THERMOCHEMICAL CONVERSION OF BIOMASS TO ETHANOL

Abstract: Method for thermochemically converting a carbohydrate material into ethanol wherein the carbohydrate material and a metal salt are reacted at elevated temperature to form an intermediate carbohydrate complex salt and/or a lactate metal salt which then is pyrolyzed in the presence of water into ethanol. Preferred carbohydrate materials for the process are various sugars and the metal salt preferably is a metal oxide, hydroxide, or carbonate. The intermediate complex and/or lactate salt may be separated from its aqueous reaction mixture prior to its pyrolysis to reduce the ultimate separation of ethanol from water. Alternatively, the metal of the metal salt may be one whose carbonate decomposes to metal oxide and carbon dioxide during the pyrolysis step of the process to generate said metal salt in situ.

Description: THERMOCHEMICAL CONVERSION OF BIOMASS TO ETHANOL Background of the Invention The present invention relates to the synthesis of ethanol from biomass and, more particularly to such synthesis by a catalytic thermochemical process. Conversion of biomass to ethanol by fermentation techniques is a well practiced process, especially with the emerging importance of gasohol in today's economy. Conventional fermentation techniques, however, suffer from a number of drawbacks including, for example, protracted reaction times, the need for sterile reaction conditions, the need for purified feedstocks, the production of voluminous by-products, and an energy intensive distillation operation for recovery of ethanol from water. The need for an alternate route for converting biomass to ethanol thus exists. Unfortunately, no alternative process has emerged in the marketplace. In studying the reaction mechanisms involved in fermentation of sugar, it has been reported that an aqueous solution of some sugars can be converted to lactic acid in the presence of an alkali metal or alkaline earth metal hydroxide or oxide. Montgomery and Ronca, "Chemical Production of Lactic and Other Acids from Molasses", Industrial and Engineering Chemistry, Vol. 45, No. 5, pp 1136-1147 (1953) and references cited therein. In other unrelated research, it has been reported that certain alkali metal or alkaline earth metal lactate salts could be decarboxylated to produce a mixture of several organic liquids and gases and on occasion some ethanol. Hanriot, "Sur la decomposition pyrogenee des acides de la serie grasse", Nouv. Ser. T. XLV, Societe Chimique, pp 79-81 (1886); Buchner and Meisenheimer, "Die chemischen Vorgange bei der alkoholischen Gahrung" Berk, deut. chem. Ges., 38, t! 620-630 (1905); and Fischer, Schrader and Wolter, "Uber die Entkarboxylierung der tt Milschaure, Gesa m. Abh. Kenntnis Kohle, 6, 99-107 (1923). For further studies on lactic acid as it may relate to fermentation of sugars, reference is made to the text by C.H. Holten, Lactic Acid: Properties in Chemistry of Lactic Acid and Derivatives, Verlag Chemie, GmbH, Copenhagen, Denmark. SUBSTITUTE /— - ~ ~ r-v — - , The present invention has solved the long standing problem of convertin biomass into ethanol by a process which does not involve fermentation. Als substantially all of the disadvantages inherent in conventional fermentation o biomass are obviated by the present invention. Broad Statement of the Invention The present invention is a method for therm ochemically converting a carbo hydrate material into ethanol. Such method comprises establishing an aqueou reaction mixture of the carbohydrate and a metal salt in a reaction zone held a elevated temperature to form an intermediate metallic complex (eg. metalli sucrate) and/or a metallic laetate salt. The metallic salt then is separated from th reaction mixture and pyrolyzed in a pyrolysis zone in the presence of water to for said ethanol. Suitable carbohydrate materials are sacchariferous materials such a monosaccharides, polysaaccharides, and oligosaccharides. Another aspect of th present invention involves the thermochemieal conversion of the carbohydrat material into ethanol " wherein the carbohydrate material, the metal salt, and wate are established in a reaction zone for the one-step conversion of the carbohydrat material into ethanol. In this aspect of the invention the metal of the metallic sal is restricted to a metal which when formed into the by-product metallic carbonate such carbonate will be decomposed in situ to generate a metallic oxide or hydroxide A further aspect of the present invention is a method for making a liqui combustible fuel blend of combustible (fossil) fuel (eg. fuel oil, diesel fuel, kerosene gasoline, etc.) and ethanol, though preferably a gasoline-alcohol blend (gasohol) wherein the ethanol is made by the thermochemieal conversion of a carbohydrat material as described above and the product ethanol is blended with the combustibl fuel, eg. gasoline. Advantages of the present invention include quick reaction times for convert ing carbohydrate feed into ethanol and specifically the ability to reduce the reactio time for making ethanol from 16-24 hours by conventional fermentation to a matte of minutes by the thermochemieal process of the present invention. Anothe advantage of the present invention is the ability to efficiently and effectivel