WO1985000502A1 - Procede de production de substances utiles a partir de farine de soya - Google Patents

Procede de production de substances utiles a partir de farine de soya Download PDF

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Publication number
WO1985000502A1
WO1985000502A1 PCT/US1984/001137 US8401137W WO8500502A1 WO 1985000502 A1 WO1985000502 A1 WO 1985000502A1 US 8401137 W US8401137 W US 8401137W WO 8500502 A1 WO8500502 A1 WO 8500502A1
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WO
WIPO (PCT)
Prior art keywords
free
product
residue
amino acids
coal
Prior art date
Application number
PCT/US1984/001137
Other languages
English (en)
Inventor
Giorgio Colmelet
Original Assignee
Durante, Joseph
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Durante, Joseph filed Critical Durante, Joseph
Publication of WO1985000502A1 publication Critical patent/WO1985000502A1/fr

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Classifications

    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J1/00—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites
    • A23J1/14—Obtaining protein compositions for foodstuffs; Bulk opening of eggs and separation of yolks from whites from leguminous or other vegetable seeds; from press-cake or oil-bearing seeds
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23J—PROTEIN COMPOSITIONS FOR FOODSTUFFS; WORKING-UP PROTEINS FOR FOODSTUFFS; PHOSPHATIDE COMPOSITIONS FOR FOODSTUFFS
    • A23J3/00—Working-up of proteins for foodstuffs
    • A23J3/30—Working-up of proteins for foodstuffs by hydrolysis
    • A23J3/32—Working-up of proteins for foodstuffs by hydrolysis using chemical agents
    • A23J3/34—Working-up of proteins for foodstuffs by hydrolysis using chemical agents using enzymes
    • A23J3/346—Working-up of proteins for foodstuffs by hydrolysis using chemical agents using enzymes of vegetable proteins

