WO2009025542A1 - Procédé amélioré de raffinage d'huile végétale et de graisses animales pour matières premières utilisées dans la production de biodiesel - Google Patents

Procédé amélioré de raffinage d'huile végétale et de graisses animales pour matières premières utilisées dans la production de biodiesel Download PDF

Info

Publication number
WO2009025542A1
WO2009025542A1 PCT/MY2008/000014 MY2008000014W WO2009025542A1 WO 2009025542 A1 WO2009025542 A1 WO 2009025542A1 MY 2008000014 W MY2008000014 W MY 2008000014W WO 2009025542 A1 WO2009025542 A1 WO 2009025542A1
Authority
WO
WIPO (PCT)
Prior art keywords
oil
crude
heating
ffa
thermopack
Prior art date
Application number
PCT/MY2008/000014
Other languages
English (en)
Inventor
Ruslee Hussain
Original Assignee
Ruslee Hussain
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 Ruslee Hussain filed Critical Ruslee Hussain
Priority to PCT/MY2008/000014 priority Critical patent/WO2009025542A1/fr
Publication of WO2009025542A1 publication Critical patent/WO2009025542A1/fr

Links

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
    • C11B3/00—Refining fats or fatty oils
    • C11B3/12—Refining fats or fatty oils by distillation

Definitions

  • the present invention relates generally to the refining of crude vegetable oil or animal fats for biodiesel feedstock for a common and popular and generally economical biodiesel transesterification process,
  • this invention relates to a method for the economical process of refining crude vegetable oil or animal fats via a modified continuous known chemical refining in combination with a modified continuous known physical refining by utilising the free fatty acid(FFA) byproduct as a clean and renewable fuel for the thermopack heater and the refined oil from the invented refining process as the heat transfer oil directly in the thermopack heater heating coils and heating lines.
  • the invention uses only a FFA fired thermopack heater without the need for any steam boiler for the total heating requirement of the refining process.
  • the use of petroleum based fuel and petroleum based heat transfer oil is totally obviated in the refining process.
  • the invention provides an energy efficient, lower capital cost, space saving, lower operation cost and environmentally safe refining process and thus is an improvement over prior crude vegetable oil or animal fats refining method.
  • a typical vegetable or animal fats refinery uses petroleum fuel as fuel in the steam boilers and thermopack heaters.
  • Petroleum based fuel like diesel and fuel oil are costly and pollute the environment.
  • a steam boiler must be employed as life steam is needed in the steam stripping process and steam ejector for producing vacuum pressure apart from supplying the processing heat requirements.
  • Thermopack heaters are used at the pre-stripping and deoderizing column to supply the necessary high temperature of about 275 Deg. Celcius for steam stripping distillation process.
  • the use of a steam boiler is a high capital investment and operational cost and requires the employment of a certified boiler chargeman by law of almost all countries.
  • a steam boiler requires the feed water to be treated and thus requires a water treatment facility and the use of chemicals to treat the water.
  • the installation of a steam ejector is also another high captital cost which uses quite a substantial amount of steam to operate.
  • a fuel cost for a typical vegetable/fats refinery can amount to as high as 50 percent of the total operational cost of the refinery.
  • Vegetable oil/animal fat is one of the most important primary foods and therefore requires maximum quality for safe human consumption.
  • the quality of the final product depends on the refining method and the nature of the raw oil.
  • a typical r efinery for food production requires the oil to be degummed, deacidified, bleached and deoderized.
  • bleaching and deoderizing process can be omitted as the final product is classified as biofuel and not as food.
  • a typical refinery uses large amount of water for steam generation and a larger water treatment plant is needed to accompany it. As large amount of water is used, the chances of polluting rivers and waterways always happened due to effluent water treatment shutdown and failures.
  • a typical refinery uses large amount of petroleum based fuel for the steam boilers and thermopack heaters. The burning of the fuel will contribute to polluting the environment as large amount of pollutants such as sulfur, NOx , CO and CO2 will be released to the environment.
