WO2011127869A1 - Procédé de traitement d'un mélange de substances mises au rebut contenant du glycérol en tant que constituant principal - Google Patents

Procédé de traitement d'un mélange de substances mises au rebut contenant du glycérol en tant que constituant principal Download PDF

Info

Publication number
WO2011127869A1
WO2011127869A1 PCT/CZ2010/000048 CZ2010000048W WO2011127869A1 WO 2011127869 A1 WO2011127869 A1 WO 2011127869A1 CZ 2010000048 W CZ2010000048 W CZ 2010000048W WO 2011127869 A1 WO2011127869 A1 WO 2011127869A1
Authority
WO
WIPO (PCT)
Prior art keywords
mixture
methane
iron
iii
oxidization
Prior art date
Application number
PCT/CZ2010/000048
Other languages
English (en)
Inventor
Alois Vasicek
Original Assignee
G.F. Agro A.S.
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 G.F. Agro A.S. filed Critical G.F. Agro A.S.
Priority to PCT/CZ2010/000048 priority Critical patent/WO2011127869A1/fr
Publication of WO2011127869A1 publication Critical patent/WO2011127869A1/fr

Links

Classifications

    • 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
    • B01J19/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J19/087—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy
    • B01J19/088—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy giving rise to electric discharges
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C29/00—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring
    • C07C29/48—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups
    • C07C29/50—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by oxidation reactions with formation of hydroxy groups with molecular oxygen only
    • 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
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0803—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy
    • B01J2219/0805—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy giving rise to electric discharges
    • B01J2219/0807—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy giving rise to electric discharges involving electrodes
    • B01J2219/0809—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy giving rise to electric discharges involving electrodes employing two or more electrodes
    • 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
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0803—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy
    • B01J2219/0805—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy giving rise to electric discharges
    • B01J2219/0807—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy giving rise to electric discharges involving electrodes
    • B01J2219/0837—Details relating to the material of the electrodes
    • B01J2219/0839—Carbon
    • 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
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0803—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy
    • B01J2219/0805—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor employing electric or magnetic energy giving rise to electric discharges
    • B01J2219/0845—Details relating to the type of discharge
    • B01J2219/0849—Corona pulse discharge
    • 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
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0871—Heating or cooling of the reactor
    • 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
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0873—Materials to be treated
    • B01J2219/0881—Two or more materials
    • B01J2219/0884—Gas-liquid
    • 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
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0873—Materials to be treated
    • B01J2219/0892—Materials to be treated involving catalytically active material
    • 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
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0894—Processes carried out in the presence of a plasma
    • B01J2219/0896—Cold plasma

