• 专利附录
  • 专利说明
  • 权利要求
  • 类似技术
  • 同族专利
  • 引用文献
  • 法律状态
  • 优先权
    • 专利摘要:
    The lipid and nucleic acid content in microbial cell masses is decreased by treating the cell masses with an extraction mixture of ammonia or ammonium hydroxide and an organic solvent of the formula I. After the removal of the extraction mixture, the residue of the cell mass is washed with water and the aqueous phase is removed. The residue is then dried - optionally after extraction with an organic solvent of the formula I. The substituents in the formula I have the meanings given in Claim 1. Instead of a compound of the formula I, isopropanol can be used as organic solvent. R1-(CH2)n-OR2 (I)I
    公开号:SU791257A3
    申请号:SU772504953
    申请日:1977-07-26
    公开日:1980-12-23
    发明作者:Шлингманн Мертен；Вертесий Ласло
    申请人:Хехст Аг (Фирма)；
    IPC主号:
    专利说明:

    one
    The invention relates to a technique for the production of protein food products from biomass of microorganisms and can be used in the microbiological and food industry. five
    A method of obtaining a food protein product from the biomass of microorganisms is known by extracting it with a solvent and ammonium hydroxide, followed by separating the extract and drying it 10.
    However, the product obtained by a known method contains an increased amount of lipids and nucleic acids, which negatively affects the use of microbial cell masses as food and feed: the content of nucleic acids leads to pathological conditions, namely gout and the presence of 20 stones in the urine, and the content of lipids limits the storage capacity of products due to their boiling and damage to the taste of products.
    In addition, according to a known method 25, the extraction process is carried out in two stages, and long extraction periods are required for the extraction of lipids with organic solvents, and aqueous solutions of alkalis cause a repeating effect.
    Protein implantation due to a change in its natural structure, in particular, lysinoalanine is formed, which later on in animal experiments causes kidney damage in rats. Because of this change in protein, the essential amino acid lysine is unsuitable for nutrition.
    The purpose of the invention is to reduce the content of lipids and nucleic acids in the product, as well as to increase the content of native protein in it.
    This is achieved by the fact that in the proposed method of obtaining a food protein product from the biomass of microorganisms, the extraction of biomass is carried out with a mixture of solvent and C1MMONIUM hydroxide in the ratio 1: 3: TO, 03-1: 6: O, 6 when using methanol or ethanol as solvent. or in a ratio of 1: 8: 0.081: 12: 1, 2 when using propanol or glycol or monoglycol ether as the solvent.
    The method carried out the mouth as follows.
    The biomass of microorganisms is subjected to extraction with a mixture of solvent and ammonium hydroxide. The quality of microorganisms is used mainly obtained by fermentation with alcohol or n-paraffins in the presence of an aqueous nutrient medium and a gas containing free oxygen. Examples of such microorganisms are methanol consuming bacteria of the genus Methy 1 omonas-, for example, Msthylomonas clara LTCC 31226, or the yeast Candida lipolytica ATCC20383, which is obtained by fermentation on n-paraffins in the presence of an aqueous nutrient medium. Dry mushroom mycelium taken from the fermenters of penicillin production after antibiotic treatment can also be used. Alcohols such as ethanol, methanol:, n-propanol and isopropanol are preferably used as solvents. Preferred are methanol and ethanol. In addition to alcohols, glycols and their monoesters can be used, namely, glycol and monomethyl glycol. Ammonia is added to the solvent in the form of NH gas or in the form of a concentrated aqueous solution depending on the water content of the solvent. NH OH is added for cell masses with a moisture content of 0-15 and NHj - with a moisture content of 10-30%. The amount of lipids removed by extraction depends on the total water content, which refers (in wt.%) To the amount of solvent used, and on the concentration of NHj (in wt.