CN1298859C - Production of alcohol fuel - Google Patents
Production of alcohol fuel Download PDFInfo
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- CN1298859C CN1298859C CNB2004100940850A CN200410094085A CN1298859C CN 1298859 C CN1298859 C CN 1298859C CN B2004100940850 A CNB2004100940850 A CN B2004100940850A CN 200410094085 A CN200410094085 A CN 200410094085A CN 1298859 C CN1298859 C CN 1298859C
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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
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- 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
Abstract
The present invention relates to a production method of fuel ethanol. Inventors invent the special unitized technology for the fuel ethanol by aiming at the large-scale ethanol production. The present invention is composed of working procedures of raw material treatment, fermentation, rectification, molecular sieve adsorption dehydration and waste liquid treatment, wherein the rectification working procedure and the molecular sieve adsorption dehydration working procedure are connected through a thermal coupling condensation evaporation process; the thermal coupling condensation evaporation method has the steps that gas phase ethanol adopted in the rectification working procedure is sent into the molecular sieve adsorption dehydration working procedure through the thermal coupling condensation evaporation process, the condensation evaporation process is accomplished through thermal coupling, heat released by condensation is used as heat sources of the ethanol evaporation, and no heat needs to be additionally added. The present invention uses corn, rice, wheat, grain sorghum, dried sweet potatoes, cassava, sugar cane juice, beet juice or molasses, etc. as raw materials.
Description
Technical field
The invention relates to the method for producing alcohol fuel for starchiness or saccharine material.
Background technology
Entered in 20th century with the raw material epoch of oil as main energy sources and petroleum chemicals.But two serious problems have also appearred thereupon: the one, and oil is non-renewable resource, because a large amount of exploitation, consumes too fastly, has faced exhaustion; The 2nd, act as a fuel and the chemical raw material has caused the havoc, particularly CO of environment with oil
2Greenhouse effect.Based on the reason of above two aspects, the clean fuel that people are making great efforts to develop the new reproducible energy and can not pollute environment.
Alcohol fuel so that starchiness or saccharine material are produced has the combustionproperty similar with mineral fuel, and its raw materials for production are biogenic, are a kind of reproducible energy.In addition, carbon monoxide and sulfurous gas that the ethanol combustion processes is discharged all are lower than gasoline combustion, remain basically stable on the quantity of carbonic acid gas that is produced and the carbonic acid gas that growth is consumed as the biogenic of raw material, this is to reducing atmospheric pollution and to suppress Greenhouse effect significant.Therefore, alcohol fuel is also referred to as " clean fuel ".
According to existing national standard, the ethanol that is used for fuel requires water-content≤0.8% (v/v) with ethanol.Because there is minimum boiling point in the mixture of second alcohol and water, can only obtain the ethanol of 95.5% (v/v) with the sepn process of conventional distillation technology.Obtain the lower dehydrated alcohol of water-content, the essential dehydration procedure that increases.
The production process of producing edible ethanol with starchy material comprises the preparation of powder slurry, liquefaction, saccharification, fermentation, rectifying and useless mash treatment process.Need to increase dehydration procedure in the production of fuel ethanol in above-mentioned operation, the ethanol water of about 95.5% (v/v) that rectifying is obtained takes off below 0.8% (v/v).Producing in the technology of edible ethanol or alcohol fuel with saccharine material, both can save the above-mentioned preparation of powder slurry, liquefaction, saccharification operation.
Alcohol fuel and edible ethanol have certain difference, and edible ethanol is had relatively high expectations to impurity but be not high to moisture requirement; And alcohol fuel is less demanding but moisture content is had relatively high expectations to impurity.Only add dehydration by the edible ethanol production technique, process for refining do not added improve and the production alcohol fuel that make production of fuel ethanol energy consumption height, investment is big, has restricted the economy of fuel ethanol production.
Jin Fengqiu etc. have proposed " a kind of industrial production technology of new alcohol (containing fuel alcohol) " (Chinese patent application 02110666.5), isolate the solid substance in the raw material before fermentation earlier; Adopt distillery yeast to separate and the part reuse technology; Organic acid in the recovery waste water, oligose etc. make alcohol waste water can realize the reuse fermentation.Sub-argument goes out the solid substance in the raw material before fermentation, and meeting residual sugar in the solid substance that sub-argument goes out causes the loss of sugar.If use the clear water repetitive scrubbing, though can reduce sugar loss, can reduce the sugared concentration of proferment feed liquid, make the wine of fermenting-ripening mash divide reduction, increase alcohol and separate the steam consumption of purifying.Yeast separation and part reuse can improve fermentation efficiency, but the used separator for processing amount of yeast separation is little, the power consumption height.Simultaneously, for being the Production of Fuel Ethanol of raw material with starch, vinasse can be used as protein fodder and use, and the existence of yeast thalline can increase the protein content in the feed.The waste water recycling method that this patent proposes uses weak base anion-exchange resin to carry out adsorption treatment, but for large-scale commercial production, regeneration of resin will produce secondary sewage, and Pollution abatement is not thorough.
