WO2010101454A2 - Procédé d'extraction d'huile de palme par évaporation - Google Patents

Procédé d'extraction d'huile de palme par évaporation Download PDF

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Publication number
WO2010101454A2
WO2010101454A2 PCT/MY2010/000029 MY2010000029W WO2010101454A2 WO 2010101454 A2 WO2010101454 A2 WO 2010101454A2 MY 2010000029 W MY2010000029 W MY 2010000029W WO 2010101454 A2 WO2010101454 A2 WO 2010101454A2
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WO
WIPO (PCT)
Prior art keywords
oil
phase
process according
sludge
liquor
Prior art date
Application number
PCT/MY2010/000029
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English (en)
Other versions
WO2010101454A3 (fr
Inventor
Sivasothy Kandiah
Ramachandran Batumalai
Original Assignee
Malaysian Palm Oil Board
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 Malaysian Palm Oil Board filed Critical Malaysian Palm Oil Board
Priority to BRPI1005939A priority Critical patent/BRPI1005939A2/pt
Publication of WO2010101454A2 publication Critical patent/WO2010101454A2/fr
Publication of WO2010101454A3 publication Critical patent/WO2010101454A3/fr

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B1/00—Production of fats or fatty oils from raw materials

Definitions

  • the present invention relates to a process for extracting palm oil from oil palm fresh fruit bunches and more particularly to a process for extracting palm oil from a liquor, consisting of a mixture of oil, water and solids originating from prior processing steps in the palm oil extraction process.
  • Fresh fruit bunches (FFB) 1 are cooked during sterilization 2 using steam at a pressure of 3 bar in horizontal autoclaves of cylindrical shape for about 60 to 90 minutes and then, as sterilized fruit bunches 3, stripped 4 to separate the sterilized fruits from the empty fruit bunches.
  • the sterilized fruits 5 are then reheated and agitated in steam-heated vessels known as digesters 6 to loosen the mesocarp from the nuts in preparation for pressing 7.
  • the screw press expels a liquor of oil, water and finely divided solids, and a press cake of fibre and nuts.
  • the oil in the press liquor has to be separated from the water and solids and this takes place during clarification.
  • the primary separation is achieved in settling tanks using gravity.
  • the diluted press liquor is then screened 9 to remove the coarse fibrous solids 20 that are subsequently returned to the digesters 6.
  • the screened and diluted press liquor 10 is then heated and pumped into the clarification tank 11 where it separates into two phases, i.e. oil 12 and sludge 16.
  • the oil layer 12 in the clarification tank is skimmed off and passed to centrifugal purifier 13 which reduces the dirt content to 0.01 percent or less.
  • the centrifuged oil is then dried in vacuum drier 14 to give a product of crude palm oil 15 with a moisture content of approximately 0.1 percent.
  • Sludge 16 from the clarification tank has approximately 4 to 10 percent oil, the bulk of which can be recovered using centrifugal separator 18 after desander 17 leaving substantially de-oiled sludge 19.
  • the oil recovered by the sludge centrifuge 18 contains some water and dirt and is therefore returned to the clarification tank 11 for further treatment.
  • the process generates about 0.6 tons of palm oil mill effluent (POME) for every ton of FFB processed. It is widely acknowledged that a more effective method of treating the POME than the widely used anaerobic/aerobic ponding system is needed.
  • One solution to the problem is to modify processes in the mill to achieve significant reduction in the amount of POME, making it viable to treat the POME using approaches that were previously considered to be not technically and/ or economically viable.
  • Two-phase decanters have primarily been used in palm oil mills for separating out the suspended solids, which may subsequently be dried using a rotary drier. It is claimed that up to 70 percent of the suspended solids and 20 percent of the dissolved solids can be separated by the decanter. Installing them prior to oil clarification leads to reduction in the amount of water needed to facilitate oil clarification. Nevertheless, they are normally used for treating the underflow from the clarification tank since this leads to lower oil loss in the cake. No significant reduction in the amount of POME is achievable in the latter case, since water is still needed to facilitate oil settling in the clarification tank.
  • three-phase decanter makes possible oil clarification and separation of the suspended solids concurrently. If press liquor is used as the feed to a three-phase decanter, it is possible to replace both the clarification tank and the sludge centrifuge. This not only reduces the amount of water needed to facilitate oil clarification significantly, but also greatly simplifies the clarification process. Nevertheless, the oil loss was observed to be higher than with the conventional process.
  • three-phase decanters are normally used in large capacity mills, with or without sludge separators, for treating the underflow from the clarification tank. As in the case of two-phase decanters, no significant reduction in the amount of POME is achievable since primary oil/ sludge separation using clarification tanks is still needed.
  • the resulting liquor 155 with reduced moisture from evaporation means 154 is subsequently fed to oil/ sludge separation means 156 for clarification using a zero- dilution clarification process to generate an oil phase 157 and a sludge phase 161.
  • the oil phase 157 is further processed using purification means 158 to remove traces of dirt therein to form a purified oil phase 158a that is subsequently dried using drying means 159 to obtain crude palm oil 160.
