WO2009016290A2 - Procédé d'incorporation d'alcool dans des carburants a forte teneur en composés aromatiques - Google Patents
Procédé d'incorporation d'alcool dans des carburants a forte teneur en composés aromatiques Download PDFInfo
- Publication number
- WO2009016290A2 WO2009016290A2 PCT/FR2008/000911 FR2008000911W WO2009016290A2 WO 2009016290 A2 WO2009016290 A2 WO 2009016290A2 FR 2008000911 W FR2008000911 W FR 2008000911W WO 2009016290 A2 WO2009016290 A2 WO 2009016290A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- alcohol
- mixture
- alcohols
- fuel
- extraction
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/10—Liquid carbonaceous fuels containing additives
- C10L1/14—Organic compounds
- C10L1/18—Organic compounds containing oxygen
- C10L1/185—Ethers; Acetals; Ketals; Aldehydes; Ketones
- C10L1/1857—Aldehydes; Ketones
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/02—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only
- C10L1/026—Liquid carbonaceous fuels essentially based on components consisting of carbon, hydrogen, and oxygen only for compression ignition
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
- C10L1/06—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for spark ignition
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/04—Liquid carbonaceous fuels essentially based on blends of hydrocarbons
- C10L1/08—Liquid carbonaceous fuels essentially based on blends of hydrocarbons for compression ignition
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10L—FUELS NOT OTHERWISE PROVIDED FOR; NATURAL GAS; SYNTHETIC NATURAL GAS OBTAINED BY PROCESSES NOT COVERED BY SUBCLASSES C10G, C10K; LIQUEFIED PETROLEUM GAS; ADDING MATERIALS TO FUELS OR FIRES TO REDUCE SMOKE OR UNDESIRABLE DEPOSITS OR TO FACILITATE SOOT REMOVAL; FIRELIGHTERS
- C10L1/00—Liquid carbonaceous fuels
- C10L1/10—Liquid carbonaceous fuels containing additives
- C10L1/14—Organic compounds
- C10L1/18—Organic compounds containing oxygen
- C10L1/182—Organic compounds containing oxygen containing hydroxy groups; Salts thereof
- C10L1/1822—Organic compounds containing oxygen containing hydroxy groups; Salts thereof hydroxy group directly attached to (cyclo)aliphatic carbon atoms
- C10L1/1824—Organic compounds containing oxygen containing hydroxy groups; Salts thereof hydroxy group directly attached to (cyclo)aliphatic carbon atoms mono-hydroxy
Definitions
- the present invention relates to a process for incorporating alcohol or a mixture of alcohols from aqueous solutions generated by biomass fermentation processes into a fuel.
- Biomass includes all organic, plant or animal materials, including:
- sugar plants sucgar beet, sugar cane, sugar sorghum .
- the alcohols produced by biomass fermentation processes are preferably ethanol produced by ethanol fermentation and butanol, as well as the ABE (acetone-butanol-ethanol) mixture produced by acetonobutyl fermentation.
- anhydrous ethanol from aqueous solutions first requires obtaining an ethanol / water mixture containing approximately 95% by volume of ethanol, the ethanol / ethanol mixture. water forming an azeotrope containing 95.6% by weight of ethanol at 0.1 MPa.
- This operation implementing a distillation process is extremely energetic. For example if starting from an aqueous solution titrating about 10% by volume of ethanol, it is necessary to use about 180 kg of vapor per hectolitre of ethanol to obtain this mixture.
- azeotropic distillation in the presence of a third body (for example benzene or cyclohexane)
- a third body for example benzene or cyclohexane
- the pathway using pervaporation on membrane is much more interesting from an energy point of view, since it consumes only about 30 kg of steam and about 4.5 kWh per hectolitre of alcohol produced.
- the adsorption on molecular sieves is moderately energy efficient, requiring about 30 to 60 kg of steam and about 2 to 3 kWh electric per hectolitre of alcohol in the case of a PSA (Pressure Swing Adsorption) with vapor phase adsorption .