  • a typical refinery uses mineral based thermal oil or mineral based food grade thermal oil or mineral white oil or mineral based synthetic oil. These thermal oils are regarded as high temperature and high performance and are thus very costly. These thermal oils needs to be replenished and replaced from time to time as the quality and properties will degrade over a short period of time as the thermal oil is subjected to an extreme temperature of up to 350 Deg. Celcius and being exposed to air in the expansion tank of the thermopack system in certain cases. Replenishing the thermal oil requiring the plant to be shutdown and labor to carry out the job. This will also contribute to the running cost of the refinery.
  • the crude vegetable oils/animal fats must be deacidified effectively or completely for a biodiesel feedstock.
  • crude jatropha oil can have an FFA content up to 10 % which can contribute to a large amount of soapstock being produced if the method selected is the chemical refining method alone.
  • the soapstock will then need to be treated using soapstock splitting process to recover the FFA, another costly treatment as strong acids such as hydrochloric acid HCL and or sulfuric acids H2SO4 are normally used which requires the use of expensive extremely durable stainless steel tanks. Soaps of less attractive value will be produced in quite a large amount and hence will pose a problem to manage the storage, handling and sales of it. On top of that, oil loss will be very substantial.
  • the goal of the invention is to produce large amount of refined vegetable oil/animal fats for biodiesel feedstock and not for food production. As such the invention is avoiding the use of the extremely expensive kind of steel used in the refinery plant that is food grade stainless steel 316.
  • the invention uses mostly mild steel and in certain areas stainless steel 304L which is much cheaper and sufficient enough to comply with the stringent safety and design requirement of the invention.
  • a smaller number of energy efficient equipments is used in the invention compared to the traditional method of physical refining. An efficient heat transfer method of cascading the heat using processing tanks heating jackets and heating coils where the heat is directly in contact with the process oil.
  • the object of the invention is to avoid the use of any steam or steam boilers. As such, no large amount of water is required in the invention and water used in the invented method is recycled. ISb water treament plant is needed and the chances of polluting rivers and waterways is completely eliminated.
  • Another object of the invention is to use the by-product from the distillation column called free fatty acid FFA to fuel the thermopack heater.
  • This FFA is cleaner and renewable compared to any fossil fuel.
  • the FFA distilled from the process has a comparable heating value and is more than enough to completely supply all the fuel needed by the thermo-pack heater.
  • the excess FFA can be packed and sold as a renewable and cleaner boiler fuel or as oleo-chemical feedstock.
  • Still yet another object of the invention is to used the processed oil as the thermal oil which avoided the use of any mineral based thermal oil or the need to purchase and replenish the thermal oil. Nb schedule shutdown is needed compared to the conventional method and this will contibute to a substantial cost saving.
  • directly heating the oil to be processed in the thermopack heater is the novel process to achieve a more energy efficient heat transfer.
  • the process oil temperature can be achieved in a shorter period of time compared to the traditional heating a separate thermal oil first to a higher temperature than the process oil as some heat transfer loss occured in the commonly used plate heat exchangers.
  • About 30 Deg. Celcius to 70 Deg. Celcius higher thermal oil operating temperature has to be used in the conventional thermopack heaters which translated to a higher energy requirement thus higher fuel cost.
  • the invented refining process and method can be called a green refinery as the use of petroleum fuel is avoided completely.
  • Nb petroleum fuel needs to be purchased or transported to the refinery.
  • the invented process and method is more energy efficient in that it does not require shutdown as mentioned above which will require a heating start-up to heat the distillation section as heating start-ups consume large amount of fuel.
  • Nb water treatment plant is needed as the water used is recycled.
  • Figure 1 is the invented refining process flow schematic design.
  • Figure 2 is the 2D design(front elevation) of the invented 50 Metric Tonne per day crude vegetable oils/animal fats refining plant.
  • Figure 3 is the isometric view of the plant showing the small foot-print needed(6m x 24m or 20ft x 80ft) for a 50 Metric Tonne per day capacity.
  • This invention is characterized by the fact that the process flow design as depicted in Figure 1 is carried out as follows; About 1 Metric Tonne of refined oil is pumped into the bottom of distillation column(14) from tank(20) using the thermopack pump(15) and about 200 kg of preheated FFA is placed in the FFA flash drum(23). Then circulation is carried out by opening all the necessary valves in the process flow design pipelines (represented by the solid arrows). The vacuum pump(24) and (29) are then be started to remove air in the thermal heating pipelines with a setting of about 5mm to 10mm Hg.