  • the sludge phase 161 contains oil that is recoverable, it is further treated using oil recovery means 162 before it is discharged as effluent sludge 164.
  • the oil 163 recovered by oil recovery means 162 will most likely be contaminated with water and solids and is recycled back to oil/ sludge separation means 156 for further processing.
  • the moisture content of the oil/ sludge discharge phase is reduced to form a concentrated liquor that consists of a mixture of oil and a concentrated sludge that contains dissolved solids and fine suspended solids; and (c) the concentrated liquor is clarified using oil/sludge separation means to produce a concentrated sludge phase and an oil phase for further processing to extract the palm oil therein.
  • Evaporation of moisture from the oil/sludge discharge phase in step (b) hereinbefore of the present invention provides a number of advantages compared to evaporation of moisture from POME as proposed in a prior art process.
  • the presence of a significant quantity of oil in the feed to the evaporation means ensures that the evaporated liquor does not become viscous. If the evaporation means used is a falling film evaporator, fouling of evaporator tubes will be significantly reduced, even if a large percentage of the moisture in the oil/ sludge mixture is removed.
  • the quantity of moisture to be removed by evaporation from the oil/ sludge mixture is significantly less than the quantity of moisture to be removed from raw POME in a conventional mill.
  • the use of a multiple-effect evaporator system makes possible the removal of moisture using a fraction of the energy required by a drier to remove an equal amount of moisture from POME, especially if heated air is used to supply the energy for drying.
  • the significant energy savings can be explained by using the following example. If we consider the heat balance of a single-effect evaporator, we find that the heat content (enthalpy) of the evaporated vapour is approximately equal to the heat input on the heating side. About 1 kg/hr of vapour will be produced by 1 kg/hr of live steam, as the specific evaporation heat values on the heating and product sides are about the same. If the vapour produced is used as heating steam in a second effect, the energy consumption of the overall system is reduced by 50 percent. This principle can be continued over further effects to save even more energy. The theoretical steam consumption of a triple-effect evaporator system is therefore one-third of the steam consumption of a single-effect evaporator system for an equivalent evaporation load.
  • Figure 1 illustrates schematically the conventional palm oil extraction process using oil palm fresh fruit bunches as the feed.
  • Figure 2 illustrates schematically the prior art process for extracting palm oil using evaporation disclosed in Malaysian Patent Application No. PI20071265.
  • Figure 3 illustrates schematically one preferred embodiment of the present invention based on the use of a two-phase separation means for removing suspended solids from the feed to the evaporation means.
  • Figure 4 illustrates schematically one preferred embodiment of the present invention based on the use of a two-phase separation means for removing suspended solids from the feed to the evaporation means and incorporating a step of gravitational settling prior to suspended solids removal.
  • Figure 5 illustrates schematically another preferred embodiment of the present invention based on the use of a three-phase separation means for removing suspended solids from the feed to the evaporation means.
  • Figure 6 illustrates schematically another preferred embodiment of the present invention based on the use of a two-phase separation means for removing suspended solids from the feed to the evaporation means and the use of a second oil/sludge separation means to recover oil still remaining in the concentrated sludge phase from the first oil/ sludge separation means.
  • Figure 7 illustrates schematically another preferred embodiment of the present invention based on the use of a two-phase separation means for removing suspended solids from the feed to the evaporation means and the use of a second oil/sludge separation means to recover oil still remaining in the concentrated sludge phase from the first oil/ sludge separation means and incorporating a step of gravitational settling prior to suspended solids removal.
  • Figure 8 illustrates schematically another preferred embodiment of the present invention based on the use of a three-phase separation means for removing suspended solids from the feed to the evaporation means and the use of a second oil/sludge separation means to recover oil still remaining in the concentrated sludge phase from the first oil/ sludge separation means.
  • the original feed liquor 51 emanating from prior processing steps used for extracting palm oil from FFB consists of a mixture of oil, water, coarse and fine fibrous solids, dissolved solids and particles of sand. It is first fed to screening means 52 as illustrated to remove the coarse fibrous solids 52a that may subsequently be recycled. The screened liquor is then heated to approximately 95°C and fed to desanding means 53, such as a cyclone desanding system, to remove the sand 53a in order to generate a feed liquor 53b for further processing.
  • desanding means 53 such as a cyclone desanding system
  • the feed liquor 53b may advantageously be a mixture comprising the liquor drained from digesters and the liquor expelled from presses, or even a mixture comprising the liquor drained from digesters, the liquor expelled from presses and all or a portion of the condensate discharged from the sterilization process.
  • Figures 3 and 6 illustrate schematically one mode for carrying out the invention based on the use of a two-phase separation means as the separation means 54 for removing a significant portion of the suspended solids from the feed liquor 53b.
