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EP0808890A2 - Procédé et dispositif de purification par adsorption d'huiles et de graisses végétales et/ou minérales - Google Patents

Procédé et dispositif de purification par adsorption d'huiles et de graisses végétales et/ou minérales Download PDF

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Publication number
EP0808890A2
EP0808890A2 EP97108383A EP97108383A EP0808890A2 EP 0808890 A2 EP0808890 A2 EP 0808890A2 EP 97108383 A EP97108383 A EP 97108383A EP 97108383 A EP97108383 A EP 97108383A EP 0808890 A2 EP0808890 A2 EP 0808890A2
Authority
EP
European Patent Office
Prior art keywords
stage
oil
separation stage
fat
filter
Prior art date
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.)
Granted
Application number
EP97108383A
Other languages
German (de)
English (en)
Other versions
EP0808890A3 (fr
EP0808890B1 (fr
Inventor
Peter Dr. Dipl.-Ing. Transfeld
Gunter Dipl.-Ing. Börner
Matthias Dipl.-Ing. Schneider
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
OEHMI AKTIENGESELLSCHAFT
Original Assignee
Ohmi Forschung und Ingenieurstechnik GmbH
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 Ohmi Forschung und Ingenieurstechnik GmbH filed Critical Ohmi Forschung und Ingenieurstechnik GmbH
Publication of EP0808890A2 publication Critical patent/EP0808890A2/fr
Publication of EP0808890A3 publication Critical patent/EP0808890A3/fr
Application granted granted Critical
Publication of EP0808890B1 publication Critical patent/EP0808890B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G25/00—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents
    • C10G25/06—Refining of hydrocarbon oils in the absence of hydrogen, with solid sorbents with moving sorbents or sorbents dispersed in the oil
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G53/00—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes
    • C10G53/02—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only
    • C10G53/08—Treatment of hydrocarbon oils, in the absence of hydrogen, by two or more refining processes plural serial stages only including at least one sorption step
    • 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
    • C11B3/10—Refining fats or fatty oils by adsorption

