US3732266A - Hydrogenation of oils - Google Patents

Hydrogenation of oils Download PDF

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Publication number
US3732266A
US3732266A US00026509A US3732266DA US3732266A US 3732266 A US3732266 A US 3732266A US 00026509 A US00026509 A US 00026509A US 3732266D A US3732266D A US 3732266DA US 3732266 A US3732266 A US 3732266A
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United States
Prior art keywords
temperature
oil
hydrogenation
coolant
condenser
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Legal status (The legal status 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 status listed.)
Expired - Lifetime
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US00026509A
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English (en)
Inventor
F Dudrow
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SPX Technologies Inc
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Chemetron Corp
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Publication of US3732266A publication Critical patent/US3732266A/en
Assigned to CHEMETRON PROCESS EQUIPMENT, INC. reassignment CHEMETRON PROCESS EQUIPMENT, INC. CHANGE OF NAME (SEE DOCUMENT FOR DETAILS). EFFECTIVE MARCH 24, 1980. Assignors: CHEMETRON-PROCESS EQUIPMENT, INC.,
Assigned to AMCA INTERNATIONAL CORPORATION, DARTMOUTH NATIONAL BANK BLDG., HANOVER, NEW HAMPSHIRE, 03755, A CORP. reassignment AMCA INTERNATIONAL CORPORATION, DARTMOUTH NATIONAL BANK BLDG., HANOVER, NEW HAMPSHIRE, 03755, A CORP. ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: CHEMETRON PROCESS EQUIPMENT, INC. A DE CORP.
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/0006—Controlling or regulating processes
    • B01J19/0013—Controlling the temperature of the process
    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
    • C11C3/12—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by hydrogenation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
    • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
    • B01J2219/00083—Coils