The present inventor proposes " a kind of alcohol refining process for producing several products " (ZL 02117068.1), is that realization raw spirit and edible ethanol are produced with device according to the identical and different production technology characteristics of raw spirit with the refining dehydration of edible ethanol.This technical process both can have been produced the edible ethanol of all size separately, can produce the raw spirit of all size again separately, also can produce the edible ethanol and the raw spirit of all size simultaneously.This technical process the handiness that has improved the Alcohol Production device is set, but will increase the plant construction investment.For being exclusively used in the device of producing alcohol fuel on a large scale, this technology still need be improved and be optimized, to reduce plant investment and process cost.
Summary of the invention
The present inventor has invented the complete set technology that is exclusively used in fuel ethanol production at extensive fuel ethanol production.Starchiness or saccharic are raw material, comprise raw material processing, fermentation, rectifying, molecular sieve adsorbing and dewatering, useless mash treatment process composition; Rectification working process is connected by thermal coupling condensation evaporation process with the molecular sieve dehydration operation, wherein thermal coupling condensation evaporation method is: the gaseous ethanol of ethanol refinery operation extraction, send into the molecular sieve adsorbing and dewatering operation by thermal coupling condensation, evaporative process, this condensation, evaporative process are finished by thermal coupling, the condensation liberated heat does not need to add in addition heat as the thermal source of ethanol evaporation.
The present invention produces alcohol fuel with starchy material technology is made of the preparation of powder slurry, starch liquefacation saccharification, fermentation, rectifying, molecular sieve adsorbing and dewatering, useless mash treatment process, as shown in Figure 1.
The process description of producing alcohol fuel with starchy material is as follows:
Powder slurry preparation section, with starchy material such as corn, rice, wheat, Chinese sorghum, sweet potato do, cassava etc. pulverizes, and is crushed to the granularity that is suitable for the starch granules stripping.The method of pulverizing can be a wet pulverization, also can be that dry ground or semidrying are pulverized.For being the process of raw material production alcohol fuel with the corn, in pulverizing process, can increase and go the shepherd's purse operation, corn shepherd's purse sub-argument is gone out, be used to produce Semen Maydis oil.The water spice, the concentration of adjusting the powder slurry is dry matter content 20 ~ 35%, pH value is 3 ~ 6.
Starch liquefacation saccharification operation adopts low temperature boiling and steam ejection liquefaction technology.Powder is starched the powder slurry adding amylase that preparation section prepares, and amylase content is 1.0 ~ 10.0 units/gram raw materials, and at first add-on is for adding 25% of amylase total amount.Add steam boiling, 75 ~ 98 ℃ of boiling temperatures, cooking time 30 ~ 60 minutes.After the boiling starch slurry is sent into Jet liquefier, carry out steam ejection liquefaction.The Heating temperature of material in Jet liquefier is 100 ~ 110 ℃, and the residence time is 10 ~ 20 minutes, finishes liquefaction process one time.Finish the mash after once liquefying, flash distillation is chilled to 90 ℃ in vacuum flasher, enters liquefied pot then, adds remaining amylase and carries out secondary liquefaction.Mash after the liquefaction makes temperature reduce to 50 ~ 60 ℃ through cooling fully, adjusts pH value to 3.0 ~ 5.0 with sulfuric acid, and adds saccharifying enzyme and nutritive salt carries out saccharification to liquefied fermented glutinous rice, and partial starch is converted into fermentable sugars.Saccharification liquid cools off through secondary, makes temperature reduce to 28 ~ 33 ℃.Mellow solution of saccharification small part after saccharification is sent distiller's yeast propagation jar, and major part is sent first jar of fermentor tank.After active dry yeast activates in activation pot, send into distiller's yeast propagation jar and carry out multiplication culture.Cultivate the first jar that qualified yeast wash is sent to fermentor tank continuously.
Fermentation procedure, fermenting process carries out in the fermentor tank of series polyphone.By converted mash and the yeast wash that liquid glucose chemical industry preface is come, first jar that enters fermentor tank ferments, continuously ferments by follow-up fermentor tank successively then.Each fermentor tank is provided with the outer circulation interchanger, to keep 30 ~ 33 ℃ of leavening temperatures.The ripe wine with dregs that fermentation is finished is through ripe wine with dregs pumping rectification working process.