  • thermopack After air has been completely removed in the heating circuit pipelines as indicated by a constant pump pressure of about 3 bar, the thermopack is fired using the preheated FFA from the FFA flash drum(23).
  • the refined oil which act as the thermal heating oil is quickly being heated-up by the thermopack heater to the required distillation temperature of around 270 Deg. C.
  • Tank(l) with a capacity of 50 curie meter and equipped with a 30 square meter of hearting surface heating coils can heat-up a 2 metric ton per hour flow rate of crude oil from 30 Deg. C up to 130 Deg. C while flowing from the top to the bottom of the tank while being agjatated by the tank agitator of speed of about 50 rpm.
  • a variable-speed pump(4) is started to deliver about 2 MT/hour flow rate.
  • Industrial grade phosphoric acid H3PO4 of about 85% purity is dosed from chute(3) via a metering pump(not shown) at about 0.01 % to 0.1% weight depending on the quality of the crude vegetable/animal fats.
  • the mixture is further agitated by the high speed agitator of speed of 2800 rpm at the bottom of the acid mixing tank(5) equipped with heating coils to maintain or regulate the required processing temperature.
  • a small amount of mild liquid caustic soda is dosed from chute(6) via a metering pump(not shown) to neutralise the acids in the process crude oil.
  • the mixtures then enters mild caustic mixing tank(7) to be further agitated by the bottom agitator of speed 2800 rpm. Gums, phosphatides and sludges are continuouly removed from the mixture in centrifugal separator(8) into a container(not shown). Meanwhile the degummed oil travels to the top of the separator where it meets chute(9) where a small of amount of hot water is dosed(if necessary depending on the quality of the crude oil) via a metering p ⁇ imp(not shown) to hydrate any traces of phosphatides remaining in the crude oil. The degummed oil and hot water mixtures then travel to the hot water mixing tank(7) to be agitated by the bottom mixer to 2800 rpm.
  • the required process temperature is achieved by controlling the tank heating coils temperature.
  • the agitated mixtures then travel to a centrifugal purifier(ll) where the degummed oil is separated from the water, hydrated phosphatides and sludge.
  • the separated impurities can be recycled(recycle line not shown) to the separator(8) in order to further minimize oil loss.
  • Most of the other impurities like sludge can be collected from the bottom of the purifier into a container(not shown).
  • the slightly less than 2 MT/hour crude degummed oil then enters the bottom of the two-stages dearation column(12) with a temperature in the region of 110 Deg. C to 150 Deg. C.
  • the heated processed oil then enters the first stage of the FFA distillation column(14) where FFA will be vaporised and pulled by the vacuum pump(24) into the FFA flash drum(23) via pipe(21) and condenser(22).
  • the degummed and deacidified oil then drops into the second stage of the FFA distillation column and then later to the third stage of the distillation column.
  • the refined oil at the bottom of the distillation column(14) now enters the thermopack heater(16) via a variable-speed pump(15) and functions as a thermal oil fluid to supply all the necessary heating process requirements of the refinery.
  • the thermopack heater temperature contoller is used to regulate and control the highest temperature requirement of the process.
  • the heated processed oil then travels to the heating jacket of the first stage dearation column(12) and then into the first stage heating jacket of the FFA distillation column(14), then to the second stage heating jacket of the distillation column(14), then to the third stage heating jacket of the distillation column(14), then into the heating jacket of the bottom of the distillation column(14). Once the heating jacket of the bottom of the distillation column is full, the refined heating oil will then travel to the second stage heating jacket of the dearation coulmn(12) before entering the bottom jacket of the dearation column(12).
  • the flow rate and pump pressure of the refined heating oil is supplied and controlled by the variable-speed thermopack heater pump(15) which then now pumps the refined heating oil out of the heating jacket of the bottom of dearation column(12) into pipeline(18) to heat tank(l).
  • Cooling water exchanger(31) is used to regulate the refined heating oil temperature to supply the necessary heat needed for the crude oil tank(l).
  • cooling exchanger(32) in pipeline(19) is used to lower or cooled down the refined oil before entering the refined vegetable oil/fats tank(20) as a finish product that is suitable as a blodiesel feedstock.

