slurry tank, the powder slurry tank is connected with a grading filter, and the grading filter is connected with the powder slurry tank through a steam ejector.
Preferably, the liquefaction system comprises a liquefaction tank, the classification filter is connected with the liquefaction tank, and the liquefaction tank is connected with a multi-stage cooler.
Preferably, the fermentation system includes the activation jar, the multistage cooler is connected with the activation jar, the activation jar is connected with yeast jar, fermentation cylinder in proper order, the fermentation cylinder is connected with washing tower survey line, washing tower survey line and CO2The low-temperature liquefaction equipment is connected.
Preferably, the crude distillation column is connected to the fermentor and the wash column vessel, respectively.
Preferably, the multi-stage cooler comprises a first stage cooler and a second stage cooler connected in series.
Preferably, the fermenter comprises a first fermenter and a second fermenter connected in series.
Preferably, the crude distillation column is connected to the fermenter and the water washing column tank, respectively, through a crude distillation column preheater.
Compared with the prior art, the utility model has the following beneficial effects: the utility model is provided with a pulping system, a liquefying system, a fermenting system and an ethanol rectification and dehydration system, thereby reducing water consumption and wastewater discharge. The utility model is suitable for industrial production and can generate remarkable economic and social benefits.
Drawings
FIG. 1 is a schematic diagram of the configuration of a pulping system and a liquefaction system in an embodiment of the utility model.
FIG. 2 is a schematic view of the structure of a fermentation system in the embodiment of the present invention.
FIG. 3 is a schematic structural diagram of an ethanol rectification and dehydration system in an embodiment of the utility model.
Wherein, 1, a screw conveyer; 2. a powder slurry tank; 3. a classification filter; 4. a liquefaction tank; 5. a steam ejector; 6. a primary cooler; 7. a secondary cooler; 8. an activation tank; 9. a wine mother tank; 10. a first fermenter; 11. a second fermenter; 12. washing the tower with water; 13. CO 22A cryogenic liquefaction plant; 14. a crude distillation column preheater; 15. a crude distillation column; 16. a light wine tank; 17. a second fine tower; 18. a molecular sieve adsorption tower; 19. a secondary fine tower preheater; 20. a fine tower; 21. a fine tower preheater; 22. an extraction tower; 23. a DDGS recovery system;
a. an alpha-amylase; b. mixing the slurry; c. liquefying the mash; d. mature mash; e. diluting with light wine; f. coarse wine; g. absolute ethyl alcohol; h. laterally collecting liquid; i. fusel oil; j. waste water; k. the extract liquor is light wine; l, raffinate fusel oil.
Detailed Description
In order to make the technical means, the creation characteristics, the achievement purposes and the effects of the utility model easy to understand, the utility model is further explained below by combining the specific drawings.
Examples
Referring to fig. 1-3, an energy-saving device for producing fuel ethanol by using starch-based raw materials comprises a pulping system, a liquefying system, a fermentation system and an ethanol rectification and dehydration system which are sequentially connected.
The pulping system comprises a screw conveyor 1, wherein the screw conveyor 1 is connected with a powder slurry tank 2, the powder slurry tank 2 is connected with a grading filter 3, and the grading filter 3 is connected with the powder slurry tank 2 through a steam ejector 5.
The liquefaction system includes liquefaction jar 4, and classifying filter 3 is connected with liquefaction jar 4, and liquefaction jar 4 is connected with multistage cooler, multistage cooler is including the one-level cooler 6 and the second grade cooler 7 of establishing ties mutually.
The fermentation system comprises an activation tank 8, a secondary cooler 7 is connected with the activation tank 8, the activation tank 8 is sequentially connected with a yeast tank 9, a first fermentation tank 10 and a second fermentation tank 11, the second fermentation tank 11 is connected with a measuring line of a water washing tower 12, and the measuring line of the water washing tower 12 is connected with CO2The cryogenic liquefaction plant 13 is connected.
The ethanol rectification dehydration system comprises a rough distillation tower 15, a first rectifying tower 20, a second rectifying tower 17 and a molecular sieve adsorption tower 18; the crude distillation tower 15 is respectively connected with the second fermentation tank 11 and the bottom of the water washing tower 12 through a crude distillation tower preheater 14, the measuring lines of the crude distillation tower 15 are respectively connected with the light wine tank 16 and the measuring lines of the second fine tower 17, and the bottom of the crude distillation tower 15 is connected with a DDGS recovery system 23; the light wine tank 16 is connected with a fine tower 20 by a measuring line; the top of the first fine tower 20 is connected with a measuring line of the second fine tower 17, the measuring line of the first fine tower 20 is connected with an extraction tower 22, and the bottom of the extraction tower 22 is connected with a light wine tank 16; the top of the second fine tower 17 is connected with a molecular sieve adsorption tower 18, the measuring line of the second fine tower 17 is connected with a light wine tank 16, and the bottom of the second fine tower 17 is connected with a DDGS recovery system 23.