Rectification working process, the technical process of rectification working process and molecular sieve adsorbing and dewatering operation as shown in Figure 3.Ripe mash from fermentation procedure enters wine with dregs tower 11 tops.The heating medium of wine with dregs Tata still reboiler 2 is the overhead gas of dehydration tower, and the heating medium of wine with dregs Tata still reboiler 1 is the raw spirit steam of dehydration procedure.Useless mash is through being pumped to useless mash treatment process at the bottom of removing the tower behind the alcohol.The light wine of cat head extraction is pumped to dehydration tower 12.In dehydration tower, deviate from most of water through refinery distillation, the cat head fraction is the azeotrope of ethanol and water, ethanol content is about 95.5% (v/v).Cat head gaseous ethanol condensation in thermal coupling condensation evaporation interchanger (6) with dehydration tower, condensed liquid phase ethanol is sent into evaporation in the thermal coupling condensation evaporation interchanger (6) with transferpump 7 through flow control, and the gaseous ethanol after the evaporation is delivered to the molecular sieve adsorbing and dewatering operation.
The molecular sieve adsorbing and dewatering operation is heated to 120 ~ 160 ℃ by the gaseous ethanol after thermal coupling condensation evaporation interchanger (6) evaporation in interchanger 4, deliver to the sieve adsorpting bed 13A that is in adsorbed state, removes remaining moisture content through the adsorption of molecular sieve.Alcohol steam after the dehydration enters the wine with dregs tower reboiler 1 of thermal coupling rectifying, as the thermal source of wine with dregs tower heating.The final fuel-grade ethanol product that obtains after the alcohol steam condensation.When the sieve adsorpting bed 13A that is in adsorbed state is saturated near absorption, adsorption bed switches, the sieve adsorpting bed 13A that is in adsorbed state switches to the desorption and regeneration state, and the adsorption bed 13B that is in the desorption and regeneration state has originally regenerated and finished, and switches to adsorbed state.So circulation, assurance device moves continuously.
The present invention proposes thermal coupling condensation evaporation process, rectification working process and molecular sieve adsorbing and dewatering operation are linked together.Thermal coupling condensation evaporation process is made up of thermal coupling condensation evaporation interchanger (6), evaporation fresh feed pump (7), under meter (8), regulating and controlling valve (9) and corresponding connection line.From the vapour phase alcohol of rectification working process, enter the hot side of thermal coupling condensation evaporation interchanger (6), vapour phase alcohol condensation when giving the heating of liquid phase vaporized alcohol.The alcohol lime set is by transferpump (7), sends into the cold side of thermal coupling condensation evaporation interchanger (6) through the flow control of strictness, is subjected to thermal evaporation.Vapour phase alcohol after the evaporation enters the molecular sieve adsorbing and dewatering operation.
Useless mash treatment process, this operation comprise centrifugation, multiple-effect evaporation and wet poor drying process.
To send into settling centrifuge from the useless mash of ethanol refinery operation, utilize high speed centrifugation sedimentation principle, carry out solid-liquid separation, isolate contained clear liquid in wet being pickled with grains or in wine to greatest extent.The isolated wet poor drying machine of sending into; Isolated centrifugal clear liquid partly returns fermentation procedure, and part is carried out multiple-effect evaporation and concentrated.It is the secondary steam that drying machine produces that multiple-effect evaporation concentrates required thermal source, and the concentrated solution-underflow of acquisition and centrifugation go out, and wet being pickled with grains or in wine sent into drying machine after mixing and carried out drying.The secondary steam that drying machine produces is as the thermal source of multiple-effect evaporation.Doing of drying machine output is poor---DDGS (Dry Distiller ' s Grain Soluble solubility vinasse protein fodder), can be according to user's requirement, and directly packing is sold, and also can carry out granulation, sells with the pellet pattern.
The present invention produces alcohol fuel with saccharine material technology transfers dense, fermentation, rectifying, molecular sieve adsorbing and dewatering, useless mash treatment process to constitute by the liquid glucose acid adjustment, as shown in Figure 2.
With saccharine material as: sugar cane juice, sugar beet juice or molasses etc. are adjusted to dry matter content 10 ~ 28% respectively, and pH value 3 ~ 6 carries out directly that distiller's yeast is cultivated and fermenting process.
Fermentation, rectifying, molecular sieve adsorbing and dewatering operation and are that the raw material production fuel alcohol is identical with starch.
Useless mash treatment process, the mash that will give up carries out multiple-effect evaporation, and the underflow that obtains can not be used as feed, can be used for production composite fertilizer or is used for boiler combustion, recovered energy.