  • the feed liquor 53b is fed to a two-phase separation means which generates two phases.
  • One phase is a cake 54a containing most of the suspended solids from the feed liquor 53b and having a moisture content of less than 80%.
  • the other phase for further processing is an oil/ sludge discharge phase 54b which consists of a mixture of oil and a sludge containing soluble solids and fine suspended solids.
  • the separation can be achieved without prior water addition by centrifugation using a two-phase decanter, or by filtration using a rotary press, a membrane filter press, a belt press or other equipment that can be used to achieve a similar objective. Naturally, the separation can also be achieved with prior water addition.
  • the oil/ sludge discharge phase 54b from separation means 54 is then fed to evaporation means 55.
  • the evaporation means 55 is used to reduce the moisture content of the oil/sludge discharge phase 54b from separation means 54, generating water 55a and a concentrated liquor 55b for further processing that consists of a mixture of oil and a concentrated sludge that contains dissolved solids and fine suspended solids.
  • a multiple-effect falling film evaporator is advantageously used as this evaporator has high heat transfer coefficients and can operate at small driving forces, and is less susceptible to scaling. It also permits very short product contact times, typically just a few seconds per pass.
  • a multiple-effect forced circulation evaporator may also be used for this purpose.
  • the removal of a significant portion of the suspended solids from the feed liquor 53b using separation means 54 to form the oil/ sludge discharge phase 54b for the subsequent feeding to the evaporator will reduce its viscosity and minimize fouling of the evaporator tubes.
  • the concentrated liquor 55b is reheated to approximately 95°C and then fed to oil/sludge separation means 56.
  • the oil/ sludge separation means 56 separates the oil from the concentrated sludge in the concentrated liquor 55b to generate a concentrated sludge phase 56a and an oil phase 56b.
  • This separation can be achieved using a simple settling tank, a coalescence plate separator, a centrifuge, a filter or a combination thereof operating in series.
  • the oil phase 56b from oil/ sludge separation means 56 will still contain some moisture and dirt and will therefore require further treatment to extract the palm oil therein.
  • the further treatment consists of purifying the oil phase 56b using purification means 57 to remove the dirt 57a therein to generate a purified oil phase 57b which is then dried using drying means 58 to remove the water 58a therein to generate palm oil 59.
  • FIGs 4 and 7 illustrate schematically another mode for carrying out the invention based on the use of a two-phase separation means as the separation means 54.
  • the feed liquor 53b is subjected to gravitational settling in a settling tank 53x prior to being fed to the two-phase separation means.
  • the feed liquor 53b in the settling tank 53x separates into an oil phase 53y and an underflow 53z consisting of a mixture of oil and sludge.
  • the oil/ sludge discharge phase 53z is fed to the two-phase separation means for further processing as described earlier.
  • the oil phase 53y is mixed with the oil phase 56b originating from the oil/ sludge separation means 56 to form a mixture 56c.
  • This mixture 56c is then subjected to further processing steps to extract the palm oil 59 therein.
  • FIGS 5 and 8 illustrate schematically yet another mode for carrying out the invention based on the use of a three-phase separation means as the separation means 54 for removing a significant portion of the suspended solids from the feed liquor 53b.
  • the feed liquor 53b is fed to a three-phase separation means which generates a cake 54a containing most of the suspended solids, an oil/ sludge discharge phase 54b for further processing as described earlier, and an oil phase 54c containing traces of dirt and moisture.
  • This oil phase 54c is advantageously mixed with the oil phase 56b originating from the oil/ sludge separation means 56 to form a mixture 56c and this mixture is then subjected to further processing steps to extract the palm oil therein.
  • the separation means 54 is advantageously a centrifuge capable of three-phase separation such as a three-phase decanter.
  • the residual oil in the concentrated sludge phase 56a is recovered using residual oil recovery means 60 to form sludge 61 and a recovered oil/ sludge discharge phase 60a.
  • the residual oil recovery means 60 is a centrifuge.
  • the recovered oil/ sludge discharge phase 60a is recycled back to the oil/sludge separation means 56.
  • the oil phase 56b is discharged into a holding tank, where settling may take place to reduce its moisture and dirt content.
  • the holding tank is heated to approximately 85°C. If settling is permitted, the bottom layer in the holding tank is continuously or intermittendy recycled.
  • the oil phase 56b is then further processed using purification means 57 to remove traces of dirt 57a in the oil to form a purified oil phase 57b that is subsequently dried using drying means 58 to obtain palm oil 59.
  • the oil phase 56b may be directly subjected to drying using drying means 58 to obtain palm oil 59 without first being purified to remove traces of dirt in the oil.
  • the present invention finds ready industrial applicability in the palm oil industry as it is a novel process for extracting palm oil using evaporation technique to reduce the moisture content in the oil/ sludge discharge phase after separation. This process provides a number of advantages compared to the conventional process.