operate with impure carbohydrate feeds which cannot be tolerated by conventiona fermentation techniques. A further advantage is the ability to convert man carbohydrate materials into ethanol which are unsuitable as feedstock for con ventional fermentation production of ethanol. A still further advantage of th present invention is the probable volumetric reduction of by-products from th present invention, especially compared to by-products, such as stillage, from con¬ ventional fermentation techniques. Yet another advantage is the minimization of energy consumption required for purification of the ethanol product. These and other advantages will become readily apparent to those skilled in the art based on the disclosure herein contained. Detailed Description of the Invention The process of thermochemically converting carbohydrate material feedstock into ethanol involves multiple chemical reaction steps which means flexibility in designing different operational modes for practicing the present invention. Though dominant chemical reactions can be attributed to the production of ethanol from carbohydrate feedstock, it should be recognized that competing reactions do occur during the process which often lead to by-products and lower yields of ethanol. In order to more fully appreciate the chemistry involved in the thermochemieal process of the present invention, the following postulated reactions for the process are given. It should be understood that such reactions are given for purposes of illustration only and are not to be interpreted as a limitation on the present invention. Such chemical reaction steps in the present process are as follows: (1) Carbohydrate + Metal Salt Metal Carbohydrate Complex (2) Metal Carbohydrate Complex Metal Lactate (3) Metal Lactate + H„0 — — Ethanol + Metal Carbonate (4) Metal Carbonate Metal Oxide + CO Several observations can be made based upon the foregoing reaction steps. Initially, it can be seen that a metal carbonate salt results during the ethanol production step and that such carbonate salt can be converted by conventional techniques to metal oxide (or hydroxide) plus carbon dioxide. In practical terms this means that while a wide variety of metal salts can be used in the process, clearly oxide salts may be preferred in order to take advantage of the renewable source of oxide resulting in the process. Such renewable source of the metal salt may be understood further by reference to a specific embodiment of the present invention wherein sucrose is converted into ethanol utilizing calcium oxide catalyst. With such reactants for the process, the chemical reaction steps involved are as follows: (la) Sucrose + CaO Ca„Sucrate (2a) Ca„Sucrate Calcium Lactate (3a) Calcium Lactate + H„0 Ethanol + CaCO. (4a) CaCO, CaO + CO, It should be clearly understood that the foregoing chemical synthesis utilizin sucrose and calcium oxide feed materials is for purposes of illustrating the presen invention and is in no way a limitation on the present invention. From suc chemical reaction steps, it can be seen that the calcium oxide catalyst is renewable product from the process which clearly provides certain economies t practice of the present invention. The term "catalyst" to describe the metallic sal herein is used in the sense that there is no net consumption of the metallic salt i the process as the metallic salt is regenerable to its oxide or hydroxide form. Based upon the foregoing reaction mechanisms postulated for the presen invention, it can be seen that the present process possibly can be operated in step wise fashion (assuming the ability to isolate the various products of the individua reaction steps). One of the clear advantages of the present invention is th discovery that by judicious selection of the reaction conditions prevailing in th process (for example, temperature, pressure, time, and the like), the present proces indeed can be operated in a distinct step-wise method following the chemica reactions outlined above. Moreover, the present process has the flexibility to b operated in various combinations of the reaction steps given above for additiona flexibility in operating the process efficiently and economically based upon availa bility of equipment, various carbohydrate feedstocks, various metal salts, and th like. Thus, the present process can be optimized for various combinations o reactants and reaction conditions available to any operator of the process. Con ventional fermentation techniques for conversion of sugar to ethanol clearly do no have the choice of the various operational modes available to the present invention. The individual chemical reaction steps involved in the process can be combine in several ways for the production of ethanol. Various of these combinations provid distinct advantages over other combinations as will be readily apparent to thos skilled in this art. For example, the four chemical reaction steps can be operate individually, the first and second steps can be operated together, the first thre steps can be operated together and the like. In fact by selection of the appropriat metal for use in the process, the fourth step will occur in situ under the reactio conditions prevailing in the process. An advantage of isolating the metal carb hydrate complex