Description of drawings
Fig. 1: the technology of producing alcohol fuel with starchy material;
Fig. 2: the technology of producing alcohol fuel with saccharine material;
Fig. 3: alcohol fuel thermal coupling condensation evaporation technology.
Embodiment
Further specify implementation process of the present invention below in conjunction with specific embodiment.
With starchy material such as corn, rice, wheat, Chinese sorghum, sweet potato do, cassava etc. produces alcohol fuel technology as shown in Figure 1, present embodiment is the production alcohol fuel of raw material with the corn, and the technological process of other starchy materials is roughly the same.
The raw material corn is pulverized, and breaking method can be a wet pulverization, also can be that dry method, semidrying are pulverized.The water spice, the concentration of adjusting the powder slurry is dry matter content 31%, pH value is 4.5.Add amylase, diastatic adding total amount is 2.5 units/gram raw materials, at first adds 25% of total amount.Add steam boiling, 80 ℃ of boiling temperatures, cooking time 30 minutes.After the boiling starch slurry is sent into Jet liquefier, carry out steam ejection liquefaction.The Heating temperature of material in Jet liquefier is 105 ℃, and the residence time is 15 minutes, finishes liquefaction process one time.Finish the mash after once liquefying, flash distillation is chilled to 90 ℃ in vacuum flasher, enters liquefied pot then, adds remaining amylase and carries out secondary liquefaction.Mash after the liquefaction makes temperature reduce to 55 ℃ through cooling fully, adjusts pH value to 3.8 with sulfuric acid, and adds saccharifying enzyme and nutritive salt carries out saccharification to liquefied fermented glutinous rice, and partial starch is converted into fermentable sugars.Saccharification liquid cools off through secondary, makes temperature reduce to 32 ℃.Mellow solution of saccharification small part after saccharification is sent distiller's yeast propagation jar, and major part is sent first jar of fermentor tank.After active dry yeast activates in activation pot, send into distiller's yeast propagation jar and carry out multiplication culture.Cultivate the first jar that qualified yeast wash is sent to fermentor tank continuously.
By converted mash and the yeast wash that liquid glucose chemical industry preface is come, first jar that enters fermentor tank ferments, continuously ferments by follow-up fermentor tank successively then.Each fermentor tank is provided with the outer circulation interchanger, is 30 ~ 33 ℃ to keep suitable leavening temperature, and total fermentation time is 30 hours.The ripe wine with dregs that fermentation is finished is through ripe wine with dregs pumping rectification working process.
The technical process of thermal coupling rectifying and molecular sieve adsorbing and dewatering as shown in Figure 3.Ripe mash from fermentation procedure enters wine with dregs tower 11 tops through secondary thermal coupling heat exchange.The heating medium of wine with dregs Tata still reboiler 2 is the overhead gas of dehydration tower, and the heating medium of wine with dregs Tata still reboiler 1 is the raw spirit steam of dehydration procedure, and the tower still pressure of wine with dregs tower is-0.5 ~ 0MPa, and tower still temperature is 70 ~ 100 ℃.Useless mash is through being pumped to useless mash treatment process at the bottom of removing the tower behind the alcohol.The light wine of cat head extraction is pumped to dehydration tower 12.The heating medium of dehydration tower is a steam, and tower still pressure is 0.2 ~ 1.0MPa, and tower still temperature is 164 ℃.In dehydration tower, deviate from most of water through refinery distillation, the cat head fraction is the azeotrope of ethanol and water, ethanol content is 95.5% (v/v).With cat head gaseous ethanol condensation in thermal coupling condensation evaporation interchanger 6 of dehydration tower, condensed liquid phase ethanol is sent into thermal coupling condensation evaporation interchanger 6 with transferpump 7 through flow control.Gaseous ethanol after the evaporation is heated to 128 ℃ in interchanger 4, deliver to the sieve adsorpting bed 13A that is in adsorbed state, removes remaining moisture content through the adsorption of molecular sieve.Alcohol steam after the dehydration enters the wine with dregs tower reboiler 1 of thermal coupling rectifying, as the thermal source of wine with dregs tower heating.The final fuel-grade ethanol product that obtains after the alcohol steam condensation.The water-content of alcohol fuel is 0.5% (V/V).When the sieve adsorpting bed 13A that is in adsorbed state is saturated near absorption, adsorption bed switches, the sieve adsorpting bed 13A that is in adsorbed state switches to the desorption and regeneration state, and the adsorption bed 13B that is in the desorption and regeneration state has originally regenerated and finished, and switches to adsorbed state.So circulation, assurance device moves continuously.