Definitions

  • the present invention relates to a new and improved method and apparatus for providing controlled temperature in a reaction mass and is especially useful in hydrogenation of unsaturated oils.
  • Demand for margarines and shortenings high in unsaturated fats has placed great emphasis on selective hydrogenation processes for producing the same.
  • the exact conditions necessary to achieve a desired nal product from a given type of raw material in a particular system are normally determined by trial and error, and once the conditions and parameters have been established it is very important to provide for a high degree of control repeatability in order to insure a continuous high quality and uniformity of the finished product.
  • vegetable oil such as soybean oil from a particular source is hydrogenated to produce margarine
  • the temperature of the oil during the process must be maintained within a narrow desired range to achieve uniformity of quality and the desired degree of selective hydrogenation.
  • the present invention provides a new and improved method and apparatus for the selective hydrogenation of unsaturated oils, wherein the temperature of the process is accurately controlled and maintained at a predetermined level with very little variation.
  • the invention affords a high degree of controlled repeatability of the hydrogenation process for a given raw material and final product, so that repeated batches can be processed with uniformity of selective hydrogenation.
  • the invention also provides a degree of temperature control previously unattainable.
  • the apparatus of the present invention includes a heat exchanger coil in the reaction vessel and a closed, coolant condensing system is 4in communication with the heat exchanger.
  • the condensing system can be maintained at any desired operating pressure, either subatmospheric or superatmospheric, for example from about 1 p.s.i.a. to about 450 p.s.i.a. Maintenance of superatmospheric pressure on the cooling system enables the coolant to be near the desired operating temperature without vaporizing so that there may be a large quantity of coolant in the coil. Reduction in condensing system pressure causes immediate vaporization so that the time for a temperature change is reduced and much closer temperature control of the hydrogenation process can be established. A-t subatmospheric pressure, the vaporization temperature is sufficiently low that the reaction mass may be chilled.
  • Another object is the provision of a new and improved method and apparatus for controlling the temperature of a hydrogenation process.
  • Yet another object of the invention is the provision of a new and improved method and apparatus for producing food products having controlled polyunsaturates therein by the hydrogenation of unsaturated oils.
  • Another object of the present invention is the provision of a new and improved method and apparatus for the controlled hydrogenation of unsaturated oil wherein the vaporization of coolant from the heat exchanger is controlled by a change of pressure in the coolant system.
  • Another object of the present invention is the provision of a new and improved method and apparatus for the controlled hydrogenation of unsaturated oils where-A in the reaction temperature of the oil is regulated and controlled by the amount of condensing surface in a condenser which is exposed above the surface level of the condensate in the condenser.
  • Yet another object of the present invention is the provision of a new and improved apparatus for the controlled hydrogenation of unsaturated oils having a closed, coolant recirculation system wherein a condenser is provided and coolant liquid condensate is metered from the condenser into the heat exchanger through a temperature controlled regulator valve sensitive to the temperature of the oil in the reaction vessel.
  • a new and improved apparatus for the controlled hydrogenation of unsaturated oils which comprises a reaction vessel for holding a batch of oil and means for introducing hydrogen into the oil below the surface thereof.
  • Heat exchanger means is provided in the vessel for initially heating the oil and thereafter extracting heat from the oil as the exothermic heat of reaction takes place.
  • a closed, coolant condensation system is provided in communication with heat exchanger means to provide for removal of heat at a controlled rate from vaporized coolant as the exothermic reaction proceeds in orde'r to maintain the temperature of the oil at a substantially predetermined value. Cooling takes place in response to a reduction in pressure in the closed condensation system.
  • reaction temperature within a range of plus or minus 7 F. and preferably plus or minus 3 F. of the optimum temperature.
  • a iixed temperature for example, 370 F., may Abe selected or a time-temperature schedule may be followed.
  • the present invention provides a high degreel of controlled repeatability for such hydrogenation processes.
  • FIG. 1 is a schematic diagram illustrating a new and improved apparatus constructed in accordance with the features of the present invention for the controlled hydrogenation of unsaturated oils.
  • a pressure vessel of the desired capacity is supported in an upright position on a plurality of legs 12 from the floor or other support.
  • Unsaturated oil to be hydrogenated in the process is supplied to the vessel through an inlet supply line 14 having a control valve 16 therein.
  • Catalyst is generally premixed with a portion of the oil before delivery to the reaction vessel but it may be added separately through a port 42.
  • the hydrogenated oil is pumped out of the vessel 10 via an outlet line 18 and motor driven pump 20.
  • a suitable control valve 22 is provided in the vessel outlet line 18 and a pump dischargeline 24 is provided to pass the oil to a lter system (not shown) for removing the catalyst from the product.
  • Hydrogen gas for the hydrogenation process is supplied from a source (not shown) through a supply line 26 having a control valve 28 and a pressure regulator valve 30 therein.
  • the hydrogen is introduced into the batch of oil in the vessel 10 well below the surface thereof through a sparger apparatus 32 which is mounted at the lower end of an agitator shaft 34.
  • the rotating shaft carries a plurality of paddles 36 for agitating and circulating the oil.
  • the hydrogen supply line 216 is connected to a sparger sleeve 35 around the shaft, and the hydrogen gas is directed downwardly from the sleeve and outwardly by the sparger into the oil.
  • the agitator is driven lby an electric motor 37 and gear reducer 38 mounted on top of the tank and coupled to the agitator shaft by a detachable coupling 40.
  • the reaction vessel 10 includes a vent line 44 with a valve 46 therein for removal of unwanted gases from the head space in the vessel above the level of the oil.
  • a heat exchanger coil 48 is mounted in the lower portion of the vessel 10 generally below the normal upper surface level of a batch volume of oil to be treated.
  • the upper end of the coil 48 is connected to a steam supply line 50 having a control valve 52 therein for admitting steam into the coil during the initial phase of operation to heat the oil prior to the introduction of hydrogen.
  • Coil 48 is connected via a T to a vapor line 54 having a control valve 56 therein, and the vapor line is connected to one end of an entrainment separator 58 (shown schematically).
  • the lower end of the heat exchanger coil 48 is connected to a discharge line 60 having a valve 62 and a steam trap 64 therein to discharge condensate during the heating step.
