SE2151091A1 - Method for producing motor fuel from ethanol - Google Patents

Method for producing motor fuel from ethanol

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Publication number
SE2151091A1
SE2151091A1 SE2151091A SE2151091A SE2151091A1 SE 2151091 A1 SE2151091 A1 SE 2151091A1 SE 2151091 A SE2151091 A SE 2151091A SE 2151091 A SE2151091 A SE 2151091A SE 2151091 A1 SE2151091 A1 SE 2151091A1
Authority
SE
Sweden
Prior art keywords
mixture
alcohols
ethanol
catalyst
olefins
Prior art date
Application number
SE2151091A
Other languages
Swedish (sv)
Other versions
SE544831C2 (en
Inventor
Igor Golubkov
Original Assignee
Swedish Biofuels Ab
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 Swedish Biofuels Ab filed Critical Swedish Biofuels Ab
Priority to SE2151091A priority Critical patent/SE2151091A1/en
Priority to IL311105A priority patent/IL311105A/en
Priority to PCT/SE2022/050676 priority patent/WO2023033692A1/en
Priority to CA3230067A priority patent/CA3230067A1/en
Priority to AU2022340452A priority patent/AU2022340452A1/en
Publication of SE544831C2 publication Critical patent/SE544831C2/en
Publication of SE2151091A1 publication Critical patent/SE2151091A1/en
Priority to CONC2024/0002849A priority patent/CO2024002849A2/en

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    • 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
    • C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
    • 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
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/02—Boron or aluminium; Oxides or hydroxides thereof
    • 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
    • B01J21/00—Catalysts comprising the elements, oxides, or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium, or hafnium
    • B01J21/10—Magnesium; Oxides or hydroxides thereof
    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/06—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of zinc, cadmium or mercury
    • 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
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/10—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00 of rare earths
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C1/00—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon
    • C07C1/20—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms
    • 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
    • C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
    • C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
    • C07C29/143—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of ketones
    • C07C29/145—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of ketones with hydrogen or hydrogen-containing gases
    • 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
    • C07C29/60—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by elimination of -OH groups, e.g. by dehydration
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    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C47/00—Compounds having —CHO groups
    • C07C47/02—Saturated compounds having —CHO groups bound to acyclic carbon atoms or to hydrogen
    • C07C47/06—Acetaldehyde
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    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
    • C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
    • 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
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
    • C07C2/02—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons
    • C07C2/04—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation
    • C07C2/06—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition between unsaturated hydrocarbons by oligomerisation of well-defined unsaturated hydrocarbons without ring formation of alkenes, i.e. acyclic hydrocarbons having only one carbon-to-carbon double bond
    • 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
    • C07C29/132—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group
    • C07C29/136—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH
    • C07C29/14—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group
    • C07C29/141—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring by reduction of an oxygen containing functional group of >C=O containing groups, e.g. —COOH of a —CHO group with hydrogen or hydrogen-containing gases
    • 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
    • C07C29/36—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by reactions with formation of hydroxy groups, which may occur via intermediates being derivatives of hydroxy, e.g. O-metal
    • C07C29/38—Preparation of compounds having hydroxy or O-metal groups bound to a carbon atom not belonging to a six-membered aromatic ring increasing the number of carbon atoms by reactions with formation of hydroxy groups, which may occur via intermediates being derivatives of hydroxy, e.g. O-metal by reaction with aldehydes or ketones
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C45/00—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds
    • C07C45/49—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide
    • C07C45/50—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by reaction with carbon monoxide by oxo-reactions
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C47/00—Compounds having —CHO groups
    • C07C47/02—Saturated compounds having —CHO groups bound to acyclic carbon atoms or to hydrogen
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/02—Gasoline
    • 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/04—Diesel 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
    • C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
    • C10G2400/08—Jet fuel
    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/02—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds to eliminate hetero atoms without changing the skeleton of the hydrocarbon involved and without cracking into lower boiling hydrocarbons; Hydrofinishing
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    • 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
    • C10G45/00—Refining of hydrocarbon oils using hydrogen or hydrogen-generating compounds
    • C10G45/32—Selective hydrogenation of the diolefin or acetylene compounds
    • 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
    • C10G50/00—Production of liquid hydrocarbon mixtures from lower carbon number hydrocarbons, e.g. by oligomerisation
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P30/00—Technologies relating to oil refining and petrochemical industry
    • Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock

Abstract

A method is for producing motor fuel, and more particularly gasoline, kerosene, and diesel, from ethanol is disclosed. The ethanol is suitably obtained from a feedstock of mainly plant origin. In addition, intermediate products and by-products from the inventive motor fuel synthesis, e.g. alcohols, aldehydes, ketones, ethers, olefins, paraffins, and aromatic compounds can be obtained using the method.

Description

METHOD FOR PRODUCING MOTOR FUEL FROM ETHANOL Field of the invention The present invention relates to a method for producing motor fuel, and more particu- larly gasoline, kerosene, and diesel, from ethanol obtained from a feedstock of mainly plant origin. ln addition, intermediate products and by-products from the inventive mo- tor fuel synthesis, that is; alcohols, aldehydes, ketones, ethers, olefins, paraffins and aromatic compounds obtained from feedstock of mainly plant origin, can be used not only in the chemical industry to produce paints or polymers, but also in the pharmaceu- tical industry, or for the manufacture of cosmetic products.
State of the art The rapid growth in the consumption of motor fuel, on the one hand resulting in a sig- nificant reduction of oil and gas reserves of our planet, and on the other hand, raising concerns of society regarding deterioration of the environment, stimulates the search for alternative motor fuels. The challenges facing modern industry concerning reducing carbon dioxide emissions to the atmosphere, stimulate research to improve existing methods and create new ones for the manufacture of motor fuel from renewable feed- stocks. Currently, the most attractive raw material for the manufacture of alternative motor fuels is biomass, which is produced directly from the carbon dioxide constantly coming to the atmosphere. Recently, a significant number of works have appeared on the methods of processing biomass into motor fuel and, first of all, on the methods of producing kerosene from raw materials of biological origin.
US 8193402 B2, US 8373012 B2, and US 8487149 B2 disclose microorganisms that, by means of fermentation, provide for conversion of carbohydrates isolated from plant biomass both into individual Cz-Cß alcohols, and into a mixture of Cz-Cß alcohols. The alcohols obtained, in turn, are dehydrated into the corresponding olefins. The Cz-Cß olefins obtained both as individual olefins and as mixtures, are oligomerized, yielding Cß-Czi olefins. Then, the Cß-Czi olefins obtained are hydrogenated resulting in a prod- uct containing one or a few saturated Cß-Cm alkanes.
WO 2018071905 and US 2020010767 A1 disclose methods and materials for oli- gomerization of lower olefins, for example Cz-Cs olefins, into transport fuels, including diesel and/orjet fuel. ln some embodiments, tungsten zirconium catalysts are used to perform the oligomerization.
US 10633320 B2 proposes a process for converting crude and/or refined fusel oil mix- tures into renewable chemicals of a higher value by means of mixed oxide metal or ze- olite catalysts. The patent discloses methods of directing a vaporized stream of crude and/or refined fusel oils through various mixed metal oxide catalysts, metal doped zeo- lites or non-metal doped zeolites, and/or metal oxides, obtaining products of higher value. The renewable chemicals produced using these catalysts include methyl isobu- tyl ketone (MIBK), diisobutyl ketone (DIBK), isoamylene, and isoprene.
US 2011245542 A1 discloses synthesis of liquid fuels from oxygenated hydrocarbons. Processes and reactor systems for converting oxygen-containing