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  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • Organic Chemistry (AREA)
  • Fats And Perfumes (AREA)
  • Vaporization, Distillation, Condensation, Sublimation, And Cold Traps (AREA)

Abstract

L'invention porte sur un procédé d'extraction d'huile de palme à partir de grappes de fruit frais de palmier à huile. Le procédé met en jeu l'extraction d'huile de palme à partir d'une liqueur d'alimentation (53b) consistant en un mélange d'huile, d'eau et de matières solides provenant d'étapes de traitement préalables du procédé d'extraction d'huile de palme. Dans l'étape initiale du procédé, une fraction significative des solides en suspension dans la liqueur d'alimentation (53b) est retirée à l'aide de moyens de séparation (54) pour générer une phase de décharge huile/boue (54b) qui consiste en un mélange d'huile et d'une boue qui contient des matières solides dissoutes et de fines matières solides en suspension. Dans la seconde étape du procédé, la teneur en humidité de la phase de décharge huile/boue (54b) est réduite par évaporation pour former une liqueur concentrée (55b) qui consiste en un mélange d'huile et d'une boue concentrée qui contient des matières solides dissoutes et de fines matières solides en suspension. Dans l'étape ultérieure du procédé, la liqueur concentrée (55b) est clarifiée à l'aide de moyens de séparation d'huile/boue (56) pour produire une phase de boue concentrée (56a) et une phase d'huile (56b) pour un nouveau traitement pour extraire l'huile de palme qui y est contenue.
PCT/MY2010/000029 2009-03-04 2010-03-04 Procédé d'extraction d'huile de palme par évaporation WO2010101454A2 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
BRPI1005939A BRPI1005939A2 (pt) 2009-03-04 2010-03-04 processo de extração de óleo de palma ultilizando evaporação

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
MYPI20090863 MY143787A (en) 2009-03-04 2009-03-04 Process for extracting palm oil using evaporation
MYPI20090863 2009-03-04

Publications (2)

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WO2010101454A2 true WO2010101454A2 (fr) 2010-09-10
WO2010101454A3 WO2010101454A3 (fr) 2010-12-09