Landscapes

  • Life Sciences & Earth Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Microbiology (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • Organic Chemistry (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Fats And Perfumes (AREA)

Abstract

La présente invention concerne un procédé et un processus pour la fabrication économique de matières premières utilisées dans la production de biodiesel à partir d'huiles végétales et de graisses animales brutes (représentées par les flèches en pointillé) par le biais d'un procédé continu mettant en œuvre un processus de raffinage d'huile modifié et simplifié, conçu spécifiquement à cette fin, tel que représenté dans la figure 1, l'huile raffinée provenant du fond d'une colonne de distillation (14) et sert d'huile thermique (représentée par les flèches pleines) dans le réchauffeur de pack chaud chauffé à l'acide gras (16) alimenté en combustible par des acides gras libres résiduels provenant de la canalisation (25) générés à partir d'acides gras libres vaporisés provenant de la canalisation (21) dans le condenseur (22) qui pénètre dans le réservoir à vaporisation instantanée (23) qui est équipé d'un serpentin de chauffage réchauffé par l'huile raffinée provenant du processus de raffinage dans le serpentin de chauffage du pack chaud.
PCT/MY2008/000014 2008-02-26 2008-02-26 Procédé amélioré de raffinage d'huile végétale et de graisses animales pour matières premières utilisées dans la production de biodiesel WO2009025542A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/MY2008/000014 WO2009025542A1 (fr) 2008-02-26 2008-02-26 Procédé amélioré de raffinage d'huile végétale et de graisses animales pour matières premières utilisées dans la production de biodiesel

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/MY2008/000014 WO2009025542A1 (fr) 2008-02-26 2008-02-26 Procédé amélioré de raffinage d'huile végétale et de graisses animales pour matières premières utilisées dans la production de biodiesel

Publications (1)

Publication Number Publication Date
WO2009025542A1 true WO2009025542A1 (fr) 2009-02-26

Family

ID=40042976

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/MY2008/000014 WO2009025542A1 (fr) 2008-02-26 2008-02-26 Procédé amélioré de raffinage d'huile végétale et de graisses animales pour matières premières utilisées dans la production de biodiesel

Country Status (1)

Country Link
WO (1) WO2009025542A1 (fr)