from step (1) would be to reduce the volume of water typicall present in this step which would make ultimate separation of product ethanol fro <*-*•• sJ water a less energy intensive operation. The same advantage can be realized also by operating the first two steps together for recovery of the metal lactate. Various other combinations clearly can be conceived by those skilled in the art based upon the disclosure herein contained. It is of note, though, that maximization of yields from the individual steps and/or purification may be achieved by a step-wise practice of the process rather than a one-step direct conversion of carbohydrate feedstock to ethanol. Suitable carbohydrate feedstock material for the present invention most often will be saecharides and often the term sugar will be used for their description. Simple monosaeeharides for use in the present process include hexoses such as, for example, glucose, mannose, gallactose, gulose, formose, and fructose; pentoses such as, for example, arabinose, xylose, ribose, and rhamnose; tetroses such as, for example, erythrose and threose; and trioses such as, for example, glycerose. Derivatives of saecharides such as, for example, gluconic acid, mono-, and di- phosphatates of fructose, etc., also can be used in the process. It should be noted that conversion of pentose sugars (for example hemicellulose from wood hydrolysis) by the preserft process will result in the production of one mole of a lactate salt and probably one mole of a glyeolate salt from reaction step (2). The thermochemieal decomposition of such salts would yield one equivalent of ethanol and one equivalent of methanol which mixture would be suitable as a fuel ingredient. The important consideration in the use of pentose sugars is that they will not poison the reaction which occurs with conventional fermentation processes because of the effect of by¬ product furfuraldehyde. Additional carbohydrate feedstock include disaccharides such as, for example, sucrose, maltose, and the like. Other suitable feedstock include polysaccharoses and oligosaccharides. Such sugars can be derived from sugar crops such as sugar cane, sugar beets, or sweet sorghum; or by the partial or complete hydrolysis of starch or starch-like materials in grains such as corn, wheat, oats, and the like; or can be derived from other crops such as potatoes, yams, manioc, and the like. Additional sugars suitable as feedstock for the present invention can be derived from lignoeellulosic materials such as agricultural and forestry residues or by-products such as, for example, corn stalks or corn cobs, sawdust and other forest residues, bagasse, cattle or other manure, leaves, newspaper from municipal waste, and the like. Such agricultural and forestry residues preferably are hydrolyzed or at least partially hydrolylzed to sugars or oligosaccharides prior to their admission to the present process. The present process also may utilize soluble polysaccharides cr* such as, for example, soluble starch or polysaccharides that have been pretreated reduce the degree of crystallinity (e.g. amorphous cellulose). _ Thus, it can be seen that a myriad of materials can be used directly converted into suitable feedstock for use in the present process. Such materia need not be rigorously purified for admission into the process as is required conventional fermentation processes, because typical fermentation poisonous mat rials do not interfere with the thermochemieal process of the present invention. Suitable catalysts for use in the present invention are those metal salts th can display a basic reaction in an acidic environment. Preferable catalysts a oxides, hydroxides, and carbonates of alkali metals and alkaline earth metals. F present purposes, alkali metals include lithium, sodium, potassium, rubidium, a cesium; and alkaline earth metals include beryllium, magnesium, calcium, strontiu and barium. Additional catalysts useful in the present invention include salts amphoteric or transition metals such as salts of, for example, aluminum, zinc, lea barium, cadmium, magnesium, mercury, silver, cobalt, manganese, bismuth, galliu niobium, copper, iron, nickel, and the like, preferably provided as an oxid hydroxide, or carbonate. Further suitable metallic salts include complex metall salts which contain one metal plus either a second metal or non-metal or oth anion. Representative anions of such complex metallie salts, for example, can selected from the following: arsenate, chromate, ferricyanide, carbonate, silicat molybdate, (dibasic, tri-basic, pyro, meta, ortho) phosphate, plumbite, sulfat aluminate, bisulfite, (meta or tetra) borate, chlorate, chloraurate, chloroplatinat dithionate, manganate, nitrite, selenate (meta or ortho) silicate, stannate, sulfit tartrate, thiocyanate, thiosulfate, tungstate, vanadate, and the like. Even mor complex metallic salts such as salts of heteropolyacids (eg. sodium salt phosphomolybdic acid) may be useful in the process also. It should be recogniz that combinations of such salts can be used as well as materials which generate th suitable salt in the reaction mixture in situ. As previously noted based upon the chemical reaction steps involved in th process, metal oxides may be preferred for use in the process since metal