Useless mash from the ethanol refinery operation is sent into settling centrifuge, carries out solid-liquid separation.The isolated wet poor drying machine of sending into; Isolated centrifugal clear liquid partly returns fermentation procedure, and part is carried out multiple-effect evaporation and concentrated.It is the secondary steam that drying machine produces that multiple-effect evaporation concentrates required thermal source, and the concentrated solution-underflow of acquisition and centrifugation go out, and wet being pickled with grains or in wine sent into drying machine after mixing and carried out drying.The secondary steam that drying machine produces is as the thermal source of multiple-effect evaporation.The dried poor DDGS protein fodder that is of drying machine output.
Embodiment 2
The technology of producing alcohol fuel with saccharine material such as sugar beet juice, sugar cane juice, molasses etc. as shown in Figure 2, present embodiment is that molasses are the production alcohol fuel of raw material.
The raw material molasses are sent into the pre-treatment jar through the precipitation slagging-off, add water and adjust sugared concentration to 24%, add acid and adjust liquid glucose pH value 3.5.Adjust the liquid glucose small part of concentration and acidity and send distiller's yeast propagation jar, major part is sent first jar of fermentor tank.After active dry yeast activates in activation pot, send into distiller's yeast propagation jar and carry out multiplication culture.Cultivate the first jar that qualified yeast wash is sent to fermentor tank continuously.
The implementation process of fermentation procedure, rectification working process, molecular sieve adsorbing and dewatering operation is identical with embodiment 1.
From wine with dregs tower reboiler obtain phlegma---the water-content of alcohol fuel is 0.4% (V/V).
Useless mash from the ethanol refinery operation is sent into settling centrifuge, carries out solid-liquid separation.Isolated centrifugal clear liquid partly returns fermentation procedure, and part is carried out multiple-effect evaporation and concentrated.The water with fixed attention of multiple-effect evaporation returns molasses and transfers dense acid adjustment operation.Wet being pickled with grains or in wine that underflow that multiple-effect evaporation obtains and solid-liquid separation go out can be used for production composite fertilizer or is used for boiler combustion, recovered energy.
Below implementation process of the present invention and effect are described in detail:
Produce with starchy material in the technological process of fuel alcohol, it is the preceding necessary operation of fermenting that starch liquefacation, saccharification are converted into fermentable sugars.In each operation of preparation fermenting-ripening wine with dregs, main steam consumption concentrates on the liquefaction operation of starch.Therefore, the liquefaction process of starch being improved is one of effective way that reduces the Production of Fuel Ethanol total energy consumption.
The present invention discovers, in starch material water-swelling process, only need adopt the low temperature gelatinization process, can reach the requirement of ideal gelatinization effect and starch stripping and sterilization.For this reason, this process using low temperature boiling technology is to reduce the steam consumption of starch slurry digestion process.Improve the concentration of starch slurry, reduce the material treatment capacity of digestion process, also can reduce steam consumption.Therefore, the present invention adopts high density to join slurry.Discover that simultaneously lower boiling temperature also can reduce the generation of impurity, reduce the loss of active princlple, improve alcohol yield.
Enzymatic liquefaction and Mashing process (double-enzyme method thinning technology) are ideal method for manufacturing sugar.The present invention is directed to the characteristics of zymamsis industry, adopt enzyme-added, high-temperature injection liquefaction, vacuum flashing chilling and a low temperature secondary liquefaction technology twice, give full play to the usefulness of high-quality fire resistant alpha-diastase, significantly reduce the consumption of zymin in the liquefaction process, improve the transformation efficiency of raw starch.Simultaneously, the present invention adopts the distillation system exhaust steam to carry out steam ejection liquefaction, and the flash distillation lime set is returned means such as powder slurry jar, has reduced the consumption of live steam and water resources.
The present invention is directed to extensive Production of Fuel Ethanol needs, develop the thick mash technology of continuously fermenting.For the scale operation device, in order to reduce the table of equipment number, reduce investment, equipment enlarging is necessary.The ethanol fermentation process relates to vapour, liquid, solid three-phase.Reduction in the fermentation later stage owing to ferment strength, CO
2Burst size reduce, the solid formation in the fermentation liquid easily deposits, thereby causes fermentation undesired.For the ultra-large type fermentor tank, this problem is particularly serious.For solving this difficult problem, the present invention adopts distributed reduce power consumption multidimensional side whipping appts, develops the ultra-large type bio-reactor.Successfully solved the easy deposition problems of solid formation in the ethanol fermentation process ultra-large type bio-reactor, eliminated the easy microbiological contamination, residual sugar height, the yield that exist in the large scale continuous prod process and hanged down phenomenons such as reaching the production instability.