  • Condensate or coolant liquid is supplied to the lower end of the heat exchanger coil 48 through a liquid supply line 66. Any liquid entrained in the vapor is removed in the entrainment separator 58 and is directed into the line 66 through a drain line 68 and a T 70.
  • the separator drain line 68 is provided with a sight gauge 72 for indicating the level of liquid in the heat exchanger coil 48.
  • the vapor After removal of entrained liquid from the vapor in the entrainment separator 58, the vapor 'passes out through a vapor line 74 into the shell 75 of a condenser 76.
  • condenser 76 includes a pressurized outer shell 75 with a head chamber 78 at one end. Cooling water is introduced into the lower half of the head chamber through inlet line 80, and leaves the condenser from the upper half of the head chamber 78 through an outlet line 82. The cooling water passes from the lower half of the head chamber 78 through a bundle of heat exchanger tubes 84 in the shell which may be of the U-tube type as shown. The vapor entering the upper portion of the condenser shell passes over the U-tubes to condense and collect as shown. The How of cooling water through the U-tu-bes is adequate to maintain a flooded condition in the condenser shell when desired.
  • Condensate may be recirculated back to the liquid supply line 66 through a condensate drain line 86.
  • a condenser level sight gauge 88 is provided between the vapor line 74 and the condensate line 86 to indicate the height of condensate liquid in the condenser.
  • condensate is removed from the condenser shell 75 and the liquid is introduced into the lower end of the heat exchanger coil 48 from the liquid supply line 66.
  • the ilow rate of condensate is controlled lby a temperature controlled regulator valve 90.
  • the valve 90 is actuated in response to a temperature sensing device 92 in the vessel 10 and the device 92 is directly responsive to the temperature of the oil in the vessel.
  • the valve opens and closes to drain more or less condensate from the condenser 76 in response to temperature variations as sensed by the temperature probe 92.
  • the temperature sensitive probe 92 sends a signal to the temperature controlled regulator valve 90 causing the valve to move toward a more open position, thereby increasing the ow rate of condensate from the condenser 76.
  • the temperature of the oil in the vessel start to drop below the selected level.
  • the regulator valve 90 thus exposes more or less coil surface of the condenser 76 by controlling the flow rate of condensate therefrom. This in turn varies the pressure in the closed system and controls the amount of coolant being evaporated in the coil 48 and passing out through the line 54 in vapor form.
  • the coil 48 in the hydrogenation vessel 10 serves in effect as an internal coolant reservoir from which coolant is vaporized as the valve 90 meters the condensate from the condenser.
  • a batch of soybean oil with catalyst is introduced into the vessel 10 through the inlet supply line 14.
  • the valves 56 and 67 are closed and the valve 52 is opened to admit steam at p.s.i.g. into the upper end of the heat exchanger coil 48 from the line 50.
  • Condensate valve 62 is opened and the steam heats the oil to about 300 F., at which time the condensate valve 62 is closed.
  • the steam now condenses in the coil and the condensate level in the coil is permitted to rise until the coil 48 is about 50% or 75% full.
  • valve 52 is closed, vapor valve 56 and condensate valve 67 are opened. Hydrogen is introduced at 5 p.s.i.g.
  • control regulator valve 90 begins to open and drain condensate from the condenser 76 into the lower end of the heat exchanger coil 48.
  • make up water is not required because sufcient coolant iluid is provided by condensate from the steam used for initially heating up the oil and, accordingly, the valve 97 is generally closed. As heat is generated by the hydrogenation process, it is absorbed by vaporization of the coolant in the coil 48.
  • Heat generated by the chemical reaction taking place in the vessel is removed at a controlled rate by vapor izing the coolant fluid in the coil 48 to maintain a desired oil temperature. This heat is then removed from the recirculation system in the condenser 76 by exposed tubes carrying the condenser coolant water.
  • the temperature controlled regulator valve 90 regulates the flow rate of condensate from the condenser 76 in a precisely controlled amount to exactly expose suicient condenser tube area to balance the amount of heat generated by the exothermic reaction of the hydrogenation process.
  • the pressure in the coil and condenser and other portions of the system can be above or below atmospheric and, accordingly, the varporizing temperature of the coolant vaporizing in the coil 48 is not fixed as in atmospherically vented systems but varies with the pressure. If the desired hydrogenation or reaction temperature is to be 350 F., for example, the present invention, using the closed condensation cooling system, can be set up to control and maintain this temperature within plus or minus 3 F., even though water is the coolant used. When hydrogenation is complete, the batch of oil is cooled to a much lower filtering temperature, such as 180 F.
  • the temperature regulating valve 92 is set to a lower control point which causes the valve to go completely open and drain all the condensate from the condenser 76, thus exposing all of the condenser surface. This causes the condensing system pressure to decrease until it nearly corresponds to the cooling water temperature.
  • the pressure in the condensing system is about 1 p.s.i. absolute. It is to be understood, of course, that other types of heat exchange media can be used and that the invention is not limited to the use of water.
  • the coolant uid can be maintained at an operating temperature range much closer to the desired oil temperature than hereto possible so that when desired heat may be removed from the oil without substantially changing its temperature. Moreover, violent ash-ol and resulting vibration and hammering in the heat exchanger coil are eliminated. Precise control over the operating temperature is achieved and a high degree of controlled repeatability is possible with the method and apparatus of the present invention.
  • the heat exchanger coil 48 may be replaced or supplemented by a jacket on the vessel 10.
  • vapor transferred from the heat exchanger coil 48 to the condenser 76 may contain so little liquid that the entrainment separator 58, may be unnecessary.
  • Condensers other than the U-tube type may suitably be employed.
  • a method of batch hydrogenation of unsaturated oil according to a time-temperature schedule comprising the steps of heating the oil by condensing a heat exchange medium under pressure to provide a body of liquid medium in thermal communication with said oil, introducing hydrogen into the heated oil to establish an exothermic hydrogenation reaction, reducing the pressure over said medium to vaporize a portion of said medium and thereby adjust the temperature to the value scheduled for the hydrogenating oil and, subsequently, further reducing the pressure over said liquid medium to cool the oil to a filtering temperature.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Organic Chemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • Physical Or Chemical Processes And Apparatus (AREA)
  • Fats And Perfumes (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
US00026509A 1970-04-08 1970-04-08 Hydrogenation of oils Expired - Lifetime US3732266A (en)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US2650970A 1970-04-08 1970-04-08