- PSA Pressure Swing Adsorption
- the present invention proposes a new scheme of process for extracting directly with a fuel with a high content of aromatic compounds. Unlike distillation, extraction does not require any steam. The energy expenditure is then only of an electric nature. It is related to the contact and the mixing of the fluids in the extractor, as well as to the pressure losses that the fluids undergo in this apparatus.
- the process according to the invention makes it possible to directly incorporate the alcohol into the fuel, without first going through a distillation step, which makes it possible to greatly reduce the energy expenditure.
- Figure 1 shows a diagram of the process according to the present invention.
- FIG. 2 represents an embodiment of the process according to the present invention in which an oxygenated compound is introduced at an intermediate height in the extraction column.
- FIG. 3 represents an embodiment of the process according to the present invention in which the drying step consists of a cooling resulting in demixing of an aqueous phase.
- Figure 4 shows an embodiment of the process according to the present invention wherein the drying step is carried out by adsorption by circulating dry fuel from the production unit.
- the present invention describes a process for incorporating alcohol or a mixture of alcohols into fuels with a high content of aromatic compounds chosen from a gasoline reformate cut, a gasoline pyrolysis cut or a typical diesel fuel.
- LCO including:
- a liquid-liquid extraction step of the alcohol with at least one or more fuel bases by directly contacting an aqueous phase containing the alcohol or the mixture of alcohols and a hydrocarbon phase consisting of said fuel base, and
- the fuel in which the alcohol or mixture is incorporated has an aromatic content of at least 70% by weight.
- the fuel has an aromatic content greater than 80% by weight.
- a gasoline reformate cut preferably resulting from the refining process called reforming
- a gasoline pyrolysis cut a by-product of the steam cracking process
- This type of gas allows a much more favorable extraction with a gasoline obtained by mixing cuts from different refining processes. Indeed, the extraction of alcohol is much less effective if the aromatics content of gasoline is lower.
- a LCO gas oil is preferably chosen from the catalytic cracking units, also characterized by a high content of aromatics.
- the alcohol or the mixture of alcohols comes from any biomass fermentation process and is more particularly chosen from ethanol, butanol or acetone-butanol-ethanol (ABE) mixture.
- the fuel may optionally be supplemented with an oxygenated compound or a mixture of oxygenated compounds, which makes it possible to further improve the efficiency of the extraction of the alcohol.
- oxygenated additives are preferably:
- ethers for example ITEBE (ethyltertiobutyl ether), MTBE
- MEPEME (2-methyl-2-methoxypentane) or DIMEBU (2,3-dimethyl-2-methoxybutane)
- PTBE n-propyl tert-butyl ether
- alcohols for example butanol, TBA (terbutyl alcohol), IPA (isopropyl alcohol), isobutyl alcohol and / or methanol.
- the extraction step is carried out by directly contacting the aqueous phase containing the alcohol or the mixture of alcohols and the hydrocarbon phase constituted by one or more fuel bases.
- the aqueous phase may contain from 1 to 99% by volume of alcohol or mixture of alcohols.
- the aqueous phase contains 1 to 30% by volume of alcohol or mixture of alcohols. Even more preferentially, it contains between 5 and 15% by volume of alcohols or mixture of alcohols.
- Said aqueous phase containing the alcohol or the alcohol mixture is introduced at the top of the extraction column and said hydrocarbon phase containing the fuel base is introduced at the bottom of the extraction column.
- the aqueous phase and the hydrocarbon phase can be introduced into the extraction column at identical or different temperatures.
- the hydrocarbon phase can be used to heat the aqueous phase.
- the extraction is all the more favored as the temperature is high.
- the extraction step is carried out at a temperature between room temperature ,
- the pressure of the extractor is between atmospheric pressure and 10 MPa, preferably between atmospheric pressure and 1 MPa.
- the extraction step is performed by circulating the two phases against the current in devices promoting dispersion, contact and exchange of material between the aqueous phase and the hydrocarbon phase.
- an oxygenated compound in the case where an oxygenated compound is added to the fuel, it may be introduced with the hydrocarbon phase at the bottom of the column, or separately, at an intermediate height.