The present invention develops the special-purpose thermal coupling distillation technology of Production of Fuel Ethanol.The reboiler of wine with dregs tower is become the thermal coupling process with the design of condenser of dehydration tower---the reboiler of wine with dregs tower has been realized the second stage employ of energy as the dehydration tower condenser.In traditional biomass to alcohol conversion process, the steam consumption of rectifying is up to 7.0 tons.Adopt thermal coupling distillation technology of the present invention, the steam consumption quantity of rectifying can be reduced to below 1.8 tons.
The present inventor has developed alternating temperature transformation molecular sieve dehydration technology.Compound alternating temperature and transformation process in ethanol molecule sieve dewatering process have realized the high efficiency manipulation of absorption and desorption process.Adopt the control condensation process to realize transformation, guaranteed system operation stability and controllability.Flexible many adsorption beds combined process flow of preparation has farthest improved the utilization ratio of molecular sieve.Make the steam consumption of alternating temperature transformation adsorption dewatering process alcohol fuel per ton only be 1/3 of traditional method.
In the ethanol refinery process, obtain liquid phase alcohol usually.And molecular sieve adsorbing and dewatering is a gas phase process.Therefore, before molecular sieve adsorbing and dewatering, at first need the liquid phase vaporized alcohol is gasified.Obtain the process of liquid phase alcohol revaporization from rectification working process, make rectification working process consume water coolant, and vaporized alcohol consumes steam again.If rectification working process dehydration tower gas-phase alcohol directly enters molecular sieve adsorbing and dewatering, the consumption of steam and recirculated water will be saved.But rectifying tower is the operate continuously of pressure-stabilisation, and the pressure of sieve adsorpting bed is to change in the cycle.The dehydration tower gas phase is directly introduced sieve adsorpting bed, and the pressure change of adsorption bed can cause the pressure surge of dehydration tower.Conventional regulating measure is difficult to adapt to the pressure surge of adsorption bed, and the pressure-stabilisation with the control dehydration tower influences the normal running of dehydration tower.In addition, because the fluctuation of pressure causes difficulty for the flow measurement and the control of the gaseous stream that enters the dehydration bed.The stable efficient operation to assurance dehydrating effect and sieve adsorpting bed of the inlet amount of adsorption bed is vital.For solving this difficult problem, the present invention proposes thermal coupling condensation evaporation technology.
The thermal coupling condensation evaporation process that the present invention proposes is made up of thermal coupling interchanger, evaporation fresh feed pump, under meter, regulating and controlling valve and corresponding connection line, according to the difference that evaporation is provided with, lime set receiving tank, evaporation vapor-liquid separation tank etc. can be set also.From the vapour phase alcohol of rectification working process, enter the hot side of thermal coupling interchanger, vapour phase alcohol condensation when giving the heating of liquid phase vaporized alcohol.The alcohol lime set is by transferpump, sends into the cold side of thermal coupling interchanger through the flow control of strictness, is subjected to thermal evaporation.Vapour phase alcohol after the evaporation enters the molecular sieve adsorbing and dewatering operation.
The thermal coupling condensation evaporation process that the present invention proposes has three big technical superioritys, and the first, carry out the condensation evaporation operation with the thermal coupling process, do not consume and add heat, reached energy saving purposes; The second, thermal coupling condensation evaporation process is divided into two independently systems with rectification working process and molecular sieve adsorbing and dewatering operation on pressure, avoided mutual pressure interference, has guaranteed the smooth running of former and later two operations; The 3rd, realized the accurate control of molecular sieve adsorbing and dewatering operation inlet amount, guaranteed the dehydrating effect of adsorption bed and stablizing of product.
The pollution that the discharging of useless mash causes is to perplex the difficult problem of industry actually always, is seriously restricting the development of alcohol industry.For the production of extensive fuel alcohol, this contradiction will be more outstanding.Useless mash processing mode effectively is to carry out multiple-effect evaporation.But evaporative process always is the big power consumer, in useless mash treating processes, steam the water of wherein the overwhelming majority, and the height of energy consumption becomes one of key issue that influences the Production of Fuel Ethanol economic benefit.
The present invention utilizes the secondary steam that drying machine can produce in the wet poor drying process to carry out the technology that centrifugal clear liquid evaporates, and the live steam steam consumption that makes evaporative process is zero.This technology will be sent into settling centrifuge from the useless mash of ethanol refinery operation, carry out solid-liquid separation, isolate the solid formation in the useless mash.Isolated solid formation is sent into drying machine; Isolated centrifugal clear liquid partly returns fermentation procedure, and part is carried out multiple-effect evaporation and concentrated.It is the secondary steam that drying machine produces that multiple-effect evaporation concentrates required thermal source, and the concentrated solution-underflow of acquisition and centrifugation go out, and wet being pickled with grains or in wine sent into drying machine after mixing and carried out drying.The secondary steam that drying machine produces is as the thermal source of multiple-effect evaporation.The lime set of multiple-effect evaporation is returned powder slurry preparation section and is used for batching.The poor protein fodder that can be used as of doing of drying machine output is sold.