%) Related to the loaded solvent. A mixture of solvent and ammonium hydroxide for the process of extrusion is taken in a ratio of 1: 3: 0.03 1: 6: 0,6 when using methanol or ethanol as a solvent, or in a ratio of 1: 8: 0.08-1: 12 : 1.2 when using propanol or glycol or monoglycol ether as solvent. At the end of the treatment, a mixture of solvent and ammonium hydroxide is used to obtain a protein, which is separated, for example, by centrifugation, filtration or sedimentation. Filtration is preferred. The resulting solid residue is re-treated with an organic solvent to remove lipids as completely as possible. For dissolving residues, the dissolving residue is dried, preferably at a reduced pressure of 80-150 Torr and at an elevated temperature, preferably 40-50 0. The defatted and dried product is odorless. The liquid phase separated from the solid material contains ammonia and dissolved lipids. The solvent is separated from the fat by vacuum distillation for reuse. Then defatted and dried cell masses are mixed with water, preferably in the ratio of water to cell mass from 1: 1 to 1: 30, in particular from 1: 5 to 1:15. The amount of water should be sufficient for possible mixing of the suspension. During processing, the pH is maintained at 5-8.5, preferably 6-7.5. The extraction of nucleic acids, salts, polysaccharides and water-soluble secondary metabolites with water is carried out at 40-70 °, most preferably at 50-60. The duration of the extraction, depending on the extraction temperature and the amount of water, is 5-120 minutes, preferably 2545 minutes. Centrifuged suspension at 10-. Dry the solid phase, freed from the liquid, for example by freeze-drying, in a vacuum or in a spray dryer. By removing lipids and nucleic acids, the product is suitable for the preparation of food and feed. The content of lipids in the final product is from 0.5 to 3.5 wt.%, And nucleic acids from 0.5 to 4.5 wt.%. Example 1. Under aerobic conditions, Methylomonas clara ATCC 31226 is grown in a nutrient medium containing methanol as the sole carbon, ammonia as the sole source of nitrogen, phosphates, salts of iron and magnesium, and other trace elements. The resulting bacterial cell mass is separated from the solution and spray dried. Then, 300 g of methanol was added to 100 g of cell mass and 10 g of NHj gas was introduced into the suspension with stirring, while the temperature was maintained in the range from -5 to -35 ° C. A mixture of methanol, ammonia and cell mass is stirred for 30 minutes at 20 ° C. To separate the solid and liquid phases, the mixture is filtered and the solid residue is washed once with 300 ml of methanol, re-filtered, and then both filtrates are combined. The solution is brown in color and contains lipids loaded with the original substance. Next, methanol and ammonia are removed by vacuum distillation (100 Torr). The balance of 9.5% by weight of the loaded cellular material is dark brown in color and is a foul-smelling paste consisting of free fatty acids, glycerin, phospholipids and secondary metabolites. The solid residue of the extracted cell mass obtained during the filtration process is dried vacuum
    (100 Torr) at 5 hours and get 90 g of a defatted, odorless, non-fat cell mass that has a lighter color than the starting material.
    To reduce the content of nucleic acids, this cell mass is suspended in 900 ml of water, homogenized by stirring at pH 6.9. Next, the temperature is adjusted and stirred for another 20 minutes, cooled until and separated into solid and liquid phases by centrifugation. The resulting sediment is again mixed with 900 ml of water and centrifuged again at 20 ° C. The sediment is dried under reduced pressure.
    The yield is 65 g. The content of nucleic acids is reduced from 11.2% to 1.5%. The dry product is odorless, and when mixed with water it has a pleasant smell.
    Example 2. The starting material is the bacterial cell mass as in Example 1. It is subjected to the same processing steps and under the same conditions, but using 30 ml of 3% NH-OH solution as a reagent instead of gaseous.
    Example 3 The process is carried out as described in example 2, but 60 ml of concentrated (33%) are used.
    Example 4. The process is carried out as described in Example 2, but ethanol is used as the solvent instead of methanol.
    Example 5. The process is carried out as described in Example 2, but instead of methanol, glycol monomethyl ether is used as the solvent.
    Example 6. The process is carried out as described in example 2, but isopropanol is used as the solvent instead of methanol.