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BR (1) BRPI1005939A2 (fr)
CO (1) CO6501163A2 (fr)
MY (1) MY143787A (fr)
WO (1) WO2010101454A2 (fr)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012096561A2 (fr) * 2011-01-10 2012-07-19 Low Teck Yin Procédé d'extraction d'huile de palme
WO2014035760A1 (fr) * 2012-08-29 2014-03-06 Desmet Ballestra North America, Inc. Extraction par solvant de fibrse de palme pressées
WO2015037980A1 (fr) * 2013-09-10 2015-03-19 Malaysian Palm Oil Board Procédé de clarification d'huile de palme à zéro décharge liquide
WO2015190907A1 (fr) * 2014-06-10 2015-12-17 Palmite Process Engineering Sdn Bhd Procédé d'extraction d'huile de palme brute au moyen d'une technologie verte
WO2016129986A3 (fr) * 2015-02-10 2016-12-01 Ngan Teng Ye Procédé de traitement des effluents produits par le processus d'extraction de l'huile de palme
CN108133106A (zh) * 2017-12-21 2018-06-08 山东诺德能源科技有限公司 一种根据加水量预估烧结机混合料的水分含量的方法
KR101936823B1 (ko) * 2015-11-09 2019-01-09 한국생산기술연구원 팜유래 액상부산물에서 회수된 연료를 이용한 발전시스템
CN109499080A (zh) * 2018-10-31 2019-03-22 浙江本优机械有限公司 一种用于氯化钙生产的蒸发设备

Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5039455A (en) * 1989-07-31 1991-08-13 Kooi Boon Lam Process for continuous extraction of palm oil or vegetable edible oil
EP0718397A2 (fr) * 1994-09-13 1996-06-26 Tratamiento Integral De Alpechines Baena, S.L. Procédé pour la purification et développement d'un produit de déchet liquide et solide provenant d'installations d'huilerie
WO2007038963A1 (fr) * 2005-10-05 2007-04-12 Flottweg Gmbh & Co. Kgaa Processus et dispositif destinés à produire de l'huile de palme ou de l'huile végétale
WO2009017389A2 (fr) * 2007-08-01 2009-02-05 Malaysian Palm Oil Board Procédé d'extraction d'huile de palme brute

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5039455A (en) * 1989-07-31 1991-08-13 Kooi Boon Lam Process for continuous extraction of palm oil or vegetable edible oil
EP0718397A2 (fr) * 1994-09-13 1996-06-26 Tratamiento Integral De Alpechines Baena, S.L. Procédé pour la purification et développement d'un produit de déchet liquide et solide provenant d'installations d'huilerie
WO2007038963A1 (fr) * 2005-10-05 2007-04-12 Flottweg Gmbh & Co. Kgaa Processus et dispositif destinés à produire de l'huile de palme ou de l'huile végétale
WO2009017389A2 (fr) * 2007-08-01 2009-02-05 Malaysian Palm Oil Board Procédé d'extraction d'huile de palme brute

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2012096561A2 (fr) * 2011-01-10 2012-07-19 Low Teck Yin Procédé d'extraction d'huile de palme
WO2012096561A3 (fr) * 2011-01-10 2012-11-29 Low Teck Yin Procédé d'extraction d'huile de palme
WO2014035760A1 (fr) * 2012-08-29 2014-03-06 Desmet Ballestra North America, Inc. Extraction par solvant de fibrse de palme pressées
WO2015037980A1 (fr) * 2013-09-10 2015-03-19 Malaysian Palm Oil Board Procédé de clarification d'huile de palme à zéro décharge liquide
WO2015190907A1 (fr) * 2014-06-10 2015-12-17 Palmite Process Engineering Sdn Bhd Procédé d'extraction d'huile de palme brute au moyen d'une technologie verte
WO2016129986A3 (fr) * 2015-02-10 2016-12-01 Ngan Teng Ye Procédé de traitement des effluents produits par le processus d'extraction de l'huile de palme
KR101936823B1 (ko) * 2015-11-09 2019-01-09 한국생산기술연구원 팜유래 액상부산물에서 회수된 연료를 이용한 발전시스템
CN108133106A (zh) * 2017-12-21 2018-06-08 山东诺德能源科技有限公司 一种根据加水量预估烧结机混合料的水分含量的方法
CN109499080A (zh) * 2018-10-31 2019-03-22 浙江本优机械有限公司 一种用于氯化钙生产的蒸发设备

Also Published As

Publication number Publication date
CO6501163A2 (es) 2012-08-15
WO2010101454A3 (fr) 2010-12-09
MY143787A (en) 2011-07-07
BRPI1005939A2 (pt) 2016-02-10

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