The problem that scabs of interchanger in the evaporative process always is the difficult problem of some evaporation element operation of puzzlement.Heat exchange surface scabs not only can cause the reduction of heat transfer efficiency, and will be forced to end ordinary production and go to carry out scar operation clearly, thereby causes the decline of throughput.Clear scar method commonly used has alkali cleaning, pickling and labor cleaning etc.Aforesaid method not only can improve process cost, and can cause secondary environmental pollution problems such as soda acid discharging.The vaporizer that the present invention adopts can guarantee the operation of vaporizer long period and do not scab, and has guaranteed high heat transfer efficient and continuous and stable production, and plant capacity is increased substantially.
In useless mash treatment process, can successfully utilize the atmospheric steam that produces in the drying process be one of key of this technology.The waste hot steam that the present invention will rotate Pipebundledrier is used for the multiple-effect evaporation of useless mash, has reached the purpose that cuts down the consumption of energy.
The effect of whizzer in the solid-liquid separation process is very important, but because the complicacy of its structure and required high reliability, always the focus that becomes producer and be concerned about, the present inventor adopts the give up solid-liquid separation of mash of homemade horizontal screw centrifuge, separation efficiency is higher, operational stability is more reliable, and successfully is applied to realize long period trouble-free operation among the large-scale commercial production.Reduce the facility investment of DDGS production equipment effectively, made it to have more economy.
The present invention open and the method and the technology of preparing that propose, those skilled in the art can be by using for reference this paper content, and links such as appropriate change raw material, processing parameter, structure design realize.Method of the present invention and technology are described by preferred embodiment, person skilled obviously can be in not breaking away from content of the present invention, spirit and scope to method as herein described with technology is changed or suitably change and combination, realize the technology of the present invention.Special needs to be pointed out is, the replacement that all are similar and change apparent to those skilled in the artly, they are regarded as being included in spirit of the present invention, scope and the content.
Claims (7)
1. a production of alcohol fuel is a raw material with starchiness or saccharic, comprises raw material processing, fermentation, rectifying, molecular sieve adsorbing and dewatering, useless mash treatment process composition; It is characterized in that: rectification working process is connected by thermal coupling condensation evaporation process with the molecular sieve adsorbing and dewatering operation, described thermal coupling condensation evaporation method is: the gaseous ethanol of rectification working process extraction, send into the molecular sieve adsorbing and dewatering operation by thermal coupling condensation, evaporative process, this condensation, evaporative process are finished by thermal coupling, the condensation liberated heat does not need to add in addition heat as the thermal source of ethanol evaporation.
2. production of alcohol fuel as claimed in claim 1 is characterized in that described thermal coupling condensation evaporation process is made up of thermal coupling condensation evaporation interchanger (6), evaporation fresh feed pump (7), under meter (8), regulating and controlling valve (9) and corresponding connection line; From the vapour phase alcohol of rectification working process, enter the hot side of thermal coupling condensation evaporation interchanger (6), vapour phase alcohol condensation when giving the heating of liquid phase vaporized alcohol; The alcohol lime set is sent into the cold side of thermal coupling condensation evaporation interchanger (6) by transferpump (7), is subjected to thermal evaporation, and the vapour phase alcohol after the evaporation enters the molecular sieve adsorbing and dewatering operation.
3. production of alcohol fuel as claimed in claim 1, it is characterized in that described raw material treatment process with starchy material comprises preparation of powder slurry and Dian Fentang liquefaction, wherein the preparation of powder slurry is that starchy material is pulverized, the water spice, the concentration of adjusting the powder slurry is dry matter content 20 ~ 35%, and pH value is 3 ~ 6.
4. production of alcohol fuel as claimed in claim 1 is characterized in that described is that the raw material treatment process of raw material is with the saccharic: saccharine material is adjusted to dry matter content 10 ~ 28% respectively, pH value 3 ~ 6.
5. production of alcohol fuel as claimed in claim 1 is characterized in that described fermentation procedure is that thick mash continuously ferments, and fermenting process carries out 30 ~ 33 ℃ of leavening temperatures in the fermentor tank of series polyphone.
6. production of alcohol fuel as claimed in claim 1 is characterized in that described rectification working process adopts wine with dregs tower and dehydration tower two tower thermal coupling rectification process, and dehydration cat head vapour is as the heating medium of wine with dregs tower reboiler.
