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    • 专利摘要:
    This invention relates to the simultaneous preparation of fatty acid nitriles and glycerol. The goal is to increase the purity of the target products. Production is carried out by reacting glycerides with ammonia in the amount of 400–800 l / kg glycerol in 1 h at 230–260 ° C in the presence of 2–5 wt.% Catalyst — salts of ZN, PB, CD, CO, or FE, saturated or unsaturated. aliphatic monocarboxylic acid or monoalkylbenzene-, naphthalenemono-, alkanmonosulfonic acid or diorganol (4+) - bis-sulphonate, at the main stage, withdrawing from the reactor the formed mixture of products consisting mainly of water, glycerin and containing fatty acid and fatty amide fatty acid nitrile acids until this If you don’t practically retain glycerol, condense the product mixture and separate the glycerin and upper fatty acid nitrile into the lower phase, return the latter back to the reactor and perform additional processing of 15-100 l of ammonia per 1 kg of the fatty acid containing nitrile in the reactor and its amide, at 1 hour at 275-300 ° C in the presence of a catalyst of the main stage, until all the fatty acid and fatty acid amide are converted to fatty acid nitrile. The upper phase is recovered during the conversion of glycerin, whereby the connecting pipe from the reactor to the condensation device is heated to the temperature at which the glyceride is converted, and the additional treatment with ammonia begins as soon as the glycerol conversion ends. 1 hp f-ly, 1 tab.
    公开号:SU1551243A3
    申请号:SU874203696
    申请日:1987-11-20
    公开日:1990-03-15
    发明作者:Штюлер Херберт；Фишер Курт
    申请人:Хехст Аг (Фирма)；
    IPC主号:
    专利说明:

    This invention relates to the simultaneous production of fatty acid nitriles and glycerol from glycerides: vegetable or animal fats, or oils, or tricaprylin, or tristearin, or glycerol monoarate, or glycerol monooleate.
    The purpose of the invention is to increase the frequency of target products.
    According to the method of simultaneous production of fatty acid nitriles and glycerin by reacting glycerides in the reactor with ammonia in an amount of 400-800 l / kg glycerol per hour at 235 2 ° C in the presence of May. 5 catalyst - salts of Zn, Pb, Cd, Co or Fe saturated or unsaturated aliphatic monocarboxylic acid.
    or monoalkylbenzene-, naphthalenemono-, alkane monosulfonic acid or diorganic-tin (IV) -bisulfonate at the main stage, removing the formed mixture of products consisting mainly of water, glycerol and containing fatty acid and amide of nitrile from the eeactor hydrochloric acid, until practically glycerin remains in this mixture, condensation of the mixture of products and separation into the lower phase of glycerin and the upper phase of the nitrile of fatty acid, return of the latter to the reactor and additional treatment of ammonia per 1 kg of them fatty acid containing nitrile in the reactor, containing fatty acid and its amide, at 1 h at 275 300 ° C in the presence of a catalysis cathode of the main stage until all fatty acid and fatty acid amide is converted to nitrile fatty acid, return the upper phase is carried out during the conversion of glyceride, while the connecting pipe from the reactor to the condensation device is heated to the temperature at which the glycerol is converted, and the additional treatment with ammonia is started as soon as it ends, turning of glitseridch. The upper phase is recovered continuously.
    Example K In this example, crude fatty acid nitrile ao, the conversion time of the glycoride is returned back to the reaction continuously.
    500 g of animal carcass fat (saponification number 185, acid number 13.9) and 10 g of zinc dodecylbenzene sulfonate as a catalyst (these are 3 wt.% Of catalyst, calculated on the basis of fat or glyceride) are loaded into the reactor. Reactor volume of 700 mp is equipped with a heater
    „
    a device for heating the contents to the reaction temperature, an agitator for mixing the contents, an internal thermometer for setting the present temperature and a gas line for the flow of ammonia. The reactor torus is connected to a cooling column, (condenser), which is located above the reactor and to the side of it. The pipeline from the top of the reactor to the bottom of the cooling column is electrically heated. The base of the cooling column is connected to a cylindrical vessel with a volume of 100 ml for receiving and precipitating condensed 0
    five
    ponentov phases. From the vessel, which is a collector, goes the pipeline to the reactor. This pipeline goes from the upper part of the collector to the upper part of the reactor and is inclined to the reactor so that there is a flow from the collector to the reactor.