Definitions

  • the invention relates to a method and a device for the adsorptive cleaning of vegetable and / or mineral oils and fats in a multi-stage countercurrent process.
  • the raw material i.e. the unpurified oil or fat
  • a first stage in which contact is made with already used and partially loaded absorbent.
  • the so contacted and pre-cleaned substance is separated in a first separation stage, the now heavily loaded adsorbent is removed from the process, the already partially cleaned and bleached oil or fat remains in the process.
  • It is now contacted with fresh adsorbent, which is introduced into the process from the outside. This process takes place in a second stage.
  • This mixture of contacted fresh adsorbent and pre-cleaned oil essentially extracts the last undesirable oil accompanying substances from the oil and is fed to a second separation stage.
  • the second separation stage then only allows the finished cleaned oil or fat to pass through.
  • This second separation stage now retains the adsorbent contained and the other constituents absorbed by this adsorbent.
  • This adsorbent - that is the core idea of a countercurrent system - should now be added to the unpurified oil in the first stage, since the only partially loaded adsorbent can still serve its cleaning purpose there.
  • the object of the invention is to propose a method and a device with which this problem can be counteracted.
  • This object is achieved in a process in that in the second separation stage, the constituents filtered out of the oil or fat are obtained and / or processed as pumpable sludge and conveyed to the unpurified oil or fat in the first stage with exclusion of air.
  • the second separation stage has a device which processes the separated components as pumpable sludge and can be fed to the first stage via a line in the absence of air.
  • Bleaching earth is primarily considered as the adsorbent; this designation is used in the following, without this being intended to restrict it to this type of absorbent. It is also possible to use activated carbon and silica gel, eg Trisyl, or also mixtures; the bleaching earth can be natural or activated.
  • the consistency of the sludge should preferably be mentioned, for example as follows:
  • the liquid content is over 30% in order to ensure good pumpability. It should also be below 80%, since an even higher amount of liquid is not necessary and in this way the oil backmixing is kept within limits. In order to keep the sludge pumpable, more oil is simply retained in the separation stage and reused and returned to the first stage. This is quite effective, but of course it does not have to be unlimited.
  • the temperature should, if possible, be above 60 ° C, since this also greatly accommodates the pumpability. In known methods, attempts are usually made to keep this temperature as low as possible, since, of course, high temperatures immediately promote the reaction with the damaging oxygen in contact with air. This risk no longer plays a role according to the invention, so that the advantage of the high temperature can be used without having to accept the simultaneous disadvantage existing in the prior art.
  • a candle filter or candle pressure filter is preferably used in the second separation stage.
  • This type of filter is also known under the name Puls Tube Filter or Cricket Filter or Contibac Filter from various suppliers.
  • a discontinuous cake discharge is preferably carried out, the filter cake (or filter sludge or sludge - see above) being buffered in the filter, so that no additional container is required.
  • the release from the second separation stage takes place in a continuous dosage; this continuous flow can possibly be interrupted each time the cake is dropped in order to avoid disruptions and influences.
  • This dosage can also be controlled in such a way that the cone is emptied between two cakes. This can be done simply by determining the amount of the filter cake in the cone and then emptying it in time.
  • a plate filter or Niagara filter can be used, which is used in a conventional normal driving style.
  • acid in particular phosphoric acid or citric acid
  • the acid addition can be supplemented by further water addition.
  • the amount of acid itself should be a maximum of 3000 ppm, the amount of water a maximum of 0.6%.
  • the addition of acid and water improves the filtration in the filters, but also improves the bleaching effect.
  • the addition of acid and water will take place before the first stage, ie before the first bleacher.
  • uncleaned oil 1 or fat is added, treated in the system as described below and leaves the process as cleaned and bleached oil 2 or fat.
  • oils and fats of vegetable and / or mineral origin are all meant; the process can be applied to a variety of different oils and fats.
  • Fresh bleaching earth 3 (or another adsorbent) must be added to the cleaning process; this adsorbent also leaves the process after several process steps as loaded adsorbent 4 together with the undesirable oil accompanying substances or components of the oil or fat, for example the dyes.
  • the unpurified oil 1 (or fat) is optionally fed together with acid 8 to a first stage 11.
  • this first stage 11 it is brought into contact with adsorbent that has already been used and is partially loaded, a motor M ensuring vigorous mixing and steam 6 being supplied for tempering the oil.
  • the details of level 11 correspond to the usual, a stirrer is provided in addition to various baffles.
  • the partially loaded adsorbent from the heavily contaminated oil liquid, due to the gradient effect, also assumes corresponding oil accompanying substances or dyes which are released by the oil in this way.
  • the entire mixture is then over one Pump 12 removed from stage 11 and transferred to the right in FIG. 1 into a first separation stage.
  • the first separation stage has two filters 15 and 16, which are connected in parallel and work in alternation: Whenever one of the two filters 15 and 16 has to be cleaned, the other runs.
  • the filters 15, 16 of the first separation stage filter out the now heavily loaded adsorbent with all undesirable oil accompanying substances and color constituents and collect them in schematically indicated collecting containers 17. From there they are removed from the cycle, as shown by arrow 4. Filters 15 and 16 are e.g. around Niagara filters or plate filters.
  • the oil or fat is now pre-cleaned and leaves the first separation stage 15, 16 as such - identified by 18 - under certain circumstances acid 8 or water can again be added.
  • This now pre-cleaned oil 18 is mixed together with fresh adsorbent 3 in a stirrer 23, this mixture is then fed from the stirrer 23 into the second stage 21.
  • steam 6 is supplied to temper the oil; vacuum 5 is again applied both in the stirrer 23 and in the second stage 21.
  • the mode of operation of the second stage 21 is basically similar to the first stage 11: the gradient effect here means that the fresh adsorbent 3 can in turn effectively remove the dyestuffs and accompanying oils from the pre-cleaned oil 18.
  • This mixture is then conveyed again via the pump 22 and fed to a second separation stage 25 as a mixture 28 of relatively well cleaned oil and adsorbent with the appropriate loads and color particles.
  • This second separation stage 25 is the core of the system or the invention.
  • the second separation stage 25 has a candle filter or a candle pressure filter, also known in the industry as a pulse tube filter or cricket filter or Contibac filter. These filters have a cone in their lower area.
  • the filter cake which consists of loaded adsorbent and oil, is discontinuously removed from the filter candles. thrown off. This discharge takes place in such a way that the filter cake formed is still sludge-shaped, that is to say that it still contains a relatively large proportion of oil compared to the prior art.
  • This liquid content is between 30% and 80% of the filter sludge formed. This filter sludge falls into the cone at the bottom and fills it up to a certain height.
  • This fill level is sensed by suitable sensors, which in this way convey an appropriate knowledge of the fill state.
  • suitable sensors which in this way convey an appropriate knowledge of the fill state.
  • the filter sludge is now used as the already mentioned, used and partially loaded adsorbent 29 and mixed with the unpurified oil. The process then continues with him.
  • the continuous supply of partially loaded adsorbent from the second separation stage 25 to the first stage 11 can occasionally be interrupted without disturbing the process, for example if no disturbances through the line are to get into the first stage during the filter cake discharge. If the supply of filter sludge is interrupted over a more or less short period of time, this has little effect on the actual cleaning process.
  • the filling level in the cone of the second separation stage 25 is periodically between 0% and 100%. Immediately before a filter cake is ejected, the filling level is approximately 0%, namely when the filter cake from the previous filter cleaning is pumped into stage 11. Immediately after a filter cake is dropped, the filling level is 100%.
  • the second separation stage 25 itself then leaves the finished oil or fat at 2 after the filtration.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Dispersion Chemistry (AREA)
  • Microbiology (AREA)
  • Wood Science & Technology (AREA)
  • Fats And Perfumes (AREA)
  • Cleaning In General (AREA)
  • Treatment Of Sludge (AREA)
  • Treatment Of Liquids With Adsorbents In General (AREA)
EP97108383A 1996-05-23 1997-05-23 Procédé et dispositif de purification par adsorption d'huiles et de graisses végétales et/ou minérales Expired - Lifetime EP0808890B1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE19620695 1996-05-23
DE19620695A DE19620695C1 (de) 1996-05-23 1996-05-23 Verfahren und Vorrichtung zur adsorptiven Reinigung von pflanzlichen und/oder mineralischen Ölen und Fetten