- the lower part of the extraction column, located under the intermediate injection behaves as a counter extraction section for the oxygenated product passed through the aqueous phase.
- an extract is obtained consisting of the fuel base containing an alcohol or mixture of alcohols and a portion of the water coming from the aqueous solution, and a raffinate.
- the raffinate is sent to a water treatment and / or recycled, for example in the upstream biomass fermentation process, and the extract containing the alcohol-enriched hydrocarbon phase is sent to the drying step. Indeed, the presence of this water may cause the demixing of the alcohol by cooling the alcoholic fuel solution storage. To avoid this demixing phenomenon, the hydrocarbon phase containing the alcohol and the water must therefore be dehydrated and / or cooled (drying).
- Drying within the meaning of the present invention, includes any method for extracting a fraction of the water content of a mixture.
- the drying can be carried out for example by the techniques mentioned below or by cooling resulting in demixing of the water.
- the drying step can be advantageously carried out by adsorption on molecular sieve, by pervaporation through membranes, or by distillation, the first two channels being preferred, in particular for reasons of lower energy consumption.
- the molecular sieves used to dry the alcohols are generally adsorbents of zeolite type, ie oxides having a structure three-dimensional resulting from the sequence of tetrahedral units leading to a network of channels of molecular size and pore diameter ranging from 3 to
- a zeolite is typically a silico-aluminate and is commonly extended to other compositions leading to a uniform three-dimensional structure, especially to a metallosilicate such as for example an aluminosilicate, a borosilicate, a ferro-silicate, silicate, a titano-silicate, an alumino-silicate, a gallo-phosphate, or a silicoaluminophosphate.
- the zeolites used to dehydrate ethanol preferably have a pore size of the order of 3 ⁇ in diameter and are in the form of beads or rods. This opening is too small to pass the ethanol whose diameter is of the order of 4.4 A.
- the water molecules have a diameter of the order of 2.8 A and can therefore penetrate in the pores of the zeolite and adsorb.
- zeolites can be used: SILIPORITE® products from CECA or SYLOBEAD® products from GRACE Davison.
- the adsorbent molecular sieve may also be a silica.
- the molecular sieves are placed in columns whose operation is intermittent and comprises two phases:
- an adsorption phase during which the mixture in liquid or vapor form passes through the column loaded with molecular sieves.
- a liquid or a vapor freed from the body retained by the molecular sieve is recovered at the outlet.
- This first phase is stopped when the adsorbent is saturated.
- the adsorption is in the liquid phase.
- TSA temperature difference regeneration
- PSA pressure swing adsorption
- vapor phase adsorption is generally preferred
- pressure differential regeneration is the generally selected desorption mode.
- the TSA method requires the use of a neutral purge gas, long regeneration sequences and also problems of degradation of the solid generated by thermal cycles (expansion-contraction).
- a description of this type of method of dehydration of alcohol by PSA-type molecular sieve adsorption is given, for example, in FR 2,719,039-B1.
- This method of vapor phase adsorption on a molecular sieve requires the prior vaporization of the alcohol or the mixture of alcohols.
- the capacity that has captured the water is evacuated.
- a mode of drying the hydrocarbon phase, enriched in alcohol or mixture of alcohols, by adsorption can be advantageously achieved by circulating in a column filled with adsorbent dry fuel base, not containing no alcohol, coming directly from its production unit, possibly reheated or cooled.
- the drying step of the hydrocarbon phase containing the alcohol or the mixture of alcohols and water can also be carried out by pervaporation on a membrane.
- This technology is based on the selective transfer of water through a selective layer associated with a vaporization of water at the downstream face of the membrane. This vaporization is induced by evacuation of the compartment downstream of the membrane associated with a condensation of the water vapor thus produced at a cold point.
- the density of water flow is directly proportional to the difference in water vapor pressure between the two faces of the membrane.
- the water vapor pressure upstream of the membrane (charge side) is a function of the composition of the charge and the temperature of said charge.