Wherein, the measuring line of the crude distillation tower 15 is connected with the measuring line of the second fine tower 17 through a second fine tower preheater 19; the weak liquor tank 16 is connected with a fine tower 20 by a fine tower preheater 21.
In this embodiment, the process based on the energy saving device includes the following steps:
s1, crushing: adopting corn as a starch-based raw material, weighing the corn by a weighbridge, then unloading the corn into a corn hopper, lifting the corn by a conveyor and a bucket elevator, purifying the corn by magnetic separation, stone removal, impurity removal, iron removal and other processes, feeding the corn into a crusher after metering, and feeding the corn into a rolling sieve by negative pressure extraction to obtain corn flour with the particle size of 1.8-2.5 mm; returning unqualified large-particle corn grits to a crushing bin, and feeding the crushed large-particle corn grits to a crushing section for re-crushing;
s2, pulping: sending 120t/h corn flour, 215t/h mixing water, alpha-amylase and a returned clear liquid into a screw conveyor 1, adding alpha-amylase a into an inlet and an outlet of the screw conveyor 1 twice, stirring, sending into a powder slurry tank 2 for powder slurry treatment, introducing steam into the powder slurry tank 2, maintaining the temperature in the tank at 90 ℃, adding alkali liquor to adjust the pH value to 5.3, and obtaining mixed slurry; the slurry mixing water consists of waste water extracted from a tower kettle of a fine tower 20, evaporative condensate of a DDGS recovery system 23 and primary water, the slurry mixing water exchanges heat with the liquefied mash through a wide-channel plate heat exchanger, and is mixed with the corn flour after being heated to 90 ℃;
s3, liquefaction: the mixed slurry is conveyed to a grading filter 3 by a pump, the filtrate directly enters a liquefaction tank 4 and is added with liquefaction enzyme for liquefaction treatment, the temperature of the liquefaction treatment is 90 ℃, compared with the same liquefaction of the traditional high-temperature cooking, the energy can be effectively saved, the consumption can be reduced, the energy can be saved by more than 20 percent, and the liquefied mash is obtained; the large powder agglomerates and the large particles intercepted by the filter are heated by a primary steam ejector 5 and then circulated back to the powder slurry tank 2 for re-gelatinization;
s4, fermentation: after heat exchange is carried out on the liquefied mash and the size mixing water b, the liquefied mash and the size mixing water b are sequentially cooled to 30 ℃ through a primary cooler 6 and a secondary cooler 7, sulfuric acid is added to adjust the pH value to 4.5, urea, saccharifying enzyme and acid protease are added to carry out fermentation treatment, and 310t/h of mature mash is obtained, wherein the ethanol concentration is 15%; the fermentation treatment specifically comprises the following steps: a small amount of liquefied mash c, dry yeast and primary water are fed into an activation tank 8 to be mixed and activated for 2 hours to obtain activated yeast; delivering 25% of liquefied mash c and activated yeast to a yeast tank 9, mixing, performing yeast propagation for 9h to obtain yeast, introducing sterile air during the yeast propagation, and cooling by an external circulation plate heat exchanger to keep the temperature of the yeast propagation at 30 ℃; the residual liquefied mash c and yeast enter a first fermentation tank 10 and a second fermentation tank 11 in sequence to be mixed and then are subjected to fermentation treatment, wherein in the fermentation treatment, a plurality of groups of parallel synchronous saccharification intermittent fermentation modes are adopted, the fermentation is kept at 32 ℃ through external circulation plate type heat exchange, and the fermentation treatment time is 62 hours; wherein the heat generated by propagation and fermentation is taken away by circulating water, and the generated CO2Sent to a water scrubber 12 for purification and then sent to CO2The low-temperature liquefaction equipment 13 recovers to obtain 37t/h liquid carbon dioxide, and reduces carbon emissionThe washing liquid and the mature mash are sent to an ethanol rectification dehydration section;
s5, rectifying and dehydrating ethanol: carrying out ethanol rectification dehydration treatment on the mature mash; the ethanol rectification dehydration treatment specifically comprises the following steps: preheating mature mash d, then feeding the preheated mash d into a coarse distillation tower 15, removing non-condensable gas at the top of the coarse distillation tower 15, collecting light wine e with high concentration of fusel from the lateral line of a degassing section of the coarse distillation tower 15, feeding the light wine e into a light wine tank 16, collecting crude wine f with high concentration of ethanol from the lateral line of a stripping section of the coarse distillation tower 15, and collecting waste mash from a tower kettle of the coarse distillation tower 15; the noncondensable gas is sent to a water scrubber, purified and sent to CO2The low-temperature liquefaction equipment is used for recycling and reducing carbon emission;