7. production of alcohol fuel as claimed in claim 1 is characterized in that described molecular sieve adsorbing and dewatering operation adopts two or more adsorption beds, alternating temperature transformation adsorption dewatering.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CNB2004100940850A CN1298859C (en) | 2004-12-29 | 2004-12-29 | Production of alcohol fuel |
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| CNB2004100940850A CN1298859C (en) | 2004-12-29 | 2004-12-29 | Production of alcohol fuel |
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| CN1644703A CN1644703A (en) | 2005-07-27 |
| CN1298859C true CN1298859C (en) | 2007-02-07 |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101260412B (en) * | 2008-04-07 | 2012-02-29 | 宁夏西部光彩新能源高新技术有限公司 | Technique for brewing alcohol |
| CN101538588B (en) * | 2009-03-24 | 2012-05-23 | 四川恒泰企业投资有限公司 | Technology for coupling the liquefaction process of corn alcohol and the concentration process of vinasse clear liquid |
Families Citing this family (16)
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|---|---|---|---|---|
| CN101157890B (en) * | 2007-08-14 | 2011-05-25 | 天津大学 | Fuel ethanol production equipment and method |
| CN101487024B (en) * | 2008-01-15 | 2013-03-06 | 中粮集团有限公司 | Method for preparing ethanol from tuber crops raw material |
| CN101487026B (en) * | 2008-01-15 | 2013-03-06 | 中粮集团有限公司 | Method for preparing ethanol from tuber crops raw material |
| CN101487025B (en) * | 2008-01-15 | 2011-09-28 | 中粮集团有限公司 | Method for preparing ethanol from tuber crops raw material |
| CN101487027B (en) * | 2008-01-15 | 2013-03-06 | 中粮集团有限公司 | Method for preparing ethanol from tuber crops raw material |
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| CN101245354B (en) * | 2008-03-26 | 2011-03-16 | 天津大学 | Novel method for producing ethanol with potato raw material |
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| CN101676396B (en) * | 2008-09-19 | 2013-03-06 | 中粮集团有限公司 | Method for preparing alcohol by utilizing potato materials |
| CN102220378B (en) * | 2010-04-16 | 2013-07-03 | 中粮集团有限公司 | Method for preparing alcohol |
| CN102040472B (en) * | 2010-11-17 | 2013-07-10 | 蓝仁水 | Energy-saving process for rectifying alcohol by adopting heat integration of three rectifying columns |
| CN102174631B (en) * | 2010-12-30 | 2014-01-08 | 吉林省农业科学院 | Method for improving yield of ethanol produced by sugar beet fermentation |
| CN105400827A (en) * | 2015-11-24 | 2016-03-16 | 广西罗城科潮基业科技发展有限公司 | Method for making ethyl alcohol with beet molasses |
| CN107058403A (en) * | 2017-06-22 | 2017-08-18 | 广西中粮生物质能源有限公司 | A kind of distiller's grains liquor is used for the method that full amylofermentation prepares ethanol |
| CN110066215B (en) * | 2019-04-30 | 2022-09-27 | 天津大学 | Heat coupling integration method for fuel ethanol production process based on wet grains product |
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| CN1067432C (en) * | 1996-11-25 | 2001-06-20 | 无锡轻工大学 | Dense mash fermenting alcohol producing method |
| CN1436815A (en) * | 2002-02-07 | 2003-08-20 | 四川大学 | Prepn of lateral hydroxyl group containing polyimide/SiO2 hybrid film |
| CN1438208A (en) * | 2003-03-18 | 2003-08-27 | 范希中 | Methanol fine-distillation technology and fine-distillation apparatus |
| CN1164547C (en) * | 2002-04-29 | 2004-09-01 | 天津大学 | Alcohol refining process for producing several products |
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| CN1067432C (en) * | 1996-11-25 | 2001-06-20 | 无锡轻工大学 | Dense mash fermenting alcohol producing method |
| CN1436815A (en) * | 2002-02-07 | 2003-08-20 | 四川大学 | Prepn of lateral hydroxyl group containing polyimide/SiO2 hybrid film |
| CN1164547C (en) * | 2002-04-29 | 2004-09-01 | 天津大学 | Alcohol refining process for producing several products |
| CN1438208A (en) * | 2003-03-18 | 2003-08-27 | 范希中 | Methanol fine-distillation technology and fine-distillation apparatus |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101260412B (en) * | 2008-04-07 | 2012-02-29 | 宁夏西部光彩新能源高新技术有限公司 | Technique for brewing alcohol |
| CN101538588B (en) * | 2009-03-24 | 2012-05-23 | 四川恒泰企业投资有限公司 | Technology for coupling the liquefaction process of corn alcohol and the concentration process of vinasse clear liquid |
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| CN1644703A (en) | 2005-07-27 |
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