    During preheating, the reactor is flushed with nitrogen. At 150 ° C, nitrogen is replaced with ammonia gas, which is circulated in an amount of 600 liters of ammonia per 1 kg of animal carcass fat (internal fat of cattle), per hour. The reactor and thus the contents of the reactor are heated to 230 ° C (start conversion of glyceride or the main reaction) and maintain this temperature W. Fresh ammonia gas is continuously added during the reaction in order to maintain the indicated 600 L of ammonia. After 3 h of reaction time, the temperature is raised for 1.5 h from 230 to 260 ° C, the temperature of 2 bc is maintained for 30 min. At the end of this time (this is 5 hours of reaction), glycerol is practically no longer contained in the extracted product mixture, which indicates the end of the conversion of the injected fat of the livestock with ammonia (the end of the conversion of glyceride or the end of the main reaction). During the conversion of glyceride, which starts at 230 ° C, the resulting mixture of products, consisting mainly of glycerol, crude fatty acid nitrile and water, with an excess flow of ammonia is removed through first heated to 230 ° C and then to 2bO ° C
    40
    45
    connecting pipe from the reactor to the cooling column (in this case, it is achieved that condensation of glyceride in this pipeline and thereby the return of glycerol to the reactor is excluded). Both components, glycerin and crude fatty acid nitrile (the latter contains about 2 wt.% Fatty acid and 3 wt.% Fatty acid amide), are almost completely condensed in the cooling column and collected in the collector during precipitation. the lower phase of glycerol and the upper phase of the crude fatty acid nitrile. The ammonia and mostly all the water are discharged from the cooling column in gaseous form (ammonia is returned back to the reactor after separation of the water). The temperature of the collection and thus its contents is maintained at 15CfC,
    50
    whereby residual water and dissolved ammonia, if necessary, are removed. The glycerin phase is kept in motion with a magnetic stirrer in order to speed up and complete the removal of ammonia.
    A collection with a capacity of 100 ml after −30 min of the reaction time is filled with 90 ml before the point of onset being connected to the fatty acid nitrile. A clean, flexible pipeline to the reactor (i.e., before the catalyst is only still a catalyst,,
    A single pipe and goes back to the reactor (the collector is separated from the ayooooa and from the cooling column, as it is no longer required) at the beginning of the additional reaction. After the mentioned reaction time (1.5 c), the components to be converted (fatty acid and fatty acid amide) turn over the transition,). During this time, about 15% v / v, glycerol plus crude fatty acid nitrile, in terms of the expected total amount of glycerol and crude fatty acid nitrile (90 ml consists of 8 ml of glycerin and 8 ml of fatty acid nitrile) are output. After filling the collector, a forced return flow of ct poro nitrile of fatty acid begins through the connecting pipe to the reactor. Traced nitrile fatty acids are removed from the reactor and released from the catalyst at the distillation stage.
    The following results were obtained: 38 ml (kS g) of glycerol, this is 90 May, / from theory, and glycerol is practically free from water, fatty acid, fatty acid amide and fatty acid nitrile and, therefore, without kg of any further cleaning operation. already present pure glycerin; 533 ml (j.fg) of nitrile fatty acid is 95% by weight of theory. The resulting nitrile
    respectfully
    now return inevitably
    in the reaction the same amount of raw
    fatty acid nitrile. Clean, obsessing only more catalyst,,
    A single pipe and goes back to the reactor (the collector is separated from the ayooooa and from the cooling column, as it is no longer required) at the beginning of the additional reaction. After the indicated reaction time (1.5 c), the components to be converted (fatty acid and fatty acid amide) are converted to fatty acid nitrile from the reactor and released from the catalyst at the distillation stage.