- the partial water pressure downstream of the membrane is generally dependent on the level of cold applied at the condenser, the pressure losses in the steam circuit. This technology is particularly advantageous because the energy required for the separation is reduced only to the enthalpy of vaporization of the water downstream of the membrane.
- membranes based on zeolites A or T marketed by the Japanese company Mitsui Engineering & Shipbuilding. These membrane materials whose synthesis is described in US Patents 5,554,286 and US 6,159,542 are the preferred option of the present invention. These membranes are indeed known to offer a very high selectivity water / ethanol, of the order of 30000. In addition, it has been shown that these membranes can be operated for a long time at high temperatures, of the order of 11O 0 C or 120 ° C. (Morigami et al., Separation and Purification Technology 25 (2001) 251-260).
- the Mitsui membrane has shown a capacity to dehydrate industrial ethanol loads containing about 8% water up to water levels of the order of 0.05%.
- An industrial unit of ultimate ethanol dehydration located in Karya in Japan and based on the same type of membrane reduces the water content of this alcohol from 10% to 0.2% (mass fraction).
- This unit can treat 600 L / h of load with a useful membrane surface of 60 m 2 .
- membrane materials based on hydrophilic vitreous polymers have also been tested on a pilot scale for the dehydration of solvents and may advantageously be used for the present invention: polyimides (Huang et al., J.Appl.polymer Sci., 85 (2002) 139-152), or polymer blends comprising polyimides (Cranford et al., J. of Membrane Sci., 155 (1999) 231-240), cellulose acetate, polysulfones or polyethersulfones.
- Membrane materials based on microporous silica for example as described in J. of Membrane Science 254 (2005) 267-274, may also be used.
- the fuel base is enriched in alcohol or mixture of alcohols and can be mixed with other cuts to form a marketable fuel. It is however necessary that the residual water content in the final gasoline is sufficiently low not to generate demixing on storage.
- the extract is subjected to cooling allowing demixtion of an aqueous phase containing alcohol and can be recycled in the extraction column.
- the stress related to the residual water content in the final gasoline must be taken into account during the drying step and / or during the incorporation of stabilizing additives.
- the drying step can be optionally supplemented by the addition of oxygenated compounds to the fuel base enriched in alcohol or mixture of alcohols.
- oxygenated compounds are identical to those that can be added to the fuel base to improve the efficiency of liquid-liquid extraction.
- ethers for example ETBE (ethyltertiobutylether), MTBE (methyltertiobutylether), TAEE (tert-amylethylether), TAME (tert-amylmethylether), DIPE (diisopropylether), C7ethers such as MEPEME ( 2-methyl-2-methoxypentane) or DIMEBU (2,3-dimethyl-2-methoxybutane), PTBE (n-propyl tert-butyl ether), IPTBE (isopropyltertiobutyl ether), DPE (dipropyl ether), or
- alcohols for example butanol, TBA (terbutyl alcohol), IPA (isopropyl alcohol), isobutyl alcohol and / or methanol.
- FIG. 1 represents one embodiment of the method according to the present invention:
- the aqueous phase containing the alcohol or the mixture of alcohols is introduced through the conduit 1 into an exchanger E1, to be brought to the extraction temperature. It is then sent through line 2 to the extractor B1.
- the hydrocarbon phase that is to say the fuel base, is introduced against the current of the aqueous phase in the same apparatus via line 4. previously in the exchanger E2 through line 3 to be brought to the extraction temperature.
- the temperatures of the two phases may be different from each other.
- the fuel base may advantageously make it possible to heat the aqueous solution.
- the extractor contains devices for promoting the dispersion and contact of the aqueous and hydrocarbon phases, as well as the exchange of material between these two phases. Numerous countercurrent extraction technologies can thus be potentially used to operate the extraction: battery of mixer settlers, centrifuges, column (or series of columns) with gravity flow. In the latter case, the column may be empty (spray column) or preferably equipped with perforated tray type internals, disks and crowned, trays spillways. The column may be agitated by pulsation of the liquid or internals, or preferably by rotary mechanical agitation. The columns can also be filled with various loose or structured packings.