Definitions

  • the present invention is directed for a method for recover ing useful products from de-oiled soymeal.
  • the present invention is directed to a method for recover ing a useful soluble proteic substance and free amino acid ⁇ - ⁇ from soymeal.
  • Amino acids are the essential components of proteins, therefore there is a high nutritional requirement for them. Amino acids may be provided from food protein, however, the body must break down this food protein into free, individ-
  • FIG. 1 is a diagram of the preferred steps in the method according to the present invention.
  • FIG. 2 is a diagram of the preferred apparatus for use according to the present invention.
  • the present invention provides a method for recovering useful products from de-oiled soymeal comprised of steps of extracting the de-oiled soymeal with aqueous liquid at a temperature in the range of 60-95°C; separating the liquid extract from the residue and subjecting the residue to aqueous acidic hydrolyzing conditions; separating the liquid phase from the hydrolysis mixture and absorbing it onto a cationic sulfonated resin; eluing the amino acids from the resin with aqueous base; ultrafiltering the eluate; and purifying the filtrate from the ultrafiltration to provide a mixture of free amino acids.
  • the method according to the present invention also provide a soluble proteic substance by utilizing the liquid extrac derived above from the de-oiled soymeal. Boiling of th liquid extract, followed by cooling and separating th liquid phase from the solid material, and lyophilizing th liquid phase forms a useful soluble proteic substance.
  • the primary products derived from the present process are soluble proteic substance containing assimilable carbohy drates and a quantity of protides (proteins and amin acids) suitable to impart an agreeable taste to the mix ture.
  • a second substance produced according to the presen process is a composition containing free amino acids.
  • the starting material is soymeal from which the oil has been extracted (de-oiled soymeal) .
  • a typical analysis of de-oiled soymeal is approximately 37% proteins, 35% carbohydrates, 14% ashes (mineral salts) , 5% lipids, and about 9% water.
  • the de-oiled soymeal is first dried 10.
  • the mixture is then extracted 11 with warm water, . usually in the range of 60-95 ⁇ C, and the extract and solid residues are separated, usually by centrifugation 12.
  • the hot water extraction is usually accomplished within about 3 hours for a load of 8000 kilograms soymeal, wherein the initial temperature of extraction is about 95 ⁇ C, with gradual cooling to about 60°C.
  • the liquid from the centrifugation is then concentrated 13, usually to a dense fluid with a specific weight (at 80°C) of about 1.3 to 1.4.
  • the concentrate is then boiled 14, usually for about 2 hours, then cooled 15 to about 20°C and centrifuged 16.
  • the solid residue from centrifugation 16 may be dried 17 and milled 18 to yield cellulose, protein and starchy substances, termed By-Product 1. After drying at 120°C, the typical composition of By-Product 1 is shown below in Table 1.
  • the liquid from centrifugation step 16 may be lyophilized 19 and milled 20 to yield a water-soluble proteic sub ⁇ stance.
  • a typical analysis for this soluble proteic substance is shown in Table 2.
  • the soluble proteic substance may be used, for example, to prepare beverages combined with water or milk, or may be utilized with vitamized, non-alcoholic beverages or in slightly alcoholic beverages or bitter tonics.
  • the protide content (the proteins and amino acids) of the soluable proteic substance is such that it has a pleasing taste.
  • step 12 is hydro- lyzed under aqueous acidic conditions 13, preferably with hydrochloric acid, so that the acid concentration in the reaction mass is about 15%.
  • the mixture will be heated to approximately 90-120°C, preferably 110°C, which temperature is maintained for a period of time sufficien to accomplish hydrolysis, usually in the range of 46-9 hours. It will be understood, however, that the longer th time of hydrolysis, up to the limit of approximately 10 hours, the greater the percentage of amino acids obtaine in the final product. After 100 hours of hydrolysis a 110°C, however, the yield of amino acids decreases.
  • reaction mass After hydrolysis the reaction mass is cooled 14, usually t about 35°, and diluted 15. The dilution is for the purpos of lowering the concentration of hydrochloric acid to abou 7% and to form the reaction mass into a transportabl fluid. Also, dilution prepares the reaction mass to suitable concentration for the subsequent absorption o resins for purification. The diluted mass is centrifuged 16 and the solid residue is diluted 17, centrifuged again 18, and dried 19 to produce a by-product, termed By-Product 2, having a typical composition as shown in Table 3.