heating the crude wine f, then sending the heated crude wine f to a secondary refining tower 17, introducing a gas-phase mixture of ethanol water extracted from the tower top of the secondary refining tower 17 into a molecular sieve adsorption tower 18 for dehydration to obtain anhydrous ethanol g, sending the anhydrous ethanol g into a finished product tank, wherein the flow rate of the ethanol gas after adsorption is 38t/h, the water content is less than or equal to 0.04%, extracting a side extraction liquid h with higher concentration of fusel from the side line of the secondary refining tower 17, and extracting waste mash from the tower bottom of the secondary refining tower 17; the molecular sieve adsorption tower 18 is operated in two continuous cycles; when one set is subjected to adsorption operation, the other set is subjected to regeneration desorption operation by using absolute ethyl alcohol steam, the absolute ethyl alcohol steam is condensed and sent into the finished product tank, and the desorbed ethyl alcohol is condensed and sent into the light wine tank; the operating pressure during adsorption was 50kPa, and the operating pressure during desorption was-50 kPa;
mixing the liquid in the light wine tank 16 and the side liquor h, heating the mixture by a first rectifying tower preheater 21, sending the mixture into a first rectifying tower 20, collecting crude wine f which does not contain fusel and has ethanol concentration of 88-92% from the top of the first rectifying tower 20, sending the crude wine f to a second rectifying tower 17 for further concentration, collecting fusel oil i from the side of the first rectifying tower 20, sending the fusel oil i to an extraction tower 22, and sending waste water j, the ethanol content of which is less than or equal to 0.03%, collected from the bottom of the first rectifying tower 20 to the step 2 to be used as slurry mixing water;
the extraction tower 22 uses water as an extractant to extract ethanol in fusel oil i, extract light wine k is introduced into a light wine tank 16, and raffinate fusel oil l is sent into the finished product tank;
wherein, the pressure at the top of the coarse distillation tower 15 is 60kPa, the temperature at the top of the tower is 52 ℃, and the temperature at the bottom of the tower is 83 ℃; the pressure at the top of the secondary fine tower 17 is 25kPa, the temperature at the top of the secondary fine tower is 93 ℃, and the temperature at the bottom of the secondary fine tower is 117 ℃; the pressure at the top of the fine tower 20 is 400kPa, the temperature at the top of the fine tower is 127 ℃, and the temperature at the bottom of the fine tower is 155 ℃; the rough distillation tower 15, the second rectifying tower 17 and the first rectifying tower 20 exchange heat through differential pressure rectification coupling, namely only one rectifying tower 20 adopts once fresh steam to indirectly heat the reboiler, alcohol steam generated at the top of the first rectifying tower 20 heats the reboiler of the second rectifying tower, and alcohol steam generated at the top of the second rectifying tower 17 heats the reboiler of the rough distillation tower, so that the coupling utilization of energy is realized; the crude distillation tower 15 is preheated by tower top steam and absolute ethyl alcohol steam, and the first rectifying tower 20 and the second rectifying tower 17 are preheated by tower bottom liquid;
s6, denaturation and DDGS recovery: adding gasoline into the absolute ethyl alcohol in the finished product tank, and performing denaturation treatment at the flow rate of 0.75t/h to obtain fuel ethyl alcohol with the yield of 39 t/h; 235t/h of waste mash with about 13 percent of solid from the rectifying section enters a horizontal spiral centrifuge for centrifugal separation treatment to obtain clear liquid and wet grains; taking 25% of the clear liquid as a recovered clear liquid, and concentrating the rest part of the clear liquid to 30% of solid content after evaporation concentration treatment in a multi-effect evaporation unit to obtain steam and concentrated liquid; condensing the steam to obtain condensate, wherein one part of the condensate is used as slurry mixing water, and the other part of the condensate is sent to a sewage treatment station for wastewater removal treatment; mixing the concentrated solution with the wet grains, and drying to obtain a DDGS byproduct with the yield of 32t/h, wherein waste gas generated by drying is used as a heat source for evaporation concentration treatment; the final concentration of the multi-effect evaporation is 30%.