oxides ca be generated from the process for recycle thereto. Moreover, for continuo operation of the present invention selection of a metal whose carbonate decompos to metal oxide and carbon dioxide gas under the reaction conditions prevailing in th process may be desired for self-generating catalysts for the process. Such met carbonates include, for example, magnesium carbonate, zinc carbonate, copp carbonate (possibly complexed with Cu(OH)„), cadmium carbonate, mercuro carbonate, silver (I) carbonate, cobalt (π) carbonate, iron (π) carbonate, manganese carbonate, nickel carbonate, and lead carbonate, which can be decomposed at the pyrolysis temperatures of the process. Since water is involved in the pyrolysis of the metallic lactate to ethanol and metal carbonate salt, water is the preferred solvent of choice for use in the present process. It should be recognized, however, that excessive quantities of water in the reaction mixture may not be desirable because of later separation problems of product ethanol from water-ethanol mixtures. It, then, may be desirable to employ suitable organic solvents in the process to aid in subsequent purification efforts for recovery of the desired ethanol product. Such organic solvents preferably are water soluble though this is not necessary. A particularly preferred organic solvent for use with water as a solvent system in the present invention is ethanol since ethanol is the product being made. While a solvent is not strictly required for production of the metal lactate from the carbohydrate feedstock, many carbohydrate feedstock materials for use in the present process will be in aqueous form and thus more often the entire process will be conducted in an aqueous solvent. It should be recognized, however, that in the chemical pyrolysis of the metal lactate to ethanol that the water required for the process may be in the vapor phase. Reaction conditions for the present process include temperatures ranging from between about 150° to about 400°C. and above. The actual temperatures employed in the process will depend necessarily upon which reaction steps are being run concurrently and upon the particular feedstock and metal salt employed in the process. Preferred reaction temperatures for the overall process range from about 275 to 400 C. Since such elevated temperatures are required for the process, pressures preferably will be in the superatmospheric range especially when it is desired to retain the aqueous solvents in the process in the liquid phase. It should be recognized that atmospheric pressure and pressures slightly above atmospheric may find use in the present process. Preferable pressures range from about 500 to about 3,000 psig, though it may be convenient in running the process to maintain autogenous pressure. Again, the pressure used in the process will depend necessarily upon the other reaction conditions and reactants used in the process. The process additionally may be conducted under an inert gas blanket or inert atmosphere especially when the process is conducted in several distinct stages. Such inert gas atmosphere minimizes side reactions in the process. Suitable inert or non-reactive gases in the process include, for example, nitrogen, carbon dioxide, propane, argon, and the like and even mixtures thereof. SUBS ~t T ~ ?i~ ιB r i ? " •"" ' The primary product of the present invention is ethanol though a variety other products and by-products normally will result from the process. One su product is a metal carbonate which suitably is converted to additional metal oxi for use in the process. Other products that may be produced by the process includ for example, methanol and 2,4-dihydroxy-3-pentanone. It will be appreciated th the particular by-products resulting from the process will necessarily depend up particular reactants used in the process and especially the carbohydrate feedsto of choice, upon the particular reaction conditions maintained in the proces whether the process is run in distinct steps or as a one-step direct conversi ethanol process, and the like. Such additional organic products produced by t process may be separated from the ethanol by fractionation techniques includi (molecular) distillation and crystallization, or can be left with the product ethan for use as a fuel additive or as a chemical feedstock for additional processing. In practicing the present process, it should be recognized that yields of t products resulting from the various reaction steps necessarily also depend upon t concentration of the reactants used as well as the other reaction conditions (e. tirtie, temperature, pressure, etc.). In the formation of the metal lactate, pri work has shown that yields thereof depend upon the concentration of both t carbohydrate feedstock and the metal salt catalyst, as would be expected. Since t other reaction conditions established in the process (e.g. time, temperature, a pressure) appear to control the yields of products and by-products in the prese process to a greater extent than the particular ratio of reactants used, t proportion of reactants used in the process will be adjusted accordingly. It important to note, however, that sufficient water must be present during t pyrolysis of the metal lactate salt intermediate in order to achieve the