Definitions

  • the invention relates to the method for processing of a mixture of waste substances containing glycerol as the prevailing component, in particular recycling of waste glycerol phase from the rape-seed oil methyl ester production.
  • the waste glycerol contains usually various amounts of water (up to 50 wt %) and various amounts of other waste materials, whereas owing to prevailing technologies such as processing of fats, oils or related substances a waste glycerol mixture contains in particular substances of basic character such as alkaline salts or hydroxides.
  • This fuel is produced from vegetable oils by way of re-esterification.
  • triacylglyceride of fatty acid is converted to methyl ester of the respective fatty acid using methanol.
  • a state-of-the art method of processing of the waste product is based on receiving of pure glycerol which is further treated for acrylaldehyde or epichlorohydrin. Ho wever, the process of purification of the glycerol phase to technical-pure anhydrous glycerol is not a cheap one.
  • a step al) in which produced methane is separated from carbon dioxide is carried out before the partial oxidation of methane in the step b).
  • waste substances containing glycerol may have various composition and dilution.
  • the preferable waste mixture is the glycerol phase of the rape oil methyl ester production.
  • the method of processing of methyl esters of the respective vegetable oils eliminates considerably the recycling method of the glycerol phase of these productions according to the invention in which methanol is recovered from the raw waste phase.
  • the external acting field during deoxidation is heterogeneous electric and magneto-electric field, whereas it is more preferable if heterogeneous electric field is generated by pulsed high-frequency current combined with low-frequency or direct current.
  • the above-mentioned mixture of waste substances passes an electric field in the full range of electric current 30 to 400 A with co-acting of pulsed high-frequency current of resonance bands of oscillation from 100 Hz to 100 kHz resulting in corona of cold plasma with a temperature between 700 °C to 2100 °C, and simultaneously a circular magnetic field forms the outside edge of which covers the space of the cold plasma formed in the process.
  • elementary carbon is a convenient example of a catalytic-reduction agent which can be preferably coke, anthracite, graphite, carbon black or charcoal or their mixture, and the range of size of carbon particles is preferably 5 to 50 mm. . ; ' ⁇ .,
  • the most preferable embodiment involves, according to the invention, coke as the elementary carbon.
  • Surface of elementary carbon is in the preferable embodiment treated with deposition (adsorbing) of organic and/or inorganic substances/compounds containing iron, chrome and copper ions.
  • the deposition is performed via immersion the particles into aqueous solutions or suspensions containing the substances.
  • the inorganic particles adsorbed on the elementary carbon is iron(III) oxide in the case of iron compounds, copper(I) oxide in the case of copper compounds, or adsorbed aqueous solution of iron(III) and chromium(III) salts.
  • the step of separation of methane from carbon dioxide is performed specifically using a hydroxide or hydroxide mixture, with calcium hydroxide-Ca(OH) 2 being the most preferable one, particularly in the form of lime milk.
  • step b) partial oxidization of methane to methanol is realized preferably using the following sequential steps
  • Preferable oxidization gas for partial oxidization is air and/or oxygen whereas the rate of passing stream of gaseous mixture is in the range from approx. 0.1 to 1 m/s.
  • the subject of the invention is also a device for performing of partial oxidization of methane to methanol; it comprises a catalytic oxidization reactor consisting of at least one tube of electrically non-conductive material through the centre of which an electric resistance conductor passes connected outside to a source of electric current with feedback regulation.
  • a preferable embodiment according to the invention is the embodiment in which the electrical resistance conductor is made of iron, whereas another preferable material of an iron, nickel and chromium can be used.
  • the method according to the present invention involves two main technological steps.
  • the deoxidization step to which raw glycerol containing waste mixture of glycerol and minor amount of other waste substances enter, glycerol is deoxidized using a plasma reactor with reduction filling controlled by an electric field, with production of two main products of the reaction - methane and carbon dioxide.
  • the controlling non-homogenous electric field leading the reaction develops in the space between electrodes in which the catalytic reduction filling is also placed;
  • the filling consists of particles containing in their composition carbon selected from the group of materials containing coke, charcoal, anthracite surface of which is preferably treated with deposition of substances containing chromium and/or iron and/or copper.
  • the deposition is performed via immersing the particles in aqueous solution or suspensions containing the substances.
  • the electrodes are connected to a source of electric current.
  • Electric current in the space between two electrodes passes in a regime of co-acting low-frequency current of 30 to 400 A and high-frequency current in resonance bands of oscillation from 100 Hz to 100 kHz.
  • Such a generated electric field activates the filling between electrodes so that coronas of cold plasma having the temperature of 700 °C to 2100 °C form in between the particles of the reduction filling of the reactor.
  • the glycerol phase passes through the ⁇ it is immediately decomposed to methane and carbon dioxide, whereas the reduction filling of the reactor is also involved in stoichiometry of this reaction.
  • the products having average temperature between 350 °C and 550 °C go from the reactor to a cooler in which they are cooled to a temperature under 30 °C and then continue to the room of gas purification in which the mixture of methane and carbon dioxide is counterflown with hydroxide solution/solutions, preferably
  • Methane which is produced in the reaction, enters in the second technological step, partial catalytic oxidization where it enters in a blending equipment at first in which it is mixed with air in a stoichiometric ratio of partial oxidization and then the mixture is led to the catalytic oxidization reactor which consists of parallel tubes made of electrically non- conductive material, preferably glass or ceramics, with a diameter of 8 to 15 mm.
  • the catalytic oxidization reactor which consists of parallel tubes made of electrically non- conductive material, preferably glass or ceramics, with a diameter of 8 to 15 mm.