  • the liquid supernatant from centrifugation step 16 is then absorbed on cationic sulfonated resins 20.
  • the amino acids are eluted 21, with an aqueous base, such as 2% aqueous ammonia.
  • aqueous base such as 2% aqueous ammonia.
  • the ammonia elutions and washings are then concentrated 22 and ultrafiltered 23 through a membrane having a molecular weight cutoff of 1000.
  • the retentate from the ultrafiltra- tion step comprises By-Product 3 which has ancillary uses, such as animal feed or fertilizer.
  • the filtrate from the ultrafiltration step 23 is purified 24, usually by adsorp ⁇ tion onto a carbonaceous material with heating. After cooling 25, the mixture is centrifuged 26 and the separated carbon, which may contain about 10% of the recoverable amino acids, is diluted 27, boiled 28, centrifuged 29.
  • the liquid from the centrifugation step 29 may be mixed from the liquid from centrifugation step 26 for further recovery of amino acids.
  • the carbon recovered from the centrifuga tion step 29 may then be dried 30, and then recycled.
  • Th liquid from centrifugation step 26 is concentrated 31, dried 32, and cooled 33 in vacuum.
  • the resulting drie product is then milled 34, and comprises a mixture of amin acids which may then be packaged.
  • a typical yield of th amino acid mixture is about 2,000 kilograms from a 8,000 kilogram soymeal sample, or about 25% yield.
  • a typical analysis of the amino acid mixture product is shown belo in Table 5.
  • the steps 31, 32, 33 and 34 are preferably conducted utilizing a conventional micronizer, many of which are commercially available, such as the NIRO model micronizer.
  • the liquid will be concentrated to about one-tenth of its volume then added to the micronizer.
  • the micronizer will typically provide a current of forced air heated at approximately 80°C to further evaporate liquid at a rate of about 500 liters per hour. Using liquid feed containing about 20% amino acids, this v. produce a solid product at the rate of about 100 kilogra..._. per hour.
  • the micronized solid may then be further dried by aspiration and collected as a powder in waterproof bags.
  • the moisture content of the final product will usually be in the range of 0.5 to 1% by weight.
  • the analysis (Table 5) is the median value obtained from a series of twelve preparations.
  • HISTIDINE 2. .79 3.02 ARGI INE 7. .81 7.66
  • the panels remaining from the various phases of purifi cation are dried and group up and mixed and packaged i sacks of 25 kg (Table 7) .
  • Step 24 described above comprises absorption of the fil trate onto a carbonaceous material.
  • commercia activated carbon may be utilized for this purpose, it i preferred that activated carbon be prepared from natura coal according to the following process.
  • Coal either i its natural wet state or in a dried form, is mixed wit deionized water. The amount of water used should be abou twice by weight of the amount of coal which is used.
  • This slurry is then heated to boiling, preferably for approxi ⁇ mately one hour, then cooled and the solids are separated, preferably by centrifuge.
  • the coal comprising a solid residue is then heated to about 2,000°C for approximately two hours. Then, the temperature is lowered to about 1,000° with further heating for about four hours.
  • the resultant activated carbon may then be utilized in Step 24 described above.
  • the yield of activated coal from this process is approximately 80-85% based on the weight of the
  • OMPI vripo original undried coal The activated coal made according to this process should be maintained in an anhydrous environment after cooling and before use.
  • FIG. 2 there is shown a typical apparatus for use in the present process.
  • the soymeal is poured into inlet 40 of a continuous cycle rotary oven 41.
  • a typical oven may be 12 meters long, divided into two sections each of six meters. The first section may be heated to about 80°C and the second to 110 ⁇ C.
  • An aspirator 42 withdraws vapors from the oven.
  • the capacity of a typical oven is 33 kilograms per minute so that drying of the whole load of 8000 kilograms may be accomplished in approximately four hours.
  • the dried flour is removed from the oven and pumped into an iron boiler 43, typically having a capacity of 100 cubic meters and having stem heat coils on its exterior. About 48 cubic meters of water at 95°C is previously added to the tank 43 before pumping in the dried soymeal.
  • the soymeal is gradually added to the tank over a period of approximately 30 minutes with slow agitation. After all the soymeal is added the mixture is agitated for an addi ⁇ tional 30 minutes at 95°C.