requir ethanol and metal carbonate products. Such proportion of water, though, should n be excessive as subsequent purification efforts of the ethanol would be retarde thereby. In connection with the various operational modes which can be designed f the process based on the series of reaction steps given above, it will be appreciate that a variety of equipment can be interconnected for reducing such operation modes to commercial practice. In order to further illustrate several present preferred operational modes and typical equipment suitable for implementation such modes, the following process systems discussion is given. For a one-ste process for directly converting carbohydrate feedstock into product ethanol, th carbohydrate feedstock suitably in an aqueous solvent can be fed along with t metallic salt, preferably as an aqueous slurry or solution, to an agitated reaction vessel having freeboard space above the liquid level maintained therein. With the reaction vessel maintained at operating conditions, an ethanol product stream containing ethanol, carbon dioxide, water, and other volatile material can be vented from the freeboard space within the reactor continuously while the carbohydrate feedstock is fed to the reaction vessel continuously. Metal carbonate product formed from the reaction can be removed as an underflow from the reaction vessel and sent to a combustion zone using coal, biomass, or other convenient fuel to regenerate metal oxide and carbon dioxide gas therefrom. The metal oxide then can be recycled to the reaction vessel on a continuous basis, if required. Alternatively, for those metal carbonates which will decompose under the reaction conditions (for example, zinc carbonate at about 300°C, copper carbonate at about 200 C, and the like), the metal oxide will be regenerated in situ in the reactor so that at most only make-up metal salts should be required to be passed into the reaction zone. Separation of the ethanol from the ethanol product stream is practiced as described above. Alternatively, for insoluble or slightly soluble metal salts, a fixed bed of the catalyst metal salt can be maintained within a flow reaction vessel of suitable design (e.g., a tubular flow reactor) and an aqueous solution or dispersion of the carbohydrate material passed therethrough with the aqueous ethanol product stream withdrawn therefrom. For a two-step process wherein either a metallic carbohydrate complex of the metal salt (eg. a metallic sucrate) or metallic lactate salt is recovered and thence converted into product ethanol, the carbohydrate feedstock and metallic salt can be fed to a reaction vessel such as described for the one-step process. Following the production of the metallic sucrate salt or metallic lactate salt, the reaction mixture can be conventionally cooled for precipitation of the salt therefrom. Other methods for separation of the solid salt from the reaction mixture include evaporation or distillation of the aqueous phase therefrom. Other conventional separation tech- niques additionally may be employed. Separation of the precipitated salt from the aqueous reaction mixture effectively reduces the amount of water carried forward in the process for reducing the load placed on the ethanol purification step of the process. Even with separation of the salt by distillation of the aqueous phase from the reaction mixture, a less energy intensive process results because this distillation separation step requires no reflux nor is it an azeotropic distillation, which techniques are required in conventional fermentation production of ethanol for its SUBSTITUTE ε: separation and recovery from water. With production of a metal lactate salt by t two-step process, such recovered salt can be pyrolyzed to product ethanol described above. With separation and recovery of a metallic sucrate salt, such sa can be converted to product ethanol in a one-step process or can be converted to t metallic lactate salt which can be recovered and the recovered lactate sa pyrolyzed to product ethanol. Possible optimization of yields of the vario intermediates may be realized by such distinct step-wise practice of the process well as a reduction of the proportion of water carried forward in the process. The recovery of the intermediate metallic carbohydrate complex (eg. metalli sucrate salt) and metallic lactate salt separately may be termed a multi-ste process for production of ethanol according to the present invention. The metalli lactate salt, whether produced directly from the carbohydrate feedstock or pr duced from the recovered metallic sucrate salt intermediate, can be pyrolyzed t ethanol utilizing a variety of equipment. For example, a fluidized bed of th concentrated metallic lactate salt, optionally containing inert solids or oth reactant solids (eg. metal salt catalyst), can be established utilizing a supporting g of carbon dioxide or the like preferably containing steam for providing the wate necessary or the pyrolysis reaction to occur as desired. The ethanol product strea would be • vented from the reactor and sent to purification operations. Soli withdrawn from the fluidized bed can include the metal carbonate product or met oxide, depending upon the particular metal utilized in the process and the particul pyrolysis