- the extract contains the majority of the hydrocarbons, a significant part of the alcohol extracted from the aqueous phase and a part of the water coming from this same aqueous phase. It leaves the extractor via line 5 to be sent to the drying step.
- the raffinate of which the majority compound is water also contains traces of hydrocarbons and the remainder of alcohol that has not been extracted. It is sent via line 6 to a water treatment or recycled for example in the biomass fermentation process.
- the drying step will produce water leaving via the conduit 8 to a treatment of water or to recycling for example to the alcoholic fermentation process and the dried hydrocarbon phase containing the extracted alcohol exiting through the conduit 7. This hydrocarbon phase is sent to the fuel pool of the refinery.
- an oxygenated compound is added to the fuel base to promote the extraction
- the compound is mixed with the latter before entering the extraction apparatus, it is possible that a part of this compound is extracted by the aqueous phase, because of its partial or total solubility in water.
- one solution is to introduce the oxygenated compound added to an intermediate height in the extraction column. A counter extraction is thus carried out between the aqueous phase enriched in oxygenated compound and the fuel base.
- the apparatus B1 described here is an extraction column fed at the top by the aqueous solution containing the alcohol or the mixture of alcohols 2, at the bottom by the fuel base. 4, and using an intermediate feed 9 for the oxygenated compound or the mixture of oxygenated compounds.
- aqueous raffinate 6 At the bottom of the column is the aqueous raffinate 6 and at the top the extract 5 enriched in alcohol and oxygenated compound (s).
- the intermediate feed will preferably be located sufficiently far from the foot of the column so that at least one theoretical extraction stage separates the output of the raffinate.
- FIG. 3 Another particular embodiment is shown diagrammatically in FIG. 3. It consists in carrying out the liquid-liquid extraction in an enclosure B1 between the fuel base 4 and the aqueous solution containing the alcohol or the mixture of alcohols 2.
- the raffinate Impoverished in alcohol 6 comes out at the bottom of extraction column, while extract 5 comes out in the lead.
- the latter is cooled in a tank B3 at a temperature sufficiently cold to cause the demixing of an aqueous phase containing alcohol. This can be recycled in the extraction column.
- An oxygenated additive 11 to limit the demixing is then added to the partially dried extract.
- the cup can then be stored in a tray B4 at a colder temperature than that of the tray B3, without the risk of formation of an aqueous phase.
- the minimum temperature of the tank depends both on the nature of the additive, the amount added, and the composition of the cutaway tray B3 (including water and alcohol content). This implementation is particularly interesting because it does not in principle require any additional drying operation. It is therefore very economical compared to other ways of incorporating alcohol from alcoholic aqueous solutions.
- the implementation of the process according to the invention described in FIG. 4 consists of a particular mode of drying by adsorption in the liquid phase of the fuel base after liquid-liquid extraction.
- the extract 5 corresponding to the alcohol-enriched moist fuel base is dried by passage over a bed of suitable solid (for example zeolite 3A or silica) contained in a column B4.
- suitable solid for example zeolite 3A or silica
- the dry fuel base, containing no alcohol, from the production unit of said fuel base, possibly heated or cooled, is sent through line 4a, in a column in regeneration phase B5.
- the fuel base, then enriched with water, is then sent through line 4 into the liquid-liquid extraction column in which it is charged with alcohol and possibly with water.
- the alcohol-rich dry fuel base is extracted through line 7 to be sent to the fuel pool of the refinery.
- the system operates with at least two columns, one being in the adsorption phase, while the other is in the regeneration phase.
- a preferred implementation of the method consists in having at least two or three columns in regeneration mode and a column in adsorption mode.
- the aqueous phase flow rate is 21400 kg / h.
- the reformate flow is 80000 kg / h
- the aqueous solution and the reformate are brought to the extractor before entering the extractor at a temperature of 150 ° C.
- the drying device B2 is a hydrophilic membrane operating in pervaporation.
- the extractor used is a column type RDC (is provided with a contact system consisting of a vertical axis rotating rotating circular trays) multistage against the current. It has a diameter of 1.9 m, a total height of 9 m, and is composed of 25 compartments.