Cited By (32)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7915460B2 (en) 2007-09-20 2011-03-29 Uop Llc Production of diesel fuel from biorenewable feedstocks with heat integration
US7982075B2 (en) 2007-09-20 2011-07-19 Uop Llc Production of diesel fuel from biorenewable feedstocks with lower hydrogen consumption
US7982079B2 (en) 2008-09-11 2011-07-19 Uop Llc Integrated process for production of diesel fuel from renewable feedstocks and ethanol denaturizing
US7982077B2 (en) 2007-09-20 2011-07-19 Uop Llc Production of diesel fuel from biorenewable feedstocks with selective separation of converted oxygen
US7982076B2 (en) 2007-09-20 2011-07-19 Uop Llc Production of diesel fuel from biorenewable feedstocks
US7982078B2 (en) 2007-09-20 2011-07-19 Uop Llc Production of diesel fuel from biorenewable feedstocks with selective separation of converted oxygen
US7999143B2 (en) 2007-09-20 2011-08-16 Uop Llc Production of diesel fuel from renewable feedstocks with reduced hydrogen consumption
US7999142B2 (en) 2007-09-20 2011-08-16 Uop Llc Production of diesel fuel from biorenewable feedstocks
US8003834B2 (en) 2007-09-20 2011-08-23 Uop Llc Integrated process for oil extraction and production of diesel fuel from biorenewable feedstocks
US8039682B2 (en) 2008-03-17 2011-10-18 Uop Llc Production of aviation fuel from renewable feedstocks
US8058492B2 (en) 2008-03-17 2011-11-15 Uop Llc Controlling production of transportation fuels from renewable feedstocks
US8193399B2 (en) 2008-03-17 2012-06-05 Uop Llc Production of diesel fuel and aviation fuel from renewable feedstocks
US8193400B2 (en) 2008-03-17 2012-06-05 Uop Llc Production of diesel fuel from renewable feedstocks
US8198492B2 (en) 2008-03-17 2012-06-12 Uop Llc Production of transportation fuel from renewable feedstocks
US8283506B2 (en) 2008-12-17 2012-10-09 Uop Llc Production of fuel from renewable feedstocks using a finishing reactor
US8304592B2 (en) 2008-06-24 2012-11-06 Uop Llc Production of paraffinic fuel from renewable feedstocks
US8314274B2 (en) 2008-12-17 2012-11-20 Uop Llc Controlling cold flow properties of transportation fuels from renewable feedstocks
US8324438B2 (en) 2008-04-06 2012-12-04 Uop Llc Production of blended gasoline and blended aviation fuel from renewable feedstocks
US8329967B2 (en) 2008-04-06 2012-12-11 Uop Llc Production of blended fuel from renewable feedstocks
US8329969B2 (en) 2008-04-06 2012-12-11 Uop Llc Fuel and fuel blending components from biomass derived pyrolysis oil
US8329968B2 (en) 2008-04-06 2012-12-11 Uop Llc Production of blended gasoline aviation and diesel fuels from renewable feedstocks
US8471079B2 (en) 2008-12-16 2013-06-25 Uop Llc Production of fuel from co-processing multiple renewable feedstocks
US8471081B2 (en) 2009-12-28 2013-06-25 Uop Llc Production of diesel fuel from crude tall oil
US8742183B2 (en) 2007-12-21 2014-06-03 Uop Llc Production of aviation fuel from biorenewable feedstocks
US8766025B2 (en) 2008-06-24 2014-07-01 Uop Llc Production of paraffinic fuel from renewable feedstocks
US8900443B2 (en) 2011-04-07 2014-12-02 Uop Llc Method for multi-staged hydroprocessing using quench liquid
CN104194929A (zh) * 2014-09-04 2014-12-10 陈汉卿 一种油脂提炼系统
CN104206563A (zh) * 2014-09-28 2014-12-17 蒋艳玲 一种猪油的加工方法
US8921627B2 (en) 2008-12-12 2014-12-30 Uop Llc Production of diesel fuel from biorenewable feedstocks using non-flashing quench liquid
CN105368581A (zh) * 2015-11-24 2016-03-02 重庆市盛沿食品有限责任公司 一种猪油的炼制方法
CN109370782A (zh) * 2018-11-30 2019-02-22 德州市荣光生物科技有限公司 地沟油加工处理热能循环利用装置
US11008520B2 (en) 2015-08-06 2021-05-18 Uop Llc Process for reconfiguring existing treating units in a refinery

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4623489A (en) * 1985-04-02 1986-11-18 Rivers Jr Jacob B Method of refining edible oil for preventing auto-oxidation of the oil
DE3838932C1 (en) * 1988-11-17 1990-04-26 Hermann Dr. 4400 Muenster De Stage Process and plant for the physical refining of edible oils, fats and esters
US5315021A (en) * 1992-07-01 1994-05-24 The Procter & Gamble Company Process for removing chlorophyll color impurities from vegetable oils
WO1994012596A1 (fr) * 1992-12-03 1994-06-09 Unilever N.V. Procede de raffinage d'huiles comestibles
US6251460B1 (en) * 1998-12-22 2001-06-26 Unilever Patent Holdings Bv Refining of vegetable oil
DE102005039296A1 (de) * 2005-08-19 2007-02-22 Ulrich Friesen Verfahren zum Betreiben eines Verbrennungsmotors
WO2007093326A1 (fr) * 2006-02-15 2007-08-23 Aser S.R.L. Procédé de désacidification d'huiles et/ou de graisses
WO2007146971A1 (fr) * 2006-06-13 2007-12-21 Gs Industrial Design, Inc. Procédé de raffinage d'huile récupérée à partir de produits secondaires de production d'éthanol