Publications (3)

Publication Number Publication Date
EP0808890A2 true EP0808890A2 (fr) 1997-11-26
EP0808890A3 EP0808890A3 (fr) 1999-05-06
EP0808890B1 EP0808890B1 (fr) 2002-01-23

Family

ID=7795071

Family Applications (1)

Application Number Title Priority Date Filing Date
EP97108383A Expired - Lifetime EP0808890B1 (fr) 1996-05-23 1997-05-23 Procédé et dispositif de purification par adsorption d'huiles et de graisses végétales et/ou minérales

Country Status (11)

Country Link
US (1) US5753103A (fr)
EP (1) EP0808890B1 (fr)
CN (1) CN1073149C (fr)
BR (1) BR9703388A (fr)
CA (1) CA2206032C (fr)
DE (1) DE19620695C1 (fr)
ID (1) ID17420A (fr)
IN (1) IN182570B (fr)
MX (1) MX9703820A (fr)
RU (1) RU2188852C2 (fr)
TR (1) TR199700421A3 (fr)

Families Citing this family (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19711174A1 (de) * 1997-03-18 1998-09-24 Oehmi Forsch & Ingtech Gmbh Verfahren und Vorrichtung zum Reinigen von Verunreinigungen enthaltenden Flüssigkeiten
DE102007031039A1 (de) * 2007-07-04 2009-01-08 Süd-Chemie AG Verfahren zur schonenden Raffination von Pflanzenölen mit Naturbleicherde
US8232419B2 (en) * 2008-10-02 2012-07-31 The Dallas Group Of America Triacylglycerol purification by a continuous regenerable adsorbent process
DE102011053103A1 (de) 2010-09-02 2012-03-22 G+R Technology Group Ag Einrichtung und verfahren zur gewinnung von öl und/oder fett aus öl- und/oder fetthaltigem wässerigen abfall
CN102827634B (zh) * 2012-09-05 2015-07-22 新疆现代石油化工股份有限公司 提高基础油粘度指数的吸附分离装置及方法
CN104903015B (zh) 2012-11-02 2018-06-22 罗伯特·许德克林儿 从生物废物或生物质中获得至少一种纯净物的设备和方法
CN103937543A (zh) * 2014-04-21 2014-07-23 沈阳化工大学 废旧轮胎裂解油脱色、脱臭的方法
CN104946304A (zh) * 2015-06-12 2015-09-30 宁夏宝塔石化科技实业发展有限公司 一种劣质柴油的脱色、除臭一体化装置及方法
CN106237651B (zh) * 2016-08-31 2018-04-27 山东新和成氨基酸有限公司 一种液固体系动态吸附的方法及其装置
CN108236015A (zh) * 2016-12-27 2018-07-03 丰益(上海)生物技术研发中心有限公司 亚麻籽油油脂组合物
CN106867660A (zh) * 2017-04-27 2017-06-20 武汉轻工大学 一种米糠混合油的净化方法
WO2025051086A1 (fr) 2023-09-04 2025-03-13 Basf Se Procédé de recyclage et produits recyclés

Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5342508A (en) * 1991-07-23 1994-08-30 Ohmi Forschung Und Ingenieurstechnik Gmbh Method of adsorptive purification of vegetable and/or mineral oils and fats

Family Cites Families (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB700234A (en) * 1948-11-04 1953-11-25 Girdler Corp Improvements in or relating to method of bleaching petroleum or fatty oils

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5342508A (en) * 1991-07-23 1994-08-30 Ohmi Forschung Und Ingenieurstechnik Gmbh Method of adsorptive purification of vegetable and/or mineral oils and fats

Also Published As

Publication number Publication date
EP0808890A3 (fr) 1999-05-06
MX9703820A (es) 1998-04-30
TR199700421A2 (xx) 1997-12-21
DE19620695C1 (de) 1997-05-15
EP0808890B1 (fr) 2002-01-23
RU2188852C2 (ru) 2002-09-10
ID17420A (id) 1997-12-24
IN182570B (fr) 1999-05-08
BR9703388A (pt) 2000-06-20
US5753103A (en) 1998-05-19
CN1073149C (zh) 2001-10-17
CA2206032A1 (fr) 1997-11-23
CN1174881A (zh) 1998-03-04
TR199700421A3 (tr) 1997-12-21
CA2206032C (fr) 2006-11-21

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