  • the tank is then slowly cooled by running ambient temperature water through the outer coils. Once a temperature of approximately 60 ⁇ C is ob ⁇ tained, usually in approximately 2 hours, the mass from tank 43 is extracted and unloaded with a pump (not shown) into an automatic gap centrifuge 44.
  • the liquid phase is expelled via line 45 through filter 46 into a continuous concentrator 47 and water is evaporated at a temperature of about 80°C.
  • the dense fluid mass is transported into a boiler 48 equipped with an agitator. In boiler 48 the mixture is heated with steam and boiled for approximately 2 hours. The mixture is then cooled in a separate container (not shown) to approxi ⁇ mately 20°C and then centrifuged in centrifuge 49.
  • the solid panel from centrifuge 49 contains By-Product 1, described above.
  • the liquid from centrifuge 49 is the lyophilized in lyophilizer 50 under vacuum.
  • the soli product is then ground in mill 51 and sifted through sifte 52 to produce a soluble proteic substance, described above.
  • the solids panel from centrifuge 44 is pumped through a je pump (not shown) into reactor tank 53 equipped with stea heater 54 and condenser 55. Acid is added into tank 53 from acid storage tank 56. The contents of tank 53 are then centrifuged in centrifuge 57, solids of which are collected and dried as described above to produce By-Pro ⁇ duct 2.
  • the liquid from centrifuge 57 is placed into storage tank 58 discharges onto adsorption columns 59.
  • Various washings of the adsorption columns are accomplished by appropriate valves (not shown) from ammonia solution storage tank 60 and water storage tank 61. Acidic residual from columns 59 may be taken off to residual storage tank 62.
  • the amir- acid containing eluate from columns 59 is filtered thrc filter 63 into concentrator 64, then ultrafiltered through ultrafiltration means 65.
  • the retentate is collected on the ultrafiltration membrane in 65 and is periodically removed as By-Product 3, described above.
  • the filtrate from ultrafiltration means 65 lead into tank 66 equipped with heating coils and condenser where it is purified by heating with carbonaceous solids.
  • the carbon ⁇ aceous solids used will be activated carbon prepared as in the process described hereinabove from natural coal.
  • the contents are then filtered through filter 67 and/or centri- fuged (not shown) whereupon the solid carbonaceous residue is treated as described above for recycling.
  • the filtrate from filter 67 is conducted into concentrator 68 where it is concentrated into a syrupy mass at about 80°C.
  • the contents of tank 68 are then led into rotating drum dryer 69 where it is dried under vacuum, then ground in mill 70 and sifted in sifter 71 to provide the amino acid mixture described above.
  • soymeal Approximately 8,000 kilograms of soymeal are placed in a continuous cycle, rotary oven with a cochlea carrier for drying.
  • the soymeal is dried in a first section of the oven to add about 80°C and in a second section at about 110°C and is moved through the dryer at about 33 kilo ⁇ grams/minute so that the drying occurs in about 4 hours.
  • the dried soymeal, still hot, is removed from the dryer, gathered and pumped with a jet pump into an iron boiler with a capacity of 100 cubic meters with steam heat coils covered on the outside by metal sheets thermally isolated toward the exterior.
  • the mass of extracted matter is unloaded into an automatic gap centrifuge.
  • the load is centrifuged at 800 cycles/minute for about 4 hours.
  • the liquid phase is expelled from the centrifuge and goes directly into a continuous concentrator which in four hours evaporates 32 cubic meters of water.
  • the concentrate, 4 cubic meters, is a dense fluid having a specific weight of 1.3-1.4 at 80°C. At 80°C this dense fluid is transported into a 6 cubic meter boilers, with an agitator and an exterior coil for heat and recovery of steam.
  • the mixture is boiled for 2 hours and unloaded into a container with a water cooling coil of the capacity of 5 cubic meters.
  • the mixture is cooled to 20 ⁇ C gradually in 12 hours.
  • the insoluble portion is removed by processing
  • the cellulose, protein and starchy substances are dried in an oven at 120° and milled to produce a substance, described as By-Product 1, the composition of which is set forth in Table 1 above.
  • the liquid portion of the centri ⁇ fuge is sent to a lyophilyzation which is preceded by prefreezing at 30°C. This phase is completed in 24 hours and the product is obtained by a sifting mill (80 mesh/cm 2) and then is immediately gathered in 10 kilogram pacified cloth sacks, to yield a soluble proteic substance described above in Table 2.