- the aqueous solution flows up and down in the form of dispersed drops.
- the organic solution or reformate is the continuous phase and flows from bottom to top.
- the number of theoretical stages of extraction is 9.
- the membrane placed downstream of the extraction makes it possible to remove the water contained in the extract to reach a water content in the extract of 0.2% by volume.
- the temperature of the extract at the outlet of the membrane is 113 ° C. In view of the performance of the Mitsui membranes described above, it would be necessary to implement 3770 m 2 to perform such a pervaporation operation at the required dehydration level .
- Cooling the extract from 150 0 C to 113 0 C ensures vaporization of the water contained in the extract on both sides of the membrane.
- the dehydration carried out according to the above conditions makes it possible to avoid the demixing of the mixture at storage temperatures higher than 0 ° C.
- the specifications imposed on the maximum levels of ethanol in gasoline are respected.
- the liquid-liquid extraction is carried out under the same conditions of temperature and pressure as Example 1 with the same reformate as that of Example 1, further containing an oxygenated additive (10% by weight of MTBE) introduced at the bottom of the tube. column.
- Example 1 The liquid-liquid extraction is carried out under the same temperature and pressure conditions as Example 1 with the same reformate as that of Example 1, which also contains an oxygenated additive (10% by weight of MTBE) introduced at intermediate height. , on the 5th compartment from the bottom of a column containing 25.
- an oxygenated additive (10% by weight of MTBE) introduced at intermediate height.
- This example makes it possible to compare the extraction performances obtained by using on the one hand a final gasoline or on the other hand a section of the final gasoline rich in aromatics.
- the liquid-liquid extraction is carried out on the same apparatus and under the same conditions of temperature and pressure as in Example 1 with a mixture composed of 50% by weight of reformate previously used and 50% of isopropanol. octane.
- the mixture used is therefore closer to a final gasoline, especially in terms of aromatic compound content (about 40% by weight).
- the balance of extraction is presented in Table 4.
- Example 1 The extraction of ethanol carried out using a final gasoline is less good than that obtained in Example 1. This illustrates the interest of using a gasoline-rich gasoline cut to carry out the extraction.
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Liquid Carbonaceous Fuels (AREA)
- Preparation Of Compounds By Using Micro-Organisms (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Description
Claims
Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
BRPI0813272-0A BRPI0813272B1 (pt) | 2007-06-27 | 2008-06-26 | Processo de incorporação de álcool em carburantes de elevado teor em compostos aromáticos |
EP08826738A EP2162397A2 (fr) | 2007-06-27 | 2008-06-26 | Procédé d'incorporation d'alcool dans des carburants a forte teneur en composés aromatiques |
US12/666,668 US9309474B2 (en) | 2007-06-27 | 2008-06-26 | Method of incorporating alcohol into fuels having a high aromatic compound content |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0704673 | 2007-06-27 | ||
FR0704673A FR2918071B1 (fr) | 2007-06-27 | 2007-06-27 | Procede d'incorporation d'alcool dans les carburants |
Publications (2)
Publication Number | Publication Date |
---|---|
WO2009016290A2 true WO2009016290A2 (fr) | 2009-02-05 |
WO2009016290A3 WO2009016290A3 (fr) | 2009-04-09 |
Family
ID=38983511
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR2008/000911 WO2009016290A2 (fr) | 2007-06-27 | 2008-06-26 | Procédé d'incorporation d'alcool dans des carburants a forte teneur en composés aromatiques |
Country Status (5)