In the embodiment, the steam consumption of the crushing, liquefying, fermenting, rectifying and dehydrating sections is 1.5 t/t ethanol. And (3) blending the dehydrated ethanol with gasoline (the mass ratio is 50: 1) to obtain the fuel ethanol meeting the national standard GB 18350-2013.
In the embodiment, a low-temperature jet liquefaction process is adopted, so that energy can be effectively saved and consumption can be reduced by more than 20% compared with the traditional liquefaction process for high-temperature cooking; a low-temperature liquefaction non-cooking process is adopted, and meanwhile, the liquefied mash is cooled in multiple stages to recover heat, so that the steam consumption is reduced; the secondary addition process of amylase is adopted, so that the viscosity of the liquefied mash is reduced, the conveying energy consumption of the liquefied mash is effectively reduced, and the energy-saving purpose is achieved; the thick mash synchronous saccharification intermittent fermentation is adopted, the ethanol concentration of mature mash is more than 15%, the ethanol concentration of mature mash in the traditional step-by-step saccharification and fermentation is only 10-11%, the device investment is obviously reduced, and the steam consumption of ethanol dehydration is reduced. The embodiment purifies and recovers the carbon dioxide, and reduces carbon emission. The embodiment is also suitable for various starchy raw materials such as wheat, sorghum, rice, sweet potatoes, cassava and the like.
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 (10)
1. An energy-saving device for producing fuel ethanol by using starch-based raw materials is characterized by comprising a pulping system, a liquefying system, a fermentation system and an ethanol rectification and dehydration system which are sequentially connected;
the ethanol rectification dehydration system comprises a crude distillation tower (15), a first rectifying tower (20), a second rectifying tower (17) and a molecular sieve adsorption tower (18);
the measuring line of the crude distillation tower (15) is respectively connected with the measuring line of the light wine tank (16) and the measuring line of the secondary rectifying tower (17), and the tower kettle of the crude distillation tower (15) is connected with a DDGS recovery system (23);
the light wine tank (16) is connected with a measuring line of a fine tower (20);
the top of the first fine tower (20) is connected with a measuring line of a second fine tower (17), the measuring line of the first fine tower (20) is connected with an extraction tower (22), and the kettle of the extraction tower (22) is connected with a light wine tank (16);
the top of the secondary fine tower (17) is connected with a molecular sieve adsorption tower (18), the measuring line of the secondary fine tower (17) is connected with a light wine tank (16), and the bottom of the secondary fine tower (17) is connected with a DDGS recovery system (23).
2. Energy saving device according to claim 1, characterized in that the line of the crude distillation column (15) is connected to the line of the second fine column (17) through a second fine column preheater (19).
3. Energy saving device according to claim 1, characterized in that the weak liquor tank (16) is connected to a fine tower (20) line through a fine tower preheater (21).
4. The energy saving device according to claim 1, characterized in that the pulping system comprises a screw conveyor (1), the screw conveyor (1) is connected with a pulp tank (2), the pulp tank (2) is connected with a classifying filter (3), and the classifying filter (3) is connected with the pulp tank (2) through a steam ejector (5).
5. The energy saving device according to claim 4, characterized in that the liquefaction system comprises a liquefaction tank (4), the staged filter (3) being connected to the liquefaction tank (4), the liquefaction tank (4) being connected to a multi-stage cooler.
6. The energy saving device according to claim 5, characterized in that the fermentation system comprises an activation tank (8), the multistage cooler is connected with the activation tank (8), the activation tank (8) is connected with the wine mother tank (9) and the fermentation tank in turn, the fermentation tank is connected with a water washing tower (12) measuring line, the water washing tower (12) measuring line is connected with the CO measuring line2The low-temperature liquefaction equipment (13) is connected.
7. The energy saving device according to claim 6, wherein the crude distillation column (15) is connected to the fermenter and the bottom of the water washing column (12), respectively.
8. An energy saving device according to claim 5, characterized in that the multi-stage cooler comprises a primary cooler (6) and a secondary cooler (7) in series.
9. Energy saving device according to claim 6, characterized in that the fermenter comprises a first fermenter (10) and a second fermenter (11) connected in series.
10. The energy saving device according to claim 7, wherein the crude distillation tower (15) is connected to the fermenter and the tank of the water washing tower (12) through the crude distillation tower preheater (14), respectively.
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| CN202120587045.9U CN216404340U (en) | 2021-03-23 | 2021-03-23 | Energy-saving device for producing fuel ethanol by using starch-based raw materials |
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| CN202120587045.9U CN216404340U (en) | 2021-03-23 | 2021-03-23 | Energy-saving device for producing fuel ethanol by using starch-based raw materials |
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