  • the yield is 1,000 kilograms and corres- ponds to 10% of the soymeal.
  • the solids panel from the initial water extraction step above is pumped through a jet pump into a reactor of 60 cubic meters heated by an exterior coil and an agitator and condenser. Thirteen cubic meters of deionized water and 3,900 kilograms of anhydrous hydrochloric acid is added while controlling the flux of water and acid so that dilution is approximately 23%. The concentration of the hydrochloric acid is diluted by the added water and the water already contained in the mass to a concentration of approximately 15%. While under agitation the mixture is heated to 110°C at which temperature it is maintained for 72 hours.
  • the acid water phase from the first centrifuge step above is gathered in a fiberglass con ⁇ tainer of 60 cubic meters and adsorbed onto 8 separate columns, one meter in diameter, 4 meters in height each containing 2.5 cubic meters of cationic sulfonated resin.
  • the flowing liquid is gathered in a fiberglass container of 100 cubic meters.
  • the wash of the acid left within the columns is done with 30 meters of water and is then gathered with the previously recovered acid for recycling.
  • the amino acids obtained from the resin in the columns are diluted with 50 cubic meters of 2% ammonia.
  • the first 20 cubic meters passing through the column having approxi ⁇ mately neutral pH do not contain amino acids and are recycled into the water tank.
  • the next 30 cubic meters are continuously carried into a concentrator already prepared for the recovery of ammonia with regulated water drops in order to maintain an emmolient solution of 2%.
  • the columns are washed with 30 cubic meters of water which are then concentrated in the same evaporator.
  • the concen ⁇ tration of ammonia liquids is increased to the point that the residual volume of 4 cubic meters is reached.
  • the concentrated mixture is then subjected to an ultrafiltra ⁇ tion membrane having a molecular weight cutoff of 1,000 MW.
  • the filtration speed is approximately 70 liters/minute so that the filtration is completed in about one hour.
  • Approximately 10 kilograms of dry residue, described as By-Product 3 above, is removed from the filter as a reten- tate. Filtrate from the ultrafiltration step is emptied into a boiler heated by a coil with an agitator operated at about 10 cycles/ minute.
  • This fluid mass is kept at 80°C to prevent solidifying and is sent to a dryer with a turning drum circulating hot air with a vacuum device.
  • -.Drying is completed in 3 hours followed by cooling in vacuum.
  • the complex of amino acids is unloaded, cooled and immediately set for milling, sifting and packaging.
  • the amino acid mixture product is hygroscopic and must be stored in a dry environment with relative humidity below about 50%.
  • the yield of amino acid mixture is approximately 2,000 kilo ⁇ grams or 25% of the weight of the original soymeal.
  • Example 3 The same procedure is followed as in Example 2 above, except that the time for acid hydrolysis is reduced to 48 hours. After 48 hours of hydrolysis at 110°C in hydro ⁇ chloric acid, the process is completed as described above. The percentage of amino acids obtained is approximately 18% yield and the analysis is similar to that shown above in Table 5.
  • Example 4 The procedure is the same as in Example 2 except that the acid hydrolysis time is increased to 96 hours. The per ⁇ centage of amino acids obtained is about 26%. However, analysis revealed that there was no tryptophan in the final amino acid mixture.
  • Example 5 The same procedure is followed as in Example 2 above except that the hydrolysis step is conducted under two atmospheres of pressure, 110 ⁇ C for 48 hours. The percentage of amino acids obtained is 17.8%, with the absence of tryptophan and tyrosine from the final product.
  • Example 6 The procedure as followed is the same as Example 5 above, but the time of hydrolysis was reduced to 24 hours. The percentage of amino acids was 24.8% with amino acid analy ⁇ sis similar to Table 5 above, except the percentage of tryptophan was 0.26% (free), 0.41 (total).
  • Example 5 The same as Example 5 except that the time of hydrolysis is reduced to 12 hours.
  • the percentage of amino acids is 14.2% and with the analysis of the amino acids similar to that of Table 5, except that the percentage of tryptophan is 0.24% (free) and .43% (total).
  • Example 8 The procedure is the same as Example 2 except that the filtration step after elution from the columns is omitted. To obtain the same purity as in Example 2, it was necessary to add three times the quantity of bleaching coal relative to the expected weight of amino acids with excessive increases of water for washing to recover amino acids withheld by the carbon.