    The following results were obtained: 38 ml (kS g) of glycerol, this is 90 May, / from theory, and glycerol is practically free from water, fatty acid, fatty acid amide and fatty acid nitrile and, therefore, without kg of any further cleaning operation. is already pure glycerin; 533 ml (j.fg) of nitrile fatty acid is 95% by weight of theory. The resulting nitrile
    thirty
    35
    40
    fatty acid nitrile, which is free of fatty acid, is free of glycerol during conversion of fat with ammonia and discharged with ammonia along with glycerin and reaction water (the connecting pipe from the collector to the reactor is heated to a temperature corresponding to the reaction temperature to avoid cooling flow through the connecting pipe and possible cooling in the reactor). After the conversion of glycerol is complete, t, e, after 5 hours of reaction time, the desired glycerol is removed from the side. The amount of crude fatty acid nitrile found in the collector is fed to the reactor (this amount of crude fatty acid nitrile is very small compared to the total amount of crude fatty acid nitrile). The temperature of the reactor, in which the entire quantity of crude fatty acid nitrile is present, is raised to PDO C, and the flow of ammonia is reduced to 100 liters of ammonia per 1 kg of crude fatty acid nitrile in 1 hour. These conditions (i.e., additional reaction conditions) are maintained in for 1.5 hours. The reaction water formed in the additional reaction is discharged with an excess flow of ammonia through the unheated connection pipe and cooling column. Despite the small flow of ammonia carried with it, in the case of fatty acid nitrile, it is already condensed in unheated soybean water and contains only 0.25 more May. amide of fatty acid and 0.2 mae. of fatty acid.
    EXAMPLE 2, this example of crude and / or fatty acid, during the conversion, glyceride is periodically returned to the reaction,
    The example is carried out with the same components and under the same reaction conditions as in Example 1, with the difference that the crude fatty acid nitrile formed and removed during the conversion of the glyceride is not returned to the reaction, but in parts.
    The device used in Example 1 is changed for this purpose in such a way that the collection has a capacity of 200 ml. the connecting pipe from the collector to the reactor is not installed in the upper part of the collector, but in its lower part, and the collector also has a locking device.
    The refill is filled to overflow (from the start of glyceride conversion up to this point, 15 minutes elapse and about 5 ml of ggi are deposited and precipitated in the collector, about 40 ml of crude fatty acid nitrile, i.e. 8% by volume from the expected quantities of glycerol plus crude 55 fatty acid nitrile), for about 30 minutes, a forced reverse flow of crude fatty acid nitrile is maintained, then the reverse flow is interrupted with the aid of the mentioned locking device 45
    50
    0
    five
    0
    5 fatty acid free from glycerol
    and water and contains only another 0.25 mue. S fatty acid amide and 0.2 mue. fatty acid.
    EXAMPLE 2, this example of crude and / or fatty acid, during the conversion, glyceride is periodically returned to the reaction,
    The example is carried out with the same components and under the same reaction conditions as in Example 1, with the difference that the crude fatty acid nitrile formed and removed during the conversion of the glyceride is not returned to the reaction, but in parts.
    The device used in Example 1 is changed for this purpose in such a way that the collection has a capacity of 200 ml. the connecting pipe from the collector to the reactor is not installed in the upper part of the collector, but in its lower part, and the collector also has a locking device.
    The refill is filled to overflow (from the start of glyceride conversion until this point 15 minutes pass and about 5 ml of ggi are deposited and precipitated in the collection, about 40 ml of crude fatty acid nitrile, i.e. 8% by volume of the expected amount glycerol plus crude 5 fatty acid nitrile), for about 30 minutes, a forced reverse flow of crude fatty acid nitrile is maintained, then the reverse flow is interrupted with the help of a named locking device
    0
    so that in the collector, the crude nitrile is fatter-acidic; after 15 minutes, about) ml of crude fatty acid nitrile are collected and sent back s reactor (dos / ru) by opening the locking device H and then closing the locking device for dropping vanilla of the same amount of raw nitride acid- .Q lots. The described process of accumulation and periodic (in parts) removal of the crude fatty acid nitrile at the end of the glycerol conversion is achieved after 5 hours, repeated 9 times. Further, they act as in dimension 1.
    Obtained: 38 ml (Lg) of glycepin, this is 9U May. /, From theory, we will look for glycerin practically free of water.
    FATTY ACID, CHMID HlpHO.1 ACID
    20
    and nitrile fatty acid and, therefore, without any operation, I clean up and go to clean the glycerol; 533 - f (2c g) nitrile of lyric acid, this is the S5 May / o g 25 theory. The resulting nitfl fatty acid is free of water п-pycerite and there are still only 0.2 of us. , ° aiido
    FATTY SIZES AND 0.2 MЈS. IrNO KIS
    Lots.ZS
    The examples used in example I and 2 of the carcass of the predatorship mixture are mainly from XIHDO ooraToio cattle, CHI-oanego fat,: sleepy and bone fat.
