• 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:
    A three or optionally four stage process for the continuous removal of a gum phase from triglyceride oil is described in which in a first stage the oil containing a separate gum phase is subjected to centrifugal separation in a first centrifugal separator to yield gums with low oil content and an oil that still contains a fraction of the gums originally present in the feed, in a second stage the oil obtained from the first stage is subjected to centrifugal separation in a second centrifugal separator to yield oil with a further reduced residual gum content and a gum phase with a higher oil content than the gums obtained in the first stage, in a third stage the gum phase obtained in the second stage is recycled into the oil stream fed to the first centrifugal separator and optionally in a fourth stage the oil obtained in the second stage is washed one or more times with water.
    公开号:SU1743359A3
    申请号:SU894614423
    申请日:1989-07-05
    公开日:1992-06-23
    发明作者:Кленеверк Бернар；Девульф Франс；Ван Опсталь Мартин；Вебер Эрнст
    申请人:Н.В.Вандемоортеле Интернэшнл (Фирма)；
    IPC主号:
    专利说明:

    The invention relates to the processing of oils, in particular to methods for the purification of triglyceride oils from a separate mucous phase.
    A known method of continuous purification of triglyceride oil from a separate mucous phase, which consists in the fact that the original oil is subjected to centrifugation, and the resulting oil phase is mixed with water, followed by centrifugation and vacuum drying of the resulting oil phase.
    The disadvantage of the known method is that the degree of purification from the mucous phase is not completely satisfactory. In addition, the loss of oil is too high.
    The closest to the proposed technical essence and the achieved result is a method of continuous purification of triglyceride oil from a separate mucous phase, which consists in the fact that the original oil is subjected to centrifugation, and the resulting oil phase is mixed with a solution of sodium liquor, followed by centrifuging the resulting oil this mixture, and the resulting oil phase is mixed with water, followed by centrifuging the resulting mixture and vacuum drying obtained at ifugirovanii oil phase.
    The disadvantage of this method is its complexity due to the presence of three stages of centrifugation and two stages of mixing in it. In addition, the quality of the refined oil is not always satisfactory, and therefore losses in the final refining cannot be prevented.
    The purpose of the invention is to simplify the process and reduce losses.
    The goal is achieved according to the method of continuous purification of triglyceride oil from a separate mucous phase, which consists in the fact that |

    co

    with
    The oil is subjected to the first stage of centrifugation, and the oil phase thus obtained is subjected to the second stage of centrifugation followed by drying, and the mucous phase obtained in the second stage of centrifugation is at least partially recycled to the original oil, and the first and second stages of centrifugation are carried out 1000-8000 and 4000-15000d respectively.
    Before drying, the oil withdrawn from the second stage of centrifugation can be subjected to washing with water taken in an amount of 0.5-20% by weight, preferably in a countercurrent system. Water may be slightly acidified. This stage is necessary only if the purified oil is subjected to physical refining. However, in the case of alkaline refining, washing with water should not be carried out. The first and second centrifugation steps, as well as the washing, are usually carried out at elevated temperatures.
    It is advisable to recycle 5-20% by weight of mucous substances that were contained in the original oil. The steady state is reached very quickly after the start, the first stage of centrifugation.
    Any separate mucous phase obtained by known methods, containing triglyceride oil, can be purified by this method. As triglyceride oils, for example, soybean, sunflower, rapeseed, palm and other vegetable oils, as well as lard, cattle and fish oil can be given.
    The combination with physical refining leads to the complete elimination of effluent water, which has a great need for biological oxygen, due to the fact that only water used for washing, which contains a small amount of inorganic salts, flows out. Not needed and the stage of the division of soap. By using water to flush the oil in the countercurrent system in relation to the oil flow, effective elimination of all wastewater from the refining process is achieved.
    The proposed method allows to obtain an oil of excellent quality, containing a particularly small amount of mucous substances, as well as a mucous phase containing a particularly small amount of oil.
    Example 1. 9000 kg / h of soybean oil with a residual phosphorus content of 110 g / ml, with a content of 0.50 wt.% Free fatty acid, 0.25 wt.% Volatile compounds and moisture and 0.05 wt.% Other impurities, containing a separate mucous phase and having a temperature of 90 ° C, is subjected to
    the first stage of centrifugation at about 3800d. The oil withdrawn from the first phase of centrifugation is fed to the second stage of centrifugation, carried out at 5800d. The resulting
    At this stage, the mucous phase (oil content is about 99.5 wt.%) Is completely recycled at a flow rate of 1540 kg / h and mixed with the original oil supplied to the first stage of centrifugation. The oil withdrawn from the second stage of centrifugation (7470 kg / h) was washed twice with 5% by weight of water in a countercurrent system at 90 ° C. The resulting oil after drying has a residual content of 3.4 g / ml
    0 organic phosphorus, contains 80 g / billion of iron, 0.45 wt.% Free fatty acids and about 0.05 wt.% Moisture.
    Example 2. Example 1 is repeated, with the difference that instead of soybean oil, rapeseed oil containing a separate mucous phase with a phosphorus content of 219 g / ml is used. A purified oil is obtained with a residual phosphorus content of 6.2 g / ml. Example 3. Example 1 is repeated.