  • the source has been constructed so that enables fluent and feedback regulation of electric current. Passing of current through the conductor causes increase in the conduction temperature.
  • the conduction radiation depending on its composition acts as catalyst on the partial oxidization in the blender of the present methane to methanol whereas the oxidization reaction runs in the point of the highest radiation intensity, in the close surroundings of the conductor.
  • the output products of the oxidization reactor are cooled, vapours of methanol are condensed and the formed liquid is led e.g. to the preparation phase of methyl ester production in oil re-esterification where it is used as an entrance material.
  • the gaseous rest of condensation is removed for final purification in which it is disposed of all organic parts and released to the atmosphere.
  • the recycling method of waste glycerol phase was performed in a laboratory scale.
  • the first stage of decomposition of glycerol phase was performed in a 30 litre reactor in which a couple of graphite electrodes was placed.
  • the electrodes were fed with direct voltage of 36 V and high-frequency voltage with pulses of 10 kV and frequency 16 kHz.
  • a catalytic and reduction filling consisting of coke particles was placed between the electrodes.
  • the coke was activated in aqueous solution of iron(III) and chromium(III) salts.
  • To the reactor an inlet pipe with a diameter of 10 mm was led, connected also to a feed pump of glycerol phase.
  • the reactor outlet pipe was connected to a copper tube-type cooler with tube diameter of 15 mm.
  • the tube was corkscrewed and immersed in water.
  • the cooler outlet was led through a shower in a closed vessel in which a calcium hydroxide solution was sprayed through counterflow nozzles.
  • the gas produced was led to a 100 litre gasholder filled with water, pushed out by the entering gas.
  • the gas-holder outlet was connected through a stopcock to a blender consisting of a closed 200 litre vessel equipped with a fan of an explosion-proof type of construction. Air was supplied from another, 100 litre gas-holder to the blender through a stopcock.
  • the blender outlet was connected to a feeding membrane pump which was connected to the reactor of partial oxidization of methane consisting of one glass tube, 12 mm in diameter and 1.2 m long, through the centre of which a conductor was led - iron wire with the diameter of 1 mm.
  • the conductor was fed with voltage 14 V.
  • the feed pump fed to the first-stage reactor the glycerol phase till the gas-holder was filled with 20 litres of gaseous products.
  • the air-holder was filled up to the full volume using a compressor. Both fillings were brought into the blender and after approx. 60 s blending the membrane pump was turned on with a flow-rate of 10 litres per minute.
  • the product of the oxidization reactor was cooled with water in a laboratory glass cooler. During the time of a six-hour test 20 kg of glycerol phase was treated from which 12 kg of methanol was obtained.
  • the first stage of the method - deoxidation of the glycerol phase - was performed in a closed 300 litre vessel containing six plasma reactors connected to a common source of electric voltage 48 V and a pulse source of electric voltage 10 kV. Each of them contained in the space between electrodes a reduction catalytic filling - a mixture of coke, iron(III) oxide, copper(I) oxide in the weight ratio of 100 : 5 : 0.5. Each of the six of plasma reactors was connected through a solenoid valve to a pressure pipe in which pressure 1.6 MPa of the circulating glycerol phase was created using a gear pump.
  • the glycerol phase entered in the particular areas of the reactor and decomposed to methane, carbon dioxide and minor by-products according to the composition of the raw glycerol phase.
  • the gas produced was taken off the vessel through a tube-type cooler to a vessel containing a lime milk solution through which it was bubbled and led off to a membrane feeding device into which air was added and mixed with it in a volume ratio of 2-3 volume parts to 1 part of the produced gas.
  • the mixture was taken off to another vessel, hermetically sealed, in which a battery of glass tubes having 0 10 mm, length 1.35 m each, was placed. The tubes were interconnected so that gas passes through the tube space only.
  • each tube In the centre of each tube a conductor having 0 7mm, made of a material containing iron, chromium and nickel passed. Each conductor was connected to a voltage source terminal and provided with feedback regulation of current flow so that the conductor reached the max. temperature of 850 °C. Gas was led to the tubes so that its flow-rate did not exceed 0.5 m/s. Products from this reactor were in gaseous state and condensed in the subsequent tube-type condenser (cooler). The condensed liquid contained more than 95 % of methanol.
  • Example 2 Another example embodiment using the laboratory apparatus as in Example 1 dealt with treating of distiller's solubles from which ethanol was distilled off.
  • the method of processing of distiller's solubles containing 5 % of dry matter was performed in a laboratory scale.
  • the first stage of decomposition of distiller's solubles was carried out in a 30 litre reactor in which a couple of graphite electrodes was placed.
  • the electrodes were fed with direct voltage of 36 V and high-frequency voltage with pulses of 10 kV and frequency 16 kHz.
  • a catalytic and reduction filling consisting of coke particles was placed in between the electrodes.
  • the coke was activated in aqueous solution of iron (III) and chromium (III) salts.
  • Air was supplied from another, 100 litre gas holder to the blender trough a stopcock.
  • the blender outlet was connected to a feeding membrane pump which was connected to the reactor of partial oxidization of methane consisting of one glass tube, 12 mm in diameter and 1.2 m long, through the centre of which a conductor was led - iron wire with the diameter of 1 mm.
  • the conductor was fed with voltage 14 V.
  • the feeding pump fed to the first-stage reactor distiller ' s solubles till the gas-holder was filled with 10 litres of gaseous products.
  • the air-holder was fed to a volume of 30 litres using a compressor. Both fillings were brought into the blender and after approx.
  • the method according to the invention involving treating of waste mixtures of various materials with glycerol as the prevailing component can produce entering reaction materials for e.g. manufacture of bio-diesel fuel. This method can also considerably eliminate both ecological and economical burden caused by such wastes.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • General Health & Medical Sciences (AREA)
  • Toxicology (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Catalysts (AREA)