    II p and meper fc, 3 7 –prescribe 1 yu g similar to the winner t and e with other glycerides, cat alizgpor, ammonia quantities (XB-,, i cmmp:; rat urah and / or reaction times, ihs Indicators / 1Ps, in particular, the names of all ians and the results of make-up artists (the current percentages are ma,: marketing percentages; out of two numbers that are shown in brackets after the glyceride used, the first number indicates the number of saponification, and the second is the acid number; the data in percent after the catalyst indicates the amount of catalyst).
    Example 3- Technical beef tallow (186; 12.6); n-dode 1yls; / lonfonate lead, Z-o, 01) l Shee at the same time converting glycerite and 1 UO l N1 during an additional reaction; temperature
    acid 93 j with JS13 - amide, acid and 0.1% fatty acid,
    fl p and me k. Edible fat (190: 2, -); c-n-okgadecylsulfonate cadmium, 2n; 800 l N11 s during conversion
    35
    50
    55
    glyceride and 100 l of N113 in the voice of an additional reaction: gempeoate / pa of the reaction during the conversion of glyceride 2JJ C, 3 and, noB-tjenne to 2 ° C for 1 hour (5 ° C 1 S min), i y-p. i peak, (chi with additional Zoi O,, 3 and. and. Result: you / sd ggitserinl 914, output of nitrile zhio-yu - islo- Toi Uy about less than 0.1 amide of peaceful acid and less than 0.1 fatty ki pots.
    PRI me R 5. With another w / ip (124; 11.7) koba.cht v-oxanesulfonate, k%, chOO l time for the transformation of the face and 1bl of NfiI3 during the additional reaction; the reaction temperature in the conversion of glyceride is 230 ° C, 3 hours, then increase to 2 ° C in 1 hour (j ° C in 15 minutes), the temperature of the additional reaction is 2/5 ° C, 2 hours glyceoin, the yield of nitrile fatty acid 9 with 0.22-aru and wnpt-ol acid and 0.20-3 fatty slots,
    P p and measures 6. Sunflower, -. Oil (0.8); iron (II) -n-butylnaph halium sulfonate, 5%; A00 L N11 Sun time (glyceride and 50 L N113 during the additional reaction; the temperature of the reaction for the conversion of gly-, erida 2hO ° C, t h and with the additional reaction 3-Ul) °,, b m. Result; g; Icerolin 87%; Y-yield of fatty acid 91% with 0} 20 amide of peaceful acid and 0.15% fatty acid.
    Example. Soybean May t 203; 0.5); di-p-octyltin (IV) -bis- (toluene-sulfonate), 2%; 800 time: revaachenyl glyceride: -, 50 l N11, during the additional reaction, the reaction temperature as in example 5 “Result: glycerin 89 yield, fatty acid nitrile yield from 0.18 /; fatty acid amide and 0,10- ;; fatty acid :,
    Examples 8 to 13. Carried out analogously to example 2, with other glyceride catalysts, amounts of ammonia (NHj), temperatures and / or reaction times. Below, in particular, these variations and the results of the examples are given (all percentage G, others represent mass percentages of the reaction during the conversion of glyceriases 2B O C, 3 hours and with additional rectification 28U ° C, 1, ii hours. Result: glycerol yield 86 % s exit nitrile fat
    glyceride and 100 l of N113 in the voice of an additional reaction: gempeoate / pa of the reaction during the conversion of glyceride 2JJ C, 3 and, noB-tjenne to 2 ° C for 1 hour (5 ° C 1 S min), i y-p. i peak, (chi with additional Zoi O,, 3 and. and. Result: you / sd ggitserinl 914, output of nitrile zhio-yu - islo- Toi Uy about less than 0.1 amide of peaceful acid and less than 0.1 fatty ki pots.