    0 the difference is that instead of soybean oil they use sunflower oil containing a separate mucous phase with a phosphorus content of 93 g / ml. Get refined oil with a residual phosphorus content
    5 4.8 g / ml.
    Example 4. Example 1 is repeated with the difference that the first and second centrifugation stages are carried out at 1500 and 5800d for 26 and 15 seconds, respectively.
    0 The oil withdrawn from the second stage of centrifugation (7230 kg / h) is subjected to double countercurrent washing with water taken in an amount of 5% by weight at 90 ° C. phosphorus, 120 hours / billion of iron, 0.45 wt.% free fatty acids and about 0.05 wt.% moisture. The oil loss is 0.9% by weight based on the weight of the purified oil.
    0 Series and 5. Repeat example 1 with
    the difference is that the first and second centrifugation stages are carried out at 5500 and 8800 g for 10 and 9 seconds, respectively. The mucous phase obtained in the second stage of the centrifuge (the oil content is approximately 99.8 wt.%) Is completely recycled in the amount of 2120 kg / h and mixed with the initial oil supplied to the first centrifugation stage. Oil withdrawn from the second stage of centrifugation
    (6660 kg / h) are subjected to double counter-rinsing with water, taken in an amount of 5% by weight, at 90 ° C. The oil obtained after drying has the following quality: 3.2 parts / ml of organic phosphorus, 50 hours / billion of iron, 0.45% by weight of free fatty acids and 0.05% by weight of moisture. The oil loss is 0.85% by weight based on the weight of the purified oil.
    Example 6. Example 1 is repeated, with the difference that the first and second centrifugation stages are carried out at 1000 and 4000d for 30 seconds at each stage. The mucous phase obtained in the second stage of centrifugation (oil content approximately 97% by weight) is completely recycled in the amount of 5650 kg / h and mixed with the initial oil supplied to the first stage of centrifugation. The oil withdrawn from the second centrifugation stage (3240 kg / h) is subjected to double countercurrent washing with water, taken in an amount of 5% by weight, at ambient temperature. The oil obtained after drying has the following quality: 7.2 parts / ml of organic phosphorus, 150 parts / billion of iron, 0.45% by weight of free fatty acids and 0.05% by weight of moisture. The loss of oil is 1% by weight based on the weight of the purified oil.
    Example 7. Example 1 is repeated with the difference that the first and second centrifugation stages are carried out at 8000 and 15000 g for 5 s at each stage. The mucous phase obtained in the first stage of centrifugation (oil content approximately 99.8 wt.%) Is completely recycled in the amount of 1120 kg / h and mixed with the initial oil supplied to the first stage of centrifugation. The oil withdrawn from the second centrifugation stage (7540 kg / h) is subjected to double countercurrent washing with water, taken in an amount of 5 wt.%, At 100 ° C. The oil obtained after drying has the following quality: 2.1 parts / ml of organic phosphorus, 37 hours / billion of iron, 0.45% by weight of free fatty acids and 0.05% by weight of moisture. The oil loss is 0.8% by weight of the purified oil.
    Example 8. Example 6 is repeated, with the difference that the oil withdrawn from the second stage of centrifugation (3240 kg / h) is subjected to double countercurrent washing with water taken in an amount of 10% by weight. at ambient temperature. The oil obtained after drying has the following quality: 6.1 parts / ml of organic phosphorus, 135 hours / billion of iron, 0.45% by weight of free fatty acids and 0.05% by weight of moisture. Loss of gauze is 1% by weight of the weight of the purified oil.
    Example 9. Example 7 is repeated, with the difference that the oil withdrawn from the second stage of centrifugation (7540 kg / h) is subjected to a single countercurrent washing with water, taken in an amount of 20 wt.%, At 100 ° C. The oil obtained after drying has the following quality: 9.3 parts / ml of organic phosphorus, 160 hours / billion of iron, 0.45% by weight of free fatty acids and
    0 0.05 wt.% Moisture. The loss of oil is 0.8% by weight based on the weight of the purified oil.
    Example 10. Example 7 is repeated with the only difference that the oil withdrawn from the second stage of centrifugation (7540 kg / h)
    5 without prior washing with water is served for drying. An oil of the following quality is obtained: 39.6 parts per ml, organic phosphorus, 141 parts per billion of iron, 0.45% by weight of free fatty acids and 0.05 May,% of moisture, The loss of oil is 0, 8 wt.% From the weight of the purified oil.
    PRI me R) 1. 4500 kg / soybean oil having a separate mucous phase, containing 110 g / ml of phosphorus, 0.50 wt.%
    5 free fatty acids, 0.25 wt.% Of volatile compounds and moisture and 0.05 wt.% Of other impurities, with a temperature of 60 ° C are fed to the first stage of centrifugation at 3800 g for 15 s. Diverted from the first
    0 centrifugation stage, the oil is fed to the second centrifugation stage, carried out at 5800d for 15 s. The mucous phase obtained in the second stage of centrifugation (oil content of about 99.5% by weight) is completely recycled in the amount of 810 kg / h and mixed with the initial oil supplied to the first stage of centrifugation. The oil withdrawn from the second stage of centrifugation (3320 kg / h) is subjected to double countercurrent washing with water taken in an amount of 5 wt.% At 60 ° C. The oil obtained after drying has the following quality: 3.7 parts / ml of organic phosphorus,
    5 90 hours / billion of iron, 0.45 wt.% Free fatty acids and about 0.05 wt.% Moisture. The oil loss is 1.1% by weight of the purified oil,
    Example 12. Example 1 is repeated.