Country | Link |
---|---|
US (1) | US9309474B2 (fr) |
EP (1) | EP2162397A2 (fr) |
BR (1) | BRPI0813272B1 (fr) |
FR (1) | FR2918071B1 (fr) |
WO (1) | WO2009016290A2 (fr) |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2921385B1 (fr) * | 2007-09-21 | 2010-02-26 | Inst Francais Du Petrole | Procede de transformation de biomasse en produits renfermant des groupements acetals et leur utilisation comme biocarburants |
US9850512B2 (en) | 2013-03-15 | 2017-12-26 | The Research Foundation For The State University Of New York | Hydrolysis of cellulosic fines in primary clarified sludge of paper mills and the addition of a surfactant to increase the yield |
US9951363B2 (en) | 2014-03-14 | 2018-04-24 | The Research Foundation for the State University of New York College of Environmental Science and Forestry | Enzymatic hydrolysis of old corrugated cardboard (OCC) fines from recycled linerboard mill waste rejects |
Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2591672A (en) * | 1949-01-03 | 1952-04-08 | Standard Oil Dev Co | Dehydration of alcohols by gasoline extractive distillation |
US4251231A (en) * | 1979-09-13 | 1981-02-17 | Artisan Industries Inc. | Direct process for the production of gasohol from fermentation mixtures |
US4297172A (en) * | 1980-01-23 | 1981-10-27 | Kansas State University Research Foundation | Low energy process of producing gasoline-ethanol mixtures |
US4441891A (en) * | 1980-12-18 | 1984-04-10 | Biohol Corporation | Gasoline-aided production of alcohol and fuel |
US4445908A (en) * | 1980-12-01 | 1984-05-01 | The United States Of America As Represented By The United States Department Of Energy | Extracting alcohols from aqueous solutions |
US4482768A (en) * | 1983-03-31 | 1984-11-13 | Union Carbide Corporation | Separation of alkanols from aqueous reaction solutions |
US5113024A (en) * | 1991-06-07 | 1992-05-12 | Mobil Oil Corporation | Process for product separation in the production of di-isopropyl ether |
JPH06158064A (ja) * | 1992-11-30 | 1994-06-07 | Mitsubishi Heavy Ind Ltd | ガソホールの製造方法及びその装置 |
GB2293375A (en) * | 1994-09-21 | 1996-03-27 | Texaco Development Corp | Method of recovering ethers and alcohols from wastewater |
-
2007
- 2007-06-27 FR FR0704673A patent/FR2918071B1/fr not_active Expired - Fee Related
-
2008
- 2008-06-26 EP EP08826738A patent/EP2162397A2/fr not_active Withdrawn
- 2008-06-26 BR BRPI0813272-0A patent/BRPI0813272B1/pt not_active IP Right Cessation
- 2008-06-26 WO PCT/FR2008/000911 patent/WO2009016290A2/fr active Application Filing
- 2008-06-26 US US12/666,668 patent/US9309474B2/en not_active Expired - Fee Related
Patent Citations (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2591672A (en) * | 1949-01-03 | 1952-04-08 | Standard Oil Dev Co | Dehydration of alcohols by gasoline extractive distillation |
US4251231A (en) * | 1979-09-13 | 1981-02-17 | Artisan Industries Inc. | Direct process for the production of gasohol from fermentation mixtures |
US4297172A (en) * | 1980-01-23 | 1981-10-27 | Kansas State University Research Foundation | Low energy process of producing gasoline-ethanol mixtures |
US4445908A (en) * | 1980-12-01 | 1984-05-01 | The United States Of America As Represented By The United States Department Of Energy | Extracting alcohols from aqueous solutions |
US4441891A (en) * | 1980-12-18 | 1984-04-10 | Biohol Corporation | Gasoline-aided production of alcohol and fuel |
US4482768A (en) * | 1983-03-31 | 1984-11-13 | Union Carbide Corporation | Separation of alkanols from aqueous reaction solutions |
US5113024A (en) * | 1991-06-07 | 1992-05-12 | Mobil Oil Corporation | Process for product separation in the production of di-isopropyl ether |
JPH06158064A (ja) * | 1992-11-30 | 1994-06-07 | Mitsubishi Heavy Ind Ltd | ガソホールの製造方法及びその装置 |
GB2293375A (en) * | 1994-09-21 | 1996-03-27 | Texaco Development Corp | Method of recovering ethers and alcohols from wastewater |