    Example 7. Cell material from Mothylomonas clara (as described in example 1) is taken as the starting material.
    100 g of the spray-dried product is converted into a form suitable for processing and degreased as described in Example 1 (15 g NHj). The residue is not dried. Well pressed filter cake with a solids content of 85% is suspended in 900 ml of water. The pH is adjusted to 8.9, due to the ammonia remaining in the wet biomass. With stirring, the temperature of the suspension is raised to 65 s and after 5 min by the addition of hydrochloric acid, the pH is adjusted to 7.2.
    Then stir for another 15 minutes at, then cool to 40 ° C and centrifuge. The residue obtained is dried.
    Example 8. A yeast strain consuming hydrocarbons is cultivated.
    Cendida li;, olytica ATCC 20383 on n-paraffins in the presence of an aqueous nutrient medium and a gas containing oxygen. The yeast cell mass is separated from the nutrient solution and dried.
    100 g of dried yeast cell mass is suspended at room temperature and normal pressure in 300 g of methanol and 10 g of ammonia gas is introduced into this mixture for 15 minutes, while the temperature of the suspension is maintained until cooled. After passing the gas, it is stirred for another 20 minutes at 22 ° C and then filtered through a suction frit.
    5 On the filter cake, mix once with 300 ml of methanol and then filter. Both filtrates are combined. Solution color is yellow. Solution contains loaded cell lipids.
    0 material.
    Methanol and ammonia are removed under reduced pressure (14 Torr).
    The remainder after the second filtration, consisting of destroyed and defatted microorganism cells, is dried in a vacuum oven at 40 ° C (100 Torr) for 5 hours,
    0 The resulting product has a lighter color than the yeast mass that was originally used, and is odorless.
    For U1, the amount of nucleic acid from the initial
    7.5% by weight attributed to the starting material, 100 g of defatted and dried yeast are suspended in a solution of 1 ml of distilled water and
    Q 100 t-vi methanol. The mixture is brought under stirring and the pH is 6.8 to 5 ° C and centrifuged to separate the precipitate containing the yeast protein and the liquid phase containing the nucleic acids transferred to the dissolved state. The precipitate after repeated washing at room temperature is subjected to freeze-drying. The content of nucleic acids in the dried material is reduced from the initial 7.5 wt.%.
    Example 9. The process is carried out as described in Example 8, but ethanol is used instead of methanol and instead of 10 g of ammonia gas is taken
    5 60 ml NH4 OH (33%).
    Example 10. In a nutrient medium containing lactose, liquid phosphate, carbonate and magnesium sulfate,
    0 The known method is grown aerobically PeniciIlium chrysogenum LTCC 10238, dried mycelium serves as the starting material. The process is carried out as described in Example 8, but instead of
    5% ammonia use 33%,
    Fat-free dry mycelium is washed with water at 30 ° C.
    Example 11. The same mass as described in example 10 is used as the starting material. Ethanol is used instead of methanol, The temperature of the water extraction process is maintained at 15 minutes.
    The table shows the results obtained when carrying out the process according to examples 1-11.
    权利要求:
    Claims (1)
    [1]
    Claim
    A method of obtaining a food protein product from the biomass of microorganisms by extracting it with solvent 45 and ammonium hydroxide followed by separation of the extract and drying it, characterized in that, in order to reduce the content of lipids and nucleic acids in the product, and also 53 to increase the content of native protein in it containing all essential amino acids, biomass extraction is carried out with a mixture of solvent and ammonium hydroxide in a ratio of 1: 3: 0.03-1: 6: 0.6 when using methanol or ethanol as a solvent, or a ratio of 1: 8: 0.08-1: 12: 1.2 when using propanol or glycol or monoglycol ether as a solvent.