    0 with the difference that the first stage of centrifugation is carried out at 900d for 40 s. At the same time, the oil from the phase withdrawn from this stage practically contains even I the entire amount of the mucous phase of the initial
    5 oils.
    Example 13. Example 1 is repeated, with the difference that the second stage of centrifugation is carried out at 3900d for 15 seconds. You get a product of the following quality: 88 hours / ml of organic phosphorus, 165 hours / billion of iron, 0.45 wt.% Free fatty acids and about 0.05 wt.% Moisture. The oil loss is 0.95% by weight based on the weight of the purified oil.
    Comparison of the results of the comparative examples with the results of example 1 indicates the significance of the lower limits of the centrifugal field at both stages of centrifugation.
    Example 14. Example 7 is repeated, with the difference that the first and second centrifugation stages are carried out at 8200 and 15500d for 5 s at each stage. An oil of the following quality is obtained: 2 parts / ml of organic phosphorus, 36 parts / billion iron, 0.45% by weight of free fatty acids and about 0.05% by weight moisture. The oil loss is 0.8 wt.% Based on the weight of the purified oil.
    A comparison of the results suggests that exceeding the upper limits
    The centrifugal floor at both stages of centrifugation practically does not lead to further improvement of the product quality and enhancement of the positive effect in the part of oil loss.
    权利要求:
    Claims (2)
    [1]
    1. A method of continuous purification of triglyceride oil from the mucous phase, including centrifuging the oil in two stages and drying, so that, in order to simplify the process and reduce losses, the first and second stages of centrifugation held for 5-30 seconds at 1000-8000 and 4000-15000d, respectively, and the mucous phase from the second stage is recycled to the original oil.
    [2]
    2. A method according to claim 1, characterized in that the oil is washed before drying in
    countercurrent with water in an amount of 5-20 wt.%.
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    同族专利:
    公开号 | 公开日
    HU207528B|1993-04-28|
    HUT54728A|1991-03-28|
    CS274698B2|1991-09-15|
    MX169765B|1993-07-23|
    US4927544A|1990-05-22|
    CA1322201C|1993-09-14|
    DE68907274T2|1993-09-30|
    CS412689A2|1990-10-12|
    EP0349718A3|1990-05-30|
    PL278805A1|1990-01-08|
    EP0349718A2|1990-01-10|
    DE68907274D1|1993-07-29|
    ES2041366T3|1993-11-16|
    PL161824B1|1993-08-31|
    EP0349718B1|1993-06-23|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    CA565061A|1958-10-21|M. Watson Byron|Process for treating glyceridic oils and fats|
    US2702813A|1952-03-05|1955-02-22|Laval Separator Co De|Refining of fatty oils and fats|
    US3093667A|1961-04-27|1963-06-11|Staley Mfg Co A E|Refining soybean oil|
    DE1692566A1|1967-04-18|1971-08-05|Unilever Nv|Process for the production of partially hydrolyzed plant phosphatides with an improved emulsifying effect|
    SE7703258L|1977-03-22|1978-09-23|Alfa Laval Ab|WAY TO EXTRACT FLOUR AND FAT FROM ANIMAL RAVARA|
    GB8307594D0|1983-03-18|1983-04-27|Unilever Plc|Triglyceride oils|
    US4501671A|1984-01-03|1985-02-26|Alfa-Laval, Inc.|Method and apparatus for treatment of oily waste|
    GB8506907D0|1985-03-18|1985-04-24|Safinco Coordination Centre Nv|Removal of non-hydratable phoshatides from vegetable oils|ES2055634T3|1991-04-02|1994-08-16|Vandemoortele Int Nv|PROCEDURE FOR THE CONTINUOUS ELIMINATION OF A GUM PHASE OF A TRIGLYCERED OIL.|
    EP0560121A3|1992-03-09|1994-07-27|Vandemoortele Int Nv|Method for refining glyceride oil|
    EP0583648A3|1992-08-19|1995-02-01|Vandemoortele Int Nv|Continuous refining process with reduced waste streams.|
    US8507703B2|2007-11-27|2013-08-13|Grace Gmbh & Co. Kg.|Purification of fatty materials such as oils|
    US8876922B2|2007-12-21|2014-11-04|Grace Gmbh & Co. Kg|Treatment of biofuels|
    GB0904787D0|2009-03-20|2009-05-06|Desmet Ballestra Engineering Sa|Improved enzymatic oil recuperation process|
    MY161428A|2012-09-12|2017-04-14|Sime Darby Malaysia Berhad|Extracting Lecithin From Palm Agro-Waste|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    EP88110751|1988-07-06|
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