    PRI me R 5. With another w / ip (124; 11.7) koba.cht v-oxanesulfonate, k%, chOO l time for the transformation of the face and 1bl of NfiI3 during the additional reaction; the reaction temperature in the conversion of glyceride is 230 ° C, 3 hours, then an increase to 2 ° C for 1 hour (j C in 15 minutes), the temperature is up to 5
    WITH
    1P
    five
    50
    55
    complementary reaction 2/5 C, 2 h „° e-, the yield of glyceoin, the yield of nitrile fat-acid 9 with 0.22-aru and wnpt-ol acid and 0.20-3 fatty hours,
    P p and measures 6. Sunflower, -. Oil (0.8); iron (II) -n-butylnaph halium sulfonate, 5%; A00 L N11 Sun time (glyceride and 50 L N113 during the additional reaction; the temperature of the reaction for the conversion of gly-, erida 2hO ° C, t h and with the additional reaction 3-Ul) °,, b m. Result; g; Icerolin 87%; Y-yield of fatty acid 91% with 0} 20 amide of peaceful acid and 0.15% fatty acid.
    Example. Soybean May t 203; 0.5); di-p-octyltin (IV) -bis- (toluene-sulfonate), 2%; 800 time: revaachenyl glyceride: -, 50 l N11, during the additional reaction, the reaction temperature as in example 5 “Result: glycerin 89 yield, fatty acid nitrile yield from 0.18 /; fatty acid amide and 0,10- ;; fatty acid :,
    Examples 8 to 13. Carried out analogously to example 2, with other glyceride catalysts, amounts of ammonia (NHj), temperatures and / or reaction times. Below, in particular, these variations and the results of the examples are given (all percentage G, others are mass percent; of the two numbers given in parentheses after the glyceride used, the first is the saponification number and the second is the acid number; data in percent after the catalyst denote the amount of catalyst introduced).
    And p and me R 8. Palm oil
    (202; 0.7); zinc-C, 5 / CGS-alkanesulfonate, while the same temperature program is kept at 3%; 400 L NHj during conversion are ny in Examples 1 and 2). Result: glyceride and 15 l of MC during supplemental - glycol serum 93%, nitrile yield
    body reaction; reaction temperature as in example $ Result: you-. Glyceoin flow 92%, fatty acid nitrile yield 95% with 0.28% fatty acid amide and C, 23% fatty acid.
    PRI me R 9. Coconut oil (240; 1,8); lead salt of fatty acid fat, 5%; 600 l NH3 during pre-ammonia quantities, temperatures
    the growth of glyceride and 10U l NH, during the additional reaction; reaction temperature as in example 6, Result: 84% glycerol yield, fatty acid nitrile yield 9 with 0.24% fatty acid amide and 0315% fatty acid
    Example 10. Castor oil (173; 1.8); cadmium — methylbenzene (either at the time or at the reaction time. Below are the parameters and the results of the POR (indicated in the examples of the note are also found here). 25 Example 14. Glyirin eetriacrylate or tricaprylin (159; 2.8); - octchdecylopic (IV) -bis- (p-octadecyl-with pOonat) 5 4x; the amount of peratra reaction, as in example 4
    NHj, 1 temluol) sulfonate, U / ,; 800 l NH3 at time-30 Result; the yield of glycerol 89% yield
    m conversion of glyceride and 50 ml of NH3 during an additional reaction; reaction temperature as in example 3. Result: the yield of glycerol is 74%, the yield of fatty acid nitrile is 65% with 0.20% fatty acid amide and 0.18% fatty acid.
    Example 11: Colza oil (167; 1.8); yy-dodecylnaphthalene sulfonate cobalt, 4%; 600 L HNE during the conversion of glyceride and 50 L HN3 during the additional reaction; reaction temperature as in example 6, Result: the yield of glycerol is 89%, the yield of fatty acid nitrile is 91% with 0.16% fatty acid amide and 0.12% fatty acid.
    PRI me R 12. Whale fat (189; 6,3); iron hexylbenzenesulfonate, 4%; 400 L of NH3 during the conversion of glyceride and 50 L of NH3 during the additional reaction; reaction temperature as in example 3. Result: the yield of glycerol is 83%, the yield of fatty acid nitrile is 86% with 0.27% fatty acid amide and 0.23% fatty acid,
    EXAMPLE 13. Technical beef tallow (186; 12.6): di-p-butyl-tin (IV) -bis- (p-dodecylbenzenesulfonic
    NMGRYL PEACEFUL ACID 44% C 0.18%
     hrrnay acid and 0.12% fatty
    ACID b.