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US00026509A Expired - Lifetime US3732266A (en) 1970-04-08 1970-04-08 Hydrogenation of oils

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US (1) US3732266A (enrdf_load_stackoverflow)
JP (1) JPS524561B1 (enrdf_load_stackoverflow)
BR (1) BR7102052D0 (enrdf_load_stackoverflow)
CA (1) CA1008463A (enrdf_load_stackoverflow)
DE (1) DE2116894C3 (enrdf_load_stackoverflow)
ES (1) ES389980A1 (enrdf_load_stackoverflow)
FR (1) FR2089414A5 (enrdf_load_stackoverflow)
GB (1) GB1349528A (enrdf_load_stackoverflow)
NL (1) NL171173B (enrdf_load_stackoverflow)
SE (1) SE369528B (enrdf_load_stackoverflow)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4119670A (en) * 1976-07-15 1978-10-10 Nippon Shokubai Kagaku Kogyo Co., Ltd Process and reactor for preparing ethanolamines
US5360920A (en) * 1992-08-07 1994-11-01 The Procter & Gamble Company Hydrogenation in a plate heat exchanger
WO2001078890A3 (en) * 2000-04-13 2002-02-07 Jose P Arencibia Jr Temperature controlled reaction vessel
EP1508367A1 (de) * 2003-08-22 2005-02-23 Maschinenbau Scholz GmbH & Co. KG Vorrichtung zur Temperaturregelung des Innenraums von Druckgefässen
US6955793B1 (en) 1997-06-18 2005-10-18 Arencibia Jr Jose P Temperature controlled reaction vessel
US20140137614A1 (en) * 2009-12-30 2014-05-22 Vitag Corporation Bioorganically-Augmented HighValue Fertilizer
CN104826567A (zh) * 2015-05-07 2015-08-12 中石化南京工程有限公司 一种环己酮生产铂催化加氢热能用于脱氢工艺的装置
CN104826565A (zh) * 2015-03-31 2015-08-12 山东胜星化工有限公司 加氢反应中的防铵盐结晶装置
CN107937129A (zh) * 2017-11-15 2018-04-20 广汉市航佳食品有限公司 一种食用动物油脂精炼过程中的控温系统及工艺