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4623489A (en) * 1985-04-02 1986-11-18 Rivers Jr Jacob B Method of refining edible oil for preventing auto-oxidation of the oil
DE3838932C1 (en) * 1988-11-17 1990-04-26 Hermann Dr. 4400 Muenster De Stage Process and plant for the physical refining of edible oils, fats and esters
US5315021A (en) * 1992-07-01 1994-05-24 The Procter & Gamble Company Process for removing chlorophyll color impurities from vegetable oils
WO1994012596A1 (fr) * 1992-12-03 1994-06-09 Unilever N.V. Procede de raffinage d'huiles comestibles
US6251460B1 (en) * 1998-12-22 2001-06-26 Unilever Patent Holdings Bv Refining of vegetable oil
DE102005039296A1 (de) * 2005-08-19 2007-02-22 Ulrich Friesen Verfahren zum Betreiben eines Verbrennungsmotors
WO2007093326A1 (fr) * 2006-02-15 2007-08-23 Aser S.R.L. Procédé de désacidification d'huiles et/ou de graisses
WO2007146971A1 (fr) * 2006-06-13 2007-12-21 Gs Industrial Design, Inc. Procédé de raffinage d'huile récupérée à partir de produits secondaires de production d'éthanol

Cited By (32)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8003834B2 (en) 2007-09-20 2011-08-23 Uop Llc Integrated process for oil extraction and production of diesel fuel from biorenewable feedstocks
US7915460B2 (en) 2007-09-20 2011-03-29 Uop Llc Production of diesel fuel from biorenewable feedstocks with heat integration
US7982077B2 (en) 2007-09-20 2011-07-19 Uop Llc Production of diesel fuel from biorenewable feedstocks with selective separation of converted oxygen
US7982075B2 (en) 2007-09-20 2011-07-19 Uop Llc Production of diesel fuel from biorenewable feedstocks with lower hydrogen consumption
US7982076B2 (en) 2007-09-20 2011-07-19 Uop Llc Production of diesel fuel from biorenewable feedstocks
US7982078B2 (en) 2007-09-20 2011-07-19 Uop Llc Production of diesel fuel from biorenewable feedstocks with selective separation of converted oxygen
US7999143B2 (en) 2007-09-20 2011-08-16 Uop Llc Production of diesel fuel from renewable feedstocks with reduced hydrogen consumption
US7999142B2 (en) 2007-09-20 2011-08-16 Uop Llc Production of diesel fuel from biorenewable feedstocks
US8742183B2 (en) 2007-12-21 2014-06-03 Uop Llc Production of aviation fuel from biorenewable feedstocks
US8058492B2 (en) 2008-03-17 2011-11-15 Uop Llc Controlling production of transportation fuels from renewable feedstocks
US8039682B2 (en) 2008-03-17 2011-10-18 Uop Llc Production of aviation fuel from renewable feedstocks
US8193399B2 (en) 2008-03-17 2012-06-05 Uop Llc Production of diesel fuel and aviation fuel from renewable feedstocks
US8193400B2 (en) 2008-03-17 2012-06-05 Uop Llc Production of diesel fuel from renewable feedstocks
US8198492B2 (en) 2008-03-17 2012-06-12 Uop Llc Production of transportation fuel from renewable feedstocks
US8324438B2 (en) 2008-04-06 2012-12-04 Uop Llc Production of blended gasoline and blended aviation fuel from renewable feedstocks
US8329968B2 (en) 2008-04-06 2012-12-11 Uop Llc Production of blended gasoline aviation and diesel fuels from renewable feedstocks
US8329969B2 (en) 2008-04-06 2012-12-11 Uop Llc Fuel and fuel blending components from biomass derived pyrolysis oil
US8329967B2 (en) 2008-04-06 2012-12-11 Uop Llc Production of blended fuel from renewable feedstocks
US8766025B2 (en) 2008-06-24 2014-07-01 Uop Llc Production of paraffinic fuel from renewable feedstocks
US8304592B2 (en) 2008-06-24 2012-11-06 Uop Llc Production of paraffinic fuel from renewable feedstocks
US7982079B2 (en) 2008-09-11 2011-07-19 Uop Llc Integrated process for production of diesel fuel from renewable feedstocks and ethanol denaturizing
US8921627B2 (en) 2008-12-12 2014-12-30 Uop Llc Production of diesel fuel from biorenewable feedstocks using non-flashing quench liquid
US8471079B2 (en) 2008-12-16 2013-06-25 Uop Llc Production of fuel from co-processing multiple renewable feedstocks
US8314274B2 (en) 2008-12-17 2012-11-20 Uop Llc Controlling cold flow properties of transportation fuels from renewable feedstocks
US8283506B2 (en) 2008-12-17 2012-10-09 Uop Llc Production of fuel from renewable feedstocks using a finishing reactor
US8471081B2 (en) 2009-12-28 2013-06-25 Uop Llc Production of diesel fuel from crude tall oil
US8900443B2 (en) 2011-04-07 2014-12-02 Uop Llc Method for multi-staged hydroprocessing using quench liquid
CN104194929A (zh) * 2014-09-04 2014-12-10 陈汉卿 一种油脂提炼系统
CN104206563A (zh) * 2014-09-28 2014-12-17 蒋艳玲 一种猪油的加工方法
US11008520B2 (en) 2015-08-06 2021-05-18 Uop Llc Process for reconfiguring existing treating units in a refinery
CN105368581A (zh) * 2015-11-24 2016-03-02 重庆市盛沿食品有限责任公司 一种猪油的炼制方法
CN109370782A (zh) * 2018-11-30 2019-02-22 德州市荣光生物科技有限公司 地沟油加工处理热能循环利用装置