    Example 5. Glyceroltristearag igi uvstearin (187; 6.7), diphenylol 40
    in (-bis - (-1 octylsulphonate), 2%; oOU and XH3 during the conversion of the glyceoid and 50 l of NOEC during the additional reaction, the reaction temperature, as in Example 3). Result: glycerin yield 92%, yield. 95% fatty acid nitrile with 0.17% fatty acid amide v O8 i4% fatty acid,
    PRI me R 16. Glycerol monolaurate 45 0/8: 3; 8); diphenyltin (iv) -onc- (n- -hexadicylsulfonate), 3% 5,800 l NH $ during the conversion of glyceride and 15 liters NH3 during the additional reaction; reaction temperature ”as in example 6. Result; the yield of glycerol is 92%, the yield of fatty acid nitrile is 94% with 0.19% fatty acid amide and 0.12% fatty acid :.
    Example 1 / “Glycerol monooleate (172; 4,6); diphenyltin (IV) -bis- (fexyl sulfonate), 2%; 400 L NHa during the conversion of glyceride and 100 L NH3 in the prem of the additional reaction; reaction temperature as in example 1. Re50
    55
    nat), 2%; 800 L NH3 during the conversion of glyceride and 100 L NH3 during the additional reaction. The reaction temperature in the conversion of glyceride 230 With 3 h; then increase to 260 ° C for 1.5 hours (5 ° C for 1 minute) and 0.5 u at 2 ° C, temperature during the additional reaction is 300 ° C, 1.5 hours (96% acid with 0.14% fatty acid amide.
    1 p and merys 14-17. Carried out analogously to example 1, but with mono- or triglycernds as a glyceride, with diorganol (IV) bis-sulfonates as catalysts, and with other
    ammonia quantities, temperatures
    and / or reaction times. Below indicate. The gi variations and the results of the POR (the notes in the examples are also found here). Example 14. Glyaintricaprilat or tricaprilin (159; 2.8); di-p-octchdecylopovo (IV) -bis- (p-octadecyl-with pOonat) 5 4x; the amount of pera the reaction, as in example 4
    NHj, 1 topic; the yield of glycerol 89% yield
    NMGRYL PEACEFUL ACID 44% C 0.18%
     hrrnay acid and 0.12% fatty
    ACID b.
    Example 5. Glycerol tristearate igi uvstearin (187; 6.7), diphenylol
    in (-bis - (-1 octylsulphonate), 2%; oOU and XH3 during the conversion of the glyceoid and 50 l of NOEC during the additional reaction, the reaction temperature, as in Example 3). Result: glycerin yield 92%, yield. 95% fatty acid nitrile with 0.17% fatty acid amide v O8 i4% fatty acid,
    PRI me R 16. Glycerol monolaurate 0/8: 3; 8); diphenyltin (iv) -onc- (n- -hexadicylsulfonate), 3% 5,800 l NH $ during the conversion of glyceride and 15 liters NH3 during the additional reaction; reaction temperature ”as in example 6. Result; the yield of glycerol is 92%, the yield of fatty acid nitrile is 94% with 0.19% fatty acid amide and 0.12% fatty acid :.
    Example 1 / “Glycerol monooleate (172; 4,6); diphenyltin (IV) -bis- (fexyl sulfonate), 2%; 400 L NHa during the conversion of glyceride and 100 L NH3 in the prem of the additional reaction; reaction temperature as in example 1. D
    1 I1b
    the result: the output of gtitserich 90 / the output of nitrile fatty acid P with O, zmida fatty acid and 0, fatty acid,
    EXAMPLE 13 When carrying out the following PDPs are used, and for the rest, each time Example 1 is carried out. Catalysts: zinc, zinc stearag, zinc erukaag, lead-zinc-j

    p-dodecylbenzoate. cadmium 2-methylnaphthoate, zinc perfluorohexylsuljonate, cobalt-2-hydroxy-p-dodecane uljunate and a mixture of 1 wt. / 3 of zinc-p-dodethylbenzene sulfonate and 1 May. /, kagmiitopuolsulfonat.