Abstract

La présente invention concerne un procédé de traitement d'un mélange de substances mises au rebut contenant du glycérol en tant que constituant principal. Dans le procédé selon l'invention, le mélange est tout d'abord soumis à une désoxydation au moyen d'un agent de réduction catalytique en coaction avec un domaine extérieur, produisant ainsi les constituants principaux que sont le méthane et le dioxyde de carbone avec une oxydation partielle du méthane en méthanol. Le méthanol produit est utilisé par exemple en tant que produit de départ pour la réestérification d'huile.
PCT/CZ2010/000048 2010-04-15 2010-04-15 Procédé de traitement d'un mélange de substances mises au rebut contenant du glycérol en tant que constituant principal WO2011127869A1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
PCT/CZ2010/000048 WO2011127869A1 (fr) 2010-04-15 2010-04-15 Procédé de traitement d'un mélange de substances mises au rebut contenant du glycérol en tant que constituant principal

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/CZ2010/000048 WO2011127869A1 (fr) 2010-04-15 2010-04-15 Procédé de traitement d'un mélange de substances mises au rebut contenant du glycérol en tant que constituant principal

Publications (1)

Publication Number Publication Date
WO2011127869A1 true WO2011127869A1 (fr) 2011-10-20

Family

ID=43416351

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CZ2010/000048 WO2011127869A1 (fr) 2010-04-15 2010-04-15 Procédé de traitement d'un mélange de substances mises au rebut contenant du glycérol en tant que constituant principal

Country Status (1)

Country Link
WO (1) WO2011127869A1 (fr)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103833498A (zh) * 2012-11-22 2014-06-04 财团法人工业技术研究院 酯类脱氧的方法
EP2980015B1 (fr) * 2013-03-29 2018-07-04 JFE Steel Corporation Procédé de fabrication de gaz à teneur élevée en calories

Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20030146310A1 (en) * 2001-08-17 2003-08-07 Jackson David P. Method, process and apparatus for high pressure plasma catalytic treatment of dense fluids
WO2003080504A1 (fr) * 2002-03-27 2003-10-02 Jisouken Co., Ltd. Dispositif pour produire de l'hydrogene au moyen d'hydrocarbure ou d'un compose contenant de l'oxygene comme substance et electrode de decharge utilisee dans ce dispositif
US20030220531A1 (en) * 2002-05-10 2003-11-27 Cortright Randy D. Low-temperature hydrocarbon production from oxygenated hydrocarbons
US20040022701A1 (en) * 2000-06-30 2004-02-05 Segal David Leslie Plasma assisted reactor
WO2007075476A2 (fr) * 2005-12-21 2007-07-05 Virent Energy Systems Inc. Catalyseurs et procedes de reformage de composes oxygenes
DE102006036332A1 (de) * 2006-08-03 2008-02-07 Süd-Chemie AG Verfahren zur Herstellung von Biodieselkraftstoff
FR2933391A3 (fr) * 2008-07-03 2010-01-08 Physiques Ecp Et Chimiques Conversion du glycerol en carburant liquide propre et renouvelable
WO2010012060A2 (fr) * 2008-07-30 2010-02-04 Quattor Petroquímica S.A. Procédé catalytique de transformation de la glycérine en charges d’alimentation dans le domaine de la pétrochimie