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  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Biochemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Food Science & Technology (AREA)
  • Polymers & Plastics (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • General Chemical & Material Sciences (AREA)
  • Health & Medical Sciences (AREA)
  • Nutrition Science (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Peptides Or Proteins (AREA)
  • Polysaccharides And Polysaccharide Derivatives (AREA)

Abstract

Procédé d'extraction de produits utiles à partir de farine de soya déshuilée. Il est ainsi possible d'extraire au moins deux produits utiles, notamment une substance protéique soluble (provenant de l'étape 20) et un mélange d'acides aminés libres (provenant de l'étape 34).
PCT/US1984/001137 1983-07-22 1984-07-20 Procede de production de substances utiles a partir de farine de soya WO1985000502A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
US51628583A 1983-07-22 1983-07-22
US516,285 1983-07-22
US58783884A 1984-03-12 1984-03-12
US587,838 1984-03-12

Publications (1)

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WO1985000502A1 true WO1985000502A1 (fr) 1985-02-14

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PCT/US1984/001137 WO1985000502A1 (fr) 1983-07-22 1984-07-20 Procede de production de substances utiles a partir de farine de soya

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KR (1) KR850004704A (fr)
AU (1) AU3058084A (fr)
FR (1) FR2549351A1 (fr)
GB (1) GB2143828B (fr)
IN (1) IN162583B (fr)
IT (1) IT8421989A0 (fr)
MX (1) MX7589E (fr)
PH (1) PH21335A (fr)
WO (1) WO1985000502A1 (fr)

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPS61295219A (ja) * 1985-06-21 1986-12-26 Eiichi Sato 活性炭

Citations (22)

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US2991309A (en) * 1957-12-30 1961-07-04 Internat Minerals & Chemicals Protein hydrolysis
US3001875A (en) * 1956-05-28 1961-09-26 Griffith Laboratories Method of extracting protein from defatted soybean material
US3152955A (en) * 1960-12-22 1964-10-13 Distillers Co Yeast Ltd Amino acids concentrate
US3185675A (en) * 1963-03-28 1965-05-25 Bristol Myers Co Peptide
US3697287A (en) * 1969-01-28 1972-10-10 Morton Norwich Products Inc Amino acid food composition
US3698912A (en) * 1969-07-01 1972-10-17 Morton Norwich Products Inc Process for making nutrient composition
US3701666A (en) * 1968-02-14 1972-10-31 Morton Norwich Products Inc Process for making amino acid composition
US3778514A (en) * 1970-10-09 1973-12-11 Mayer & Co Inc O Nutritional product of whey protein and collagen hydrolysate
US3876505A (en) * 1972-12-08 1975-04-08 Calgon Corp Manufacture of activated carbon from sized coal
US3910849A (en) * 1973-01-05 1975-10-07 Agency Ind Science Techn Method for manufacture of activated carbon and apparatus therefor
US3950547A (en) * 1974-08-26 1976-04-13 Syntex (U.S.A.) Inc. Dietary composition and methods of preparing
US3951856A (en) * 1972-10-02 1976-04-20 Westvaco Corporation Process for making activated carbon from agglomerative coal
US3976597A (en) * 1975-06-09 1976-08-24 Westvaco Corporation Fluidized bed process for making activated carbon including heating by conduction through the distributor plate
US3995071A (en) * 1975-06-23 1976-11-30 Mead Johnson & Company Aqueous purified soy protein and beverage
US4054677A (en) * 1974-07-30 1977-10-18 Stefano Orban Process for preparing vegetal proteinic concentrates, products thereby obtained, and milk substituting feeds containing said concentrates
US4091120A (en) * 1976-11-15 1978-05-23 Mead Johnson & Company Liquid dietary product containing soy protein membrane isolate
US4107084A (en) * 1975-06-09 1978-08-15 Westvaco Corporation Process for activating carbonaceous material
US4130555A (en) * 1977-09-06 1978-12-19 Nippi Incorporated Peptide mixtures derived from collagenous material or gelatin
US4172828A (en) * 1977-09-30 1979-10-30 Anderson, Clayton & Co. Method for processing soy protein and composition of matter
US4185121A (en) * 1977-03-17 1980-01-22 Societe D'assistance Technique Pour Produits Nestle S.A. Process for the treatment of an acid hydrolysate of vegetable matter and the products obtained
US4268417A (en) * 1977-09-26 1981-05-19 American Minechem Corporation Method of making activated carbon
US4273619A (en) * 1979-11-19 1981-06-16 Angelo Ii James F Apparatus for continuously carbonizing and activating carbonaceous materials