    Result: exits are glistened 82 - 96 May. j, waste of nitrous acidic liquids 8E-U6 masD with (}, ms. ° /, ag. fatty number r s and 0.11-0.20 may, /; fatty acid „
    The table shows the results of the example 1Y for each i-cnor izomogo kata bottom ioca
    The proposed method is compared with the well-known half-life in a child without a dog or a dog.
    CLEANING WITH TEMPLE-iM VYKSDOM CLEAN GLI
    free-of-lead cerin, zh1-one acid, amidt of peaceful acid and fatty qypote nitrile, as well as receive neither f RIL OF FATTY ACID, TERMINAL GLITS
    Water and water, So.Tezhaschiny / Ogko 0.1 0.28 May a mil h– d: / / sg and 0.1–0.23 May, 54 July.
    权利要求:
    Claims (1)
    [1]
    1. One way of preparing for obtaining nitriles of fatty acids and glycerol from glycerides by reacting vegetable v 1 and life fats or oils, or t) icapailein, or tristearin, or glycerin monolate, or glycerimide, oleum i, as glyceoids with ammonia, in the reactor. in the amount of VJU-8U) g / kg i tizer yes in
    1h at 23U- 60C L in npf-th vii
    2b wt.% Catalysis of rop.i - salts
    0
    0
    P
    Ze
    "40
    45
    5С
    lp L, ((I, Co or It JTCbin Nchsi or nenas yi (RNioy Alifa1 l Ssk JH monograthic or moshzalkig (enzol-, iaf ts.linmono- / lka 1monosl-Pokislogy ipi and p (K -o-t- g y / i phon ga of the main md and ipo from the reactor through (. connection with the thermal sensation organizer P) of the mixture formed by D TVK, sss-i1, it is mainly from The fatty acid and the acid amide nitrite fat with l TSI until o) t- will remain practically i dens (and the mixture of prod who is ionic equipment and oatg | g iborpesaefCM collection 0 and 1 o / - glytiine i- n tr ha acid, content of P1, th Ir- to TV and omed fatty acid, returning the top of the line, crawled and processed a la kiait i kg available in rst with fatty acid and m pi-o, or rig fatty; poi 2 / Ь F npi / rcyi g HEY; / ataliza-oa smovnoi to tz roos-ooss kss kirna is sour, but a and a g d ng and sour doesn’t transform -, s-prli liyochi kispo.y, about g l and h and about ii and with g TJM, which, in order to increase the number of otsh of the target products, will be connected with the pipe from the reactor to the condensation of the pceoai Eni-ni-tsrida to heat the plasma tag 5 roi - which is carried out by tspstnechl erida and g ovrat verhne collection of the reactor y1 stvl & & the time of the retrac- tion of g / miegidt, and the ielny of the type of miax mnax npchynz - it, as in the past; / 1 h from h. - icha-preyr Nienie.
    /. Demolition according to claim., Tl lO I and g i i, which is in: glt ver 1n the reactor of the osui, ec, a, p- -cLbi3- but, with RO spc. Rev- | n / a, exercise the number of the top eeactor for that e unit / and c .pei and in the same amount.
    Zn-caprylate89
    Zn-stearate92
    Zn erukaat92
    Pb-2-methylbenzoate86
    Zn-j-dodecylbenzoate88
    Cd-2-methylnaphthoat82
    CP-perfluorohexanesulfonate9 Co-2-hydroxy-n-dodecanesulfonate93 A mixture of 1 wt.% N-dodecyl benzene sulfonate and 1 wt.% Cd-toluene sulfonate "96
    93 9 93 92 9 89 96
    9
    96
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    US2486455A|1949-11-01|Treatment of acidic compositions
    EP0406945B1|1995-12-06|Process for soap splitting using a high temperature treatment
    US3927110A|1975-12-16|Thermolysis of styrene oxide
    US3364242A|1968-01-16|Separation of gossypol from cottonseed oil
    DE1252652B|1967-10-26|Process for the production of adipic acid dinitrile
    EP0410167A1|1991-01-30|Method of producing 2,2,-dimethyl-3-hydroxypropyl-2,2-dimethyl-3-hydroxypropionate
    US3708513A|1973-01-02|Method of synthesizing fatty acids
    DE1189977B|1965-04-01|Process for the production of benzoic acid
    DE2614827A1|1977-10-20|-Phenyl-|-pyridazone prodn. - by heating ammonium |-hydroxy-|-oxophenyl-butyrate with hydrazine hydrate in aq. soln.