conditions established in the fluidized bed reactor. Alternatively, falling-bed type reactor also could be employed as well as could any oth convenient gas-solids reactor. In order to more fully appreciate the process of the present invention, th following illustrative design example for converting sugar to ethanol utilizing a lim catalyst by the two-step process of the present invention wherein the calciu lactate intermediate is recovered, is given. An aqueous sugar (sucrose) solution i fed to a tubular flow reactor maintained at about 250°C. along with a flow o recycled lime (calcium oxide) and optionally recycled water. The residence time o the reactants in the tubular flow reactor is about 2 minutes. The aqueous reactio mixture withdrawn from the tubular flow reactor is sent to a flash evaporator an preeipitator wherein water is flash-evaporated from the reaction mixture and th calcium lactate is precipitated therefrom. The water may be recycled directly t the tubular flow reactor or can be used to form additional aqueous sugar feedstoc for the process. The concentrated calcium lactate is sent to a fluidized pyrolysi bed maintained at about 250°C. for about 1 minute residence time. Solids in the fluidized pyrolysis bed are maintained in random motion utilizing carbon dioxide gas recycled from a later step of the process. Ethanol, carbon dioxide, water and other volatile by-products are vented from the fluidized pyrolysis bed and sent to purification operations for recovery of product ethanol. Limestone (calcium carbonate) withdrawn from the fluidized pyrolysis bed is sent to a lime kiln, optionally along with a flow of miscellaneous chemicals recovered from the ethanol purification operations. Additionally, bagasse or other convenient fuel can be combusted in the kiln for converting the limestone into lime (calcium oxide) and carbon dioxide gas which is used to fluidize the solids in the fluidized pyrolysis bed. The regenerated lime then can be sent back to the tubular flow reactor as indicated above. Again, it will be appreciated that this conceptual process mode is given for purposes of illustration and not by way of limitation of the present invention. Materials of construction for the various zones are conventional for this type of high temperature, high pressure operation. Thus, where corrosion-resistant materials are required, use of austenitic stainless steel, plastic, glass-lined steel, wood, or even clay may be used. Concrete or steel can be used where corrosion or erosion is inconsequential. Piping, ductwork, and other appurtenant lines will be of similar material, conventionally constructed. It will be appreciated that various of the tanks, lines, reactors, and the like can be multiple, series, cascade, or parallel connected for additional treating time or capacity, or for special effects. The following examples show how the present invention can be practiced but should not be construed as limiting. In this application, all proportions, percentages, and ratios are by weight, and all units are in the metric system unless otherwise expressly indicated. EXAMPLE 1 Conversion of Sucrose to Ethanol A one gallon, stainless steel, Autoclave Engineers' magna drive autoclave was set up with both vapor phase and liquid phase sampling tubes. The liquid phase dip tube was arranged so the line could be back-flushed with nitrogen. In the glass liner of the autoclave was placed 137 grams of sucrose (table sugar), 118.6 grams of calcium hydroxide and 580 ml of deionized water. An additional 100 ml of deionized water was placed between the liner and the autoclave. The autoclave was purged twice with nitrogen and the pressure was returned to atmospheric. The autoclave was heated, with stirring, for two hours to 300°C. An 18.0 gram sample of tan liquid was then removed. This is referred to as the zero time sample. The reac temperature was maintained at 300° 3°. Additional samples were taken at t following times (after zero time sample): 30 mins (13.7 gm), 1 hr (15.1 gm), 2 (15.1 g ), 3.5 hrs (17.8 g), 5 hrs (17.6 gm). A vapor sample (12.9 gm of condens liquid) was also removed at 5 hours. The heater and stirrer were shut off and t autoclave was allowed to cool down overnight. The residual slurry in the glass lin was 516 grams and an additional 157 grams of material was recovered from betwe the autoclave and glass liner. Also 15 grams of material was recovered by flushi the lines. The total material recovered was 798 grams compared to 935.6 gra charged. Some of the samples were analyzed for ethanol by gas chromatography. O ml of each of the samples was diluted up to 10 ml with deionized water in a 10 volumetric flask. The G.C. analyses were carried out on a Varian model 1400 with a 10 percent Carbowax 20M glass column 10 feet long. The column was heat to 80°C. The ethanol was identified by comparing retention time with an etha standard. The concentration of- the ethanol was calculated using a standard cur based on 1000 ppm, 500 ppm, and 100 ppm levels of ethanol standards. T following results were obtained: Ethanol as Weight Sample Time Sample Percent of Volatile (hr) Weight (gm) Organics Ethanol (ppm) 0 - liquid 18.00 66 1700 2 - liquid 15.1 57 2500 5 - liquid 690.6 50 2700 5 - vapor 12.9 16000 The above-tabulated results