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4119670A (en) * 1976-07-15 1978-10-10 Nippon Shokubai Kagaku Kogyo Co., Ltd Process and reactor for preparing ethanolamines
US5360920A (en) * 1992-08-07 1994-11-01 The Procter & Gamble Company Hydrogenation in a plate heat exchanger
US6955793B1 (en) 1997-06-18 2005-10-18 Arencibia Jr Jose P Temperature controlled reaction vessel
US20060013749A1 (en) * 1997-06-18 2006-01-19 Arencibia Jose P Jr Temperature controlled reaction vessel
US7645428B2 (en) 1997-06-18 2010-01-12 Arencibia Jr Jose P Temperature controlled reaction vessel
WO2001078890A3 (en) * 2000-04-13 2002-02-07 Jose P Arencibia Jr Temperature controlled reaction vessel
EP1508367A1 (de) * 2003-08-22 2005-02-23 Maschinenbau Scholz GmbH & Co. KG Vorrichtung zur Temperaturregelung des Innenraums von Druckgefässen
US8920733B2 (en) * 2009-12-30 2014-12-30 Vitag Corporation Bioorganically-augmented high value fertilizer
US20140137614A1 (en) * 2009-12-30 2014-05-22 Vitag Corporation Bioorganically-Augmented HighValue Fertilizer
US9328030B2 (en) 2009-12-30 2016-05-03 Anuvia Plant Nutrients Corporation Bioorganically-augmented high value fertilizer
US9586869B1 (en) 2009-12-30 2017-03-07 Anuvia Plant Nutrients Corporation Bioorganically-augmented high value fertilizer
CN104826565A (zh) * 2015-03-31 2015-08-12 山东胜星化工有限公司 加氢反应中的防铵盐结晶装置
CN104826567A (zh) * 2015-05-07 2015-08-12 中石化南京工程有限公司 一种环己酮生产铂催化加氢热能用于脱氢工艺的装置
CN104826567B (zh) * 2015-05-07 2016-06-15 中石化南京工程有限公司 一种环己酮生产铂催化加氢热能用于脱氢工艺的装置
CN107937129A (zh) * 2017-11-15 2018-04-20 广汉市航佳食品有限公司 一种食用动物油脂精炼过程中的控温系统及工艺
CN107937129B (zh) * 2017-11-15 2021-03-23 四川航佳生物科技有限公司 一种食用动物油脂精炼过程中的控温系统及工艺

Also Published As

Publication number Publication date
CA1008463A (en) 1977-04-12
NL7104653A (enrdf_load_stackoverflow) 1971-10-12
BR7102052D0 (pt) 1973-04-10
GB1349528A (en) 1974-04-03
DE2116894C3 (de) 1980-05-22
DE2116894A1 (de) 1971-10-21
SE369528B (enrdf_load_stackoverflow) 1974-09-02
NL171173B (nl) 1982-09-16
DE2116894B2 (enrdf_load_stackoverflow) 1979-09-06
FR2089414A5 (enrdf_load_stackoverflow) 1972-01-07
JPS524561B1 (enrdf_load_stackoverflow) 1977-02-04
ES389980A1 (es) 1973-06-16

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Owner name: CHEMETRON PROCESS EQUIPMENT, INC.

Free format text: CHANGE OF NAME;ASSIGNOR:CHEMETRON-PROCESS EQUIPMENT, INC.,;REEL/FRAME:003873/0520

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Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:CHEMETRON PROCESS EQUIPMENT, INC. A DE CORP.;REEL/FRAME:004188/0073

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