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
IL36482A0 (en) * 1970-04-04 1971-05-26 Istituto Ricerche Biomediche The manufacture of natural amino acid mixtures from protein material

Patent Citations (22)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3001875A (en) * 1956-05-28 1961-09-26 Griffith Laboratories Method of extracting protein from defatted soybean material
US2991309A (en) * 1957-12-30 1961-07-04 Internat Minerals & Chemicals Protein hydrolysis
US3152955A (en) * 1960-12-22 1964-10-13 Distillers Co Yeast Ltd Amino acids concentrate
US3185675A (en) * 1963-03-28 1965-05-25 Bristol Myers Co Peptide
US3701666A (en) * 1968-02-14 1972-10-31 Morton Norwich Products Inc Process for making amino acid composition
US3697287A (en) * 1969-01-28 1972-10-10 Morton Norwich Products Inc Amino acid food composition
US3698912A (en) * 1969-07-01 1972-10-17 Morton Norwich Products Inc Process for making nutrient composition
US3778514A (en) * 1970-10-09 1973-12-11 Mayer & Co Inc O Nutritional product of whey protein and collagen hydrolysate
US3951856A (en) * 1972-10-02 1976-04-20 Westvaco Corporation Process for making activated carbon from agglomerative coal
US3876505A (en) * 1972-12-08 1975-04-08 Calgon Corp Manufacture of activated carbon from sized coal
US3910849A (en) * 1973-01-05 1975-10-07 Agency Ind Science Techn Method for manufacture of activated carbon and apparatus therefor
US4054677A (en) * 1974-07-30 1977-10-18 Stefano Orban Process for preparing vegetal proteinic concentrates, products thereby obtained, and milk substituting feeds containing said concentrates
US3950547A (en) * 1974-08-26 1976-04-13 Syntex (U.S.A.) Inc. Dietary composition and methods of preparing
US3976597A (en) * 1975-06-09 1976-08-24 Westvaco Corporation Fluidized bed process for making activated carbon including heating by conduction through the distributor plate
US4107084A (en) * 1975-06-09 1978-08-15 Westvaco Corporation Process for activating carbonaceous material
US3995071A (en) * 1975-06-23 1976-11-30 Mead Johnson & Company Aqueous purified soy protein and beverage
US4091120A (en) * 1976-11-15 1978-05-23 Mead Johnson & Company Liquid dietary product containing soy protein membrane isolate
US4185121A (en) * 1977-03-17 1980-01-22 Societe D'assistance Technique Pour Produits Nestle S.A. Process for the treatment of an acid hydrolysate of vegetable matter and the products obtained
US4130555A (en) * 1977-09-06 1978-12-19 Nippi Incorporated Peptide mixtures derived from collagenous material or gelatin
US4268417A (en) * 1977-09-26 1981-05-19 American Minechem Corporation Method of making activated carbon
US4172828A (en) * 1977-09-30 1979-10-30 Anderson, Clayton & Co. Method for processing soy protein and composition of matter
US4273619A (en) * 1979-11-19 1981-06-16 Angelo Ii James F Apparatus for continuously carbonizing and activating carbonaceous materials

Also Published As

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IN162583B (fr) 1988-06-11
FR2549351A1 (fr) 1985-01-25
GB8417924D0 (en) 1984-08-15
PH21335A (en) 1987-10-13
KR850004704A (ko) 1985-07-27
IT8421989A0 (it) 1984-07-20
GB2143828B (en) 1987-05-13
MX7589E (es) 1989-12-20
AU3058084A (en) 1985-01-24
GB2143828A (en) 1985-02-20

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