clearly show that ethanol can be made direct from sucrose by a one-step reaction process. Thus, the chemistry of the reaction established. EXAMPLE 2 Conversion of Sucrose to Ethanol To a one liter, stainless steel, autoclave (like that autoclave described Example 1) was charged 111 gms of sucrose (table sugar), 73 gms of calcium oxid and 405 ml of deionized water. The autoclave was pressure tested with nitrogen 2,000 psig and the pressure returned to atmospheric. The autoclave was heate with stirring, for 1.5 hours to a temperature of 300°C. The reactor temperatu then was maintained at 300° + 1°C for an additional one hour. The heater and stirrer were shut off and the autoclave allowed to cool down overnight. The residual liquid slurry in the autoclave weighed 581 gms compared to the 589 gms of material that was originally charged to the autoclave. The residual slurry was filtered by gravity to remove solids and the liquid filtrate analyzed for ethanol by the gas chromatography procedure described in Example 1. The liquid sample was found to contain 9,100 mierograms of ethanol per milliliter of liquid. Also, 67% by weight of the volatile reaction product mixture evolved during the course of the reaction was determined to be ethanol. Again, the chemistry of the reaction is established in this example. EXAMPLE 3 Conversion of Sucrose to Ethanol To the one liter autoclave described in Example 2 was charged 74 gms of sucrose, 70 gms of sodium hydroxide pellets, and 500 ml of deionized water. Oxygen then was introduced into the head space in the autoclave to a pressure of 400 psig. The reactor was heated to 267°C over a three hour time period. At this temperature the autoclave pressure was determined to be 1,000 psig. The autoclave was maintained at 267° + 5°C with stirring for an additional 95 minutes during which time the pressure in the autoclave dropped to about 725 psig. A total of 626 gms of liquid slurry was recovered from the reaction mixture which represents over 97% of the 644 gms of material initially charged to the reactor. The slurry was filtered and the filtrate analyzed for ethanol by the gas chromatography technique described in connection with Example 1. The filtrate was determined to contain 7.0 gms of ethanol. Also, ethanol represented 94.7% by weight of the volatile organic materials in the reaction product. Again, the chemistry of the reaction is demonstrated in this example. EXAMPLE 4 Conversion of Sucrose to Ethanol To the one liter autoclave described in Example 2 was charged 111 gms of sucrose, 106 gms of zinc oxide, and 405 ml of deionized water. The autoclave was sealed and pressure checked at 2,000 psig with nitrogen gas. After releasing the pressure to atmospheric, the reactor was heated to 300°C over a 70 minute time period, and then maintained at 300° + 2°C for 6 hours. After the autoclave had cooled to room temperature overnight, there was a residual pressure in the TCTREA ? OMPI autoclave of 400 psig. This pressure is due to carbon dioxide gas being released the decomposition of zinc carbonate under the reaction conditions. Note that Examples 1 and 2 the pressure in the reactor upon its cooling was not abo atmospheric pressure which is consistent with the formation of calcium carbonate the reaction which is not decomposable under the reaction conditions. Also, ther was no increase in the autoclave pressure in Example 3 following termination of t reaction which again is consistent with the formation of by-product sodiu carbonate which is not decomposable under the reaction conditions. A total of 584 gms of liquid slurry was recovered from the autoclave. T filtrate was analyzed by the gas chromatography procedure described above an found to contain 830 micrograms per milliliter of ethanol. Accordingly, th example demonstrates the one-step direct conversion of biomass to ethanol utilizi a metal salt whose carbonate is decomposable under the reaction conditio established in the reactor. This means that the reactor need only be charged wit additional carbohydrate feedstock (and perhaps water) continuously for producin ethanol since the metal salt is continuously regenerated in the process. EXAMPLE 5 Conversion of Starch to Ethanol The one liter autoclave described above was charged with 115 gms of solubl starch, 93 gms of cuprous, oxide, and 405 ml of water. The autoclave was pressur tested and then heated to the reaction temperature used in Example 4. After th autoclave was cooled to room temperature overnight, there was a residual pressur of 275 psig therein due to carbon dioxide gas in the autoclave. This carbon dioxid gas is produced by the decomposition of cuprous carbonate which is formed in th reaction to regenerate the cuprous oxide catalyst. The liquid slurry was recovere from the autoclave and determined to weigh 568 gms. Gas chromatography analys revealed that the liquid slurry contained 180 micrograms per milliliter of ethano The results of this example show that a complex carbohydrate feedstock (starch) ca be successfully directly converted to ethanol according to the precepts of th present invention. The results of this example further demonstrate that cupro oxide used in the process can be continuously regenerated from its corresponding b product carbonate formed in the process.