    类似技术:
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    同族专利:
    公开号 | 公开日
    CA1101724A|1981-05-26|
    GR64056B|1980-01-21|
    JPS5530354B2|1980-08-09|
    NO772658L|1978-01-30|
    AU2731977A|1979-02-01|
    FR2359896B1|1982-04-30|
    NL7708171A|1978-01-31|
    NO147034B|1982-10-11|
    FI57443C|1980-08-11|
    EG12626A|1979-09-30|
    ATA544077A|1979-12-15|
    SE432609B|1984-04-09|
    AT357502B|1980-07-10|
    AU512670B2|1980-10-23|
    IL52594A|1980-10-26|
    BE857229A|1978-01-27|
    IT1082226B|1985-05-21|
    PL107949B1|1980-03-31|
    NO147034C|1983-01-19|
    DE2633666B2|1978-09-21|
    PL199855A1|1978-03-13|
    SE7708539L|1978-01-28|
    FR2359896A1|1978-02-24|
    DD131072A5|1978-05-31|
    FI772272A|1978-01-28|
    DK146511C|1984-04-02|
    BG37997A3|1985-09-16|
    ZA774517B|1978-06-28|
    CS207473B2|1981-07-31|
    JPS5315489A|1978-02-13|
    PT66849A|1977-08-01|
    ES460877A1|1978-04-16|
    PT66849B|1979-03-13|
    DK337677A|1978-01-28|
    DE2633666A1|1978-02-02|
    DK146511B|1983-10-24|
    IL52594D0|1977-10-31|
    CH635615A5|1983-04-15|
    HU176802B|1981-05-28|
    GB1584194A|1981-02-11|
    RO71982A|1982-09-09|
    DE2633666C3|1983-02-24|
    FI57443B|1980-04-30|
    引用文献:
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    RU2522888C2|2012-10-04|2014-07-20|Валентина Еремеевна Куцакова|Method of production of protein feed additive|US3615654A|1968-05-17|1971-10-26|Cpc International Inc|Method of treating microbial cells|
    IT954172B|1970-07-24|1973-08-30|Standard Oil Co|PROCEDURE FOR EXTRACTING PROTEIN MATERIAL FROM UNICELLULAR MICROBIAL ORGANISMS AND PRODUCT OBTAINED|
    SU419551A1|1972-01-18|1974-03-15|В. Ф. Фоменков Институт биологической физики СССР|THERMAL FLOW METER|
    GB1400691A|1973-02-08|1975-07-23|British Petroleum Co|Process for the production of proteinaceous material|
    GB1408845A|1973-02-13|1975-10-08|Ranks Hovis Mcdougall Ltd|Production of edible protein containing substances|
    JPS5411379B2|1973-02-21|1979-05-15|DE2748885A1|1977-11-02|1979-05-03|Hoechst Ag|PROCESS FOR IMPROVING THE PROPERTIES OF SCROTS OR FLOURS FROM OIL SEEDS|
    DE2907065A1|1979-02-23|1980-09-04|Hoechst Ag|METHOD FOR GREATING LEATHER AND FUR SKINS|
    CA1120314A|1979-08-22|1982-03-23|John A. Ridgway|Treatment of proteinaceous materials with anhydrousammonia gas|
    DE3143947A1|1981-11-05|1983-05-11|Hoechst Ag, 6230 Frankfurt|"FUNCTIONAL PROTEIN HYDROLYSATE, METHOD FOR THE PRODUCTION THEREOF AND FOOD CONTAINING THIS PROTEIN HYDROLYSATE"|
    DE3228500A1|1982-07-30|1984-02-02|Basf Ag, 6700 Ludwigshafen|METHOD FOR PURIFYING CARBONIC ACID ESTERS CONTAINING ALDEHYDE, ACETALS AND / OR UNSATURATED COMPOUNDS|
    DE69514549T2|1995-05-29|2000-08-24|Ni Skij I Vycislitel Nych Komp|METHOD FOR OBTAINING BIOMASS FROM MICROORGANISMS WITH LOW NUCLEIC ACID CONTENT|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE2633666A|DE2633666C3|1976-07-27|1976-07-27|Reduction of the lipid and nucleic acid content in microbial cell mass|
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