Similar Documents

Publication Publication Date Title
WO2009025542A1 (fr) Procédé amélioré de raffinage d'huile végétale et de graisses animales pour matières premières utilisées dans la production de biodiesel
Santori et al. A review analyzing the industrial biodiesel production practice starting from vegetable oil refining
US8764947B2 (en) Method and system for disposal of furfural wastewater and method and system for furfural production
CN103740462A (zh) 一种油脂精制方法
US7872149B2 (en) Biodiesel processes in the presence of free fatty acids and biodiesel producer compositions
CN101702916A (zh) 制备脂肪酸甲酯(生物柴油)的综合方法
AU2017246581B2 (en) Process for recovery of glycerol from biodiesel production streams
CN103409242A (zh) 植物油精炼中碱炼副产品-皂脚的循环利用工艺及反应器
Gavin Edible oil deodorization
JP3533061B2 (ja) 廃食用油等から高級脂肪酸のメチルエステルとグリセリンとを連続的に製造する方法および装置
US20140020282A1 (en) Method and system for integrated biodiesel production
CN114729283A (zh) 植物油连续无皂脱胶、精炼工艺及其设备
CN102206541B (zh) 一种废弃油脂的精制方法
US20160376204A1 (en) Method for Reclaiming Usable Products from Biosolids
US20100240917A1 (en) Enzymatic oil recuperation process
US20240124785A1 (en) Method for the removal of chlorine from fats, oils and greases
US10975328B2 (en) Methods for making free fatty acids and fatty acid derivatives from mixed lipid feedstocks or soapstocks
Zehnder Deodorization 1975
Lakshmanan Sustainable practices of an edible oils refining complex
CN103159590A (zh) 一种生物柴油生产过程中过量甲醇回收工艺
CN103710143A (zh) 食用油半连续精炼工艺
CN109609284A (zh) 一种废白土提油工艺及其系统
JP2016169616A (ja) バイオディーゼル発電装置
JP2011148874A (ja) 脂肪酸アルキルエステルの製造方法とその製造装置
KR102028273B1 (ko) 동물성 폐유를 이용한 바이오디젤 원료유, 중유 및 절삭유의 분리 제조방법

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 08723821

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 08723821

Country of ref document: EP

Kind code of ref document: A1