Claims: CLAIMS 1. A method for thermochemically converting a carbohydrate material into ethanol which comprises: (a) establishing an aqueous reaction mixture of said carbohydrate material, water, and a metal salt in a reaction zone held at elevated temperature to form an intermediate carbohydrate complex of said metal and/or a metallic lactate salt; (b) separating said complex and/or lactate salt from said reaction mixture; (c) admitting said separated complex and/or lactate salt and water into a pyrolysis zone, the temperature in said zone being adequate to provide said water as a vapor and to pyrolize said complex and/ or salt to form ethanol, the proportion of water in said zone being restricted to be not in substantial excess over that proportion required for formation of said ethanol and by-product metallic carbonate; and (d) removing said ethanol from said pyrolysis zone; provided that when said metal of said metallic salt is restricted to a metal whose carbonate decomposes under said conditions in said pyrolysis zone of step (d), then optionally step (a) is conducted under reaction conditions of a temperature, a pressure, and for a time adequate for said ethanol and by-product metallic carbonate to be formed in said reaction zone wherein said metallic carbonate decomposes to generate a metallie oxide or hydroxide in situ. 2. The method of claim 1 wherein said carbohydrate material is a sac- chariferous material. 3. The method of claim 2 wherein said sacchariferous material is a monosaccharide, a polysaccharide, or an oligosaecharide. 4. The method of claim 2 wherein said sacchariferous material is derived from lignocellulosic material. 5. The method of claim 1 wherein an organic cosolvent is used in said reaction mixture established in said reaction zone. 6. The method of claim 5 wherein said eosolvent is ethanol. 7. The method of claim 1 wherein said metal salt is a metal hydroxide oxide, or carbonate. 8. The method of claim 7 wherein said metal of said metal salt is an alkal metal or alkaline earth metal. 9. The method of claim 7 wherein said metal of said metal salt is calcium sodium, aluminum, or barium. 10. The method of claim 7 wherein said metal of said metal salt is selecte from magnesium, zinc, copper, lead, cadmium, mercury, silver, cobalt, iron manganese, and nickel. 11. The method of claim 1 wherein said complex and/or lactate metal sal formation of step (a) is conducted at a temperature of between about 150° an 300°C. 12. The method of claim 1 wherein said pyrolysis step (c) is conducted at temperature of between about 275° and 400 °C. 13. The method of claim 1 wherein said complex and/or lactate metal sal formation of step (a) and said pyrolysis of step (c) are conducted, independently, at pressure of between about 500 and 3000 psig. 14. The method of claim 10 wherein said metal of said metallic salt i restricted to a metal whose carbonate decomposes under said conditions in sai pyrolysis zone of step (d) and said process is conducted according to step (a) unde reaction conditions of a temperature, pressure, and time adequate for ethanol an by-product metallic carbonate to be formed wherein said metallic carbonat decomposes to generate a metallic oxide or hydroxide in situ in said reaction zone. 15. The method of claim 14 wherein said temperature is between about 150 and 400°C. SUBSTITUTE <:ZZΎ 16. The method of claim 14 wherein said pressure is between about 500 and 3000 psig. 17. The method of claim 1 wherein said ethanol is blended with a combustible liquid fuel. 18. The method of claim 14 wherein said ethanol is blended with a combust¬ ible liquid fuel. 19. The method of claim 17 or 18 wherein said liquid fuel is a fossil fuel selected from diesel fuel, fuel oil, kerosene, or gasoline. -

Inventors: HILLMAN M, HUFFMAN W, LIPINSKY E, STAMBAUGH E
Applicants: BATTELLE DEVELOPMENT CORP, BATTELLE DEV CORP
Application year: 1981
Main classification: C10L1
IPC codes: B01J23, B01J27, B01J31, C07C27, C07C29, C07C31, C07C67, C10L1