    SU1318610A1|1987-06-23|Method for processing used sodium or sodium-calcium plastic lubricants
    US2381855A|1945-08-07|Raw material for resin synthesis
    DE2823504C2|1989-08-31|
    FR2495137A1|1982-06-04|Para-hydroxy-mandelic acid continuous prepn. - from glyoxylic acid, phenol and sodium hydroxide in aq. soln. in reactors arranged in series
    DE1909440C|1973-07-26|
    Munns et al.1962|The separation of solid fatty acids from liquid fatty acids by the formation of acid soaps. I. Tallow soaps
    同族专利:
    公开号 | 公开日
    PT86163A|1987-12-01|
    IL84547D0|1988-04-29|
    DD262859A5|1988-12-14|
    ZA878694B|1988-08-31|
    ES2023396B3|1992-01-16|
    CN1014605B|1991-11-06|
    DE3771191D1|1991-08-08|
    NO874853D0|1987-11-20|
    EP0273173B1|1991-07-03|
    PT86163B|1990-11-20|
    US4801730A|1989-01-31|
    DE3639857A1|1988-06-01|
    DK610687A|1988-05-22|
    DK610687D0|1987-11-20|
    CA1305182C|1992-07-14|
    NO165394B|1990-10-29|
    CN87107926A|1988-06-01|
    JPS63150235A|1988-06-22|
    BR8706262A|1988-06-28|
    AU8144987A|1988-05-26|
    IE873145L|1988-05-21|
    EP0273173A3|1988-07-20|
    IL84547A|1992-02-16|
    NO874853L|1988-05-24|
    EP0273173A2|1988-07-06|
    NO165394C|1991-02-06|
    PH25220A|1991-03-27|
    AU598881B2|1990-07-05|
    引用文献:
    公开号 | 申请日 | 公开日 | 申请人 | 专利标题
    US3979432A|1974-06-21|1976-09-07|Eastman Kodak Company|Preparation of nitriles|
    ES472553A1|1977-08-20|1979-02-16|Hoechst Ag|Process for the production of fatty acid nitriles and glycerine from glycerides, in particular from natural fats and/or oils.|
    DE3131968A1|1981-08-13|1983-02-24|Chemische Werke Hüls AG, 4370 Marl|METHOD FOR PRODUCING ALIPHATIC NITRILES|
    DE3244752A1|1982-12-03|1984-06-07|Hoechst Ag, 6230 Frankfurt|Process for the preparation of fatty acid nitriles and glycerol from glycerides, in particular from natural fats and oils|DE60102805T2|2000-02-08|2005-04-21|Exxonmobil Chem Patents Inc|PROCESS FOR PREPARING GROUP 14 BURGLED BISCYCLOPENTADIENYL LIGANDS|
    JP4972387B2|2006-03-08|2012-07-11|花王株式会社|Method for producing aliphatic nitrile|
    FR2907781B1|2006-10-27|2010-01-08|Ceca Sa|PROCESS FOR THE SYNTHESIS OF HIGH-PURITY PRIMARY DIAMINS AND / OR TRIAMINS FROM DIMERED OR TRIMERIC ACIDS|
    FR2916445B1|2007-05-24|2009-07-10|Arkema France|PROCESS FOR CO-PRODUCTION OF CYCLIC CARBONATES AND NITRILES AND / OR FATTY AMINES|
    GT200700043A|2007-05-25|2008-03-03|NITRILE FUNCTION BIO COMPOSITES|
    FR2979342B1|2011-08-26|2013-08-09|Arkema France|PROCESS FOR THE SYNTHESIS OF C11 AND C12 OMEGA-AMINOALCANOIC ACID ESTERS COMPRISING A METATHESIS STEP|
    FR3002227B1|2013-02-20|2021-10-01|Arkema France|GAS PHASE AND GAS LIQUID NITRILATION PROCESS|
    法律状态:
    优先权:
    申请号 | 申请日 | 专利标题
    DE19863639857|DE3639857A1|1986-11-21|1986-11-21|METHOD FOR PRODUCING FATTY ACID NITRILS AND GLYCERINE FROM GLYCERIDES|
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