Patent Citations (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20040022701A1 (en) * 2000-06-30 2004-02-05 Segal David Leslie Plasma assisted reactor
US20030146310A1 (en) * 2001-08-17 2003-08-07 Jackson David P. Method, process and apparatus for high pressure plasma catalytic treatment of dense fluids
WO2003080504A1 (fr) * 2002-03-27 2003-10-02 Jisouken Co., Ltd. Dispositif pour produire de l'hydrogene au moyen d'hydrocarbure ou d'un compose contenant de l'oxygene comme substance et electrode de decharge utilisee dans ce dispositif
US20030220531A1 (en) * 2002-05-10 2003-11-27 Cortright Randy D. Low-temperature hydrocarbon production from oxygenated hydrocarbons
WO2007075476A2 (fr) * 2005-12-21 2007-07-05 Virent Energy Systems Inc. Catalyseurs et procedes de reformage de composes oxygenes
DE102006036332A1 (de) * 2006-08-03 2008-02-07 Süd-Chemie AG Verfahren zur Herstellung von Biodieselkraftstoff
FR2933391A3 (fr) * 2008-07-03 2010-01-08 Physiques Ecp Et Chimiques Conversion du glycerol en carburant liquide propre et renouvelable
WO2010012060A2 (fr) * 2008-07-30 2010-02-04 Quattor Petroquímica S.A. Procédé catalytique de transformation de la glycérine en charges d’alimentation dans le domaine de la pétrochimie

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103833498A (zh) * 2012-11-22 2014-06-04 财团法人工业技术研究院 酯类脱氧的方法
EP2980015B1 (fr) * 2013-03-29 2018-07-04 JFE Steel Corporation Procédé de fabrication de gaz à teneur élevée en calories

Similar Documents

Publication Publication Date Title
US8784617B2 (en) Process of converting gaseous hydrocarbons to a liquid hydrocarbon composition
CN109200970B (zh) 低温等离子双电场辅助气相反应合成化合物的装置和应用
EP1867702B1 (fr) Procédé de purification de carburant biodiesel
CN105754703B (zh) 废润滑油预处理方法
US11148116B2 (en) Methods and apparatus for synthesizing compounds by a low temperature plasma dual-electric field aided gas phase reaction
US9604898B2 (en) Ozonolysis operations for generation of reduced and/or oxidized product streams
JP6661534B2 (ja) 相界面反応を用いた反応生成物製造方法及び相界面反応装置、ならびに二次反応生成物製造方法
US6045761A (en) Process and device for the conversion of a greenhouse gas
CN113165913A (zh) 用于等离子体诱导的水净化的方法和设备
WO2011127869A1 (fr) Procédé de traitement d'un mélange de substances mises au rebut contenant du glycérol en tant que constituant principal
KR20010012538A (ko) 물의 직접열분해에 의한 수소가스의 생성방법 및 그의 장치
Harris et al. Cold plasma catalysis as a novel approach for valorisation of untreated waste glycerol
CN107011120B (zh) 一种资源化处理二氧化碳和水高选择性合成乙醇的方法
CN206418075U (zh) 一种新的焦油残渣的处理装置
RU2579099C2 (ru) Способ некаталитического гидрообессеривания нефтепродуктов
EP4342844A1 (fr) Procédé de production d'hydrogène
RU2479621C1 (ru) Способ электротермолиза нефтепродуктов и установка для его осуществления
US20150259615A1 (en) Fuel generation using high-voltage electric fields methods
Harris Cold plasma initiated valorisation of triglyceride containing feedstocks
US20150210930A1 (en) Fuel generation using high-voltage electric fields methods
US9765270B2 (en) Fuel generation using high-voltage electric fields methods
Bang et al. Valorization of Glycerol through Plasma‐Induced Transformation into Formic Acid
Cook Industrial uses of ozone
CN103788999B (zh) 一种高酸原油的预处理方法
RU2458005C1 (ru) Способ утилизации диоксида углерода

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: 10734637

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: 10734637

Country of ref document: EP

Kind code of ref document: A1