Also Published As
Publication number | Publication date |
---|---|
WO2009016290A3 (fr) | 2009-04-09 |
BRPI0813272B1 (pt) | 2018-07-10 |
BRPI0813272A8 (pt) | 2018-05-02 |
EP2162397A2 (fr) | 2010-03-17 |
US9309474B2 (en) | 2016-04-12 |
FR2918071B1 (fr) | 2010-10-22 |
BRPI0813272A2 (pt) | 2014-12-30 |
FR2918071A1 (fr) | 2009-01-02 |
US20100263264A1 (en) | 2010-10-21 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
EP0652194B1 (fr) | Procédé de séparation des composés oxygénés d'hydrocarbures, combinant une distillation et une perméation et son utilisation en éthérification | |
EP1616853A1 (fr) | Procédé de production d'esters alkyliques d'acides gras et de glycérol de haute pureté | |
EP2445614B1 (fr) | Procede de traitement de gaz acides | |
CA2671389C (fr) | Procede de purification par adsorption d'hydrogene avec cogeneration d'un flux de co2 en pression | |
EP0783031B1 (fr) | Procédé de déshydratation, de désacidification et de dégazolinage d'un gaz naturel, utilisant un mélange de solvants | |
EP3194350B1 (fr) | Procede de production de butadiene a partir d'ethanol en une etape reactionnelle a faible consommation en eau et en energie | |
EP1120149A1 (fr) | Procédé de purification d'un gaz par adsorption des impuretés sur plusieurs charbons actifs | |
WO2009106706A1 (fr) | Procede de separation du propane et du propylene mettant en oeuvre une colonne a distiller et une unite deseparation par membrane | |
EP1476244A1 (fr) | Procede de traitement d'un melange gazeux comprenant de l'hydrogene et du sulfure d'hydrogene | |
EP1442784A1 (fr) | Membrane inorganique poreuse contenant du carbone, son procédé de préparation et son utilisation | |
FR2922547A1 (fr) | Procede de separation d'aromatiques en c8 avec recyclage limite | |
WO2009016290A2 (fr) | Procédé d'incorporation d'alcool dans des carburants a forte teneur en composés aromatiques | |
EP3643394B1 (fr) | Procédé de déshydratation d'un gaz hydrocarbone | |
EP0675099B1 (fr) | Procédé de purification de l'éthyl tertio butyl éther combinant un procédé à membrane et une distillation | |
EP3727648B1 (fr) | Procédé de distillation d'un courant gazeux contenant de l'oxygène | |
FR2782714A1 (fr) | Procede de coproduction de metaxylene et de paraxylene | |
EP0129459B1 (fr) | Procédé de purification d'un mélange eau-alcool en C1-C2-impuretés, issu d'un procédé de fabrication industriel d'alcool en C1-C2 au moyen d'un agent d'extraction | |
EP3875876A1 (fr) | Procédé et appareil de distillation adsorptive pour la séparation cryogénique argon-oxygène | |
EP1165728A1 (fr) | Procede de traitement d'une huile utilisant un fluide a l'etat supercritique | |
EP1138377A1 (fr) | Méthode de séparation de molecules en phase gazeuse par adsorption au moyen d'adsorbants inorganiques solides agglomérés à distribution mésoporeuse étroite et calibrée | |
EP2202288A1 (fr) | Procédé de fabrication d'esters alkyliques à partir d'huile végétale ou animale et d'un monoalcool aliphatique utilisant une séparation membranaire | |
FR2779069A1 (fr) | Procede d'adsorption et de desorption d'un solvant contenu dans un gaz naturel issu d'un procede de deshydratation | |
EP3768410A1 (fr) | Procédé de décarbonatation de flux gazeux | |
WO2013088339A2 (fr) | Stripage sélectif au gaz d'une phase volatile contenue dans une émulsion dont la phase continue est moins volatile | |
BE608005A (fr) |
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: 08826738 Country of ref document: EP Kind code of ref document: A2 |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2008826738 Country of ref document: EP |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
WWE | Wipo information: entry into national phase |
Ref document number: 12666668 Country of ref document: US |
|
ENP | Entry into the national phase |
Ref document number: PI0813272 Country of ref document: BR Kind code of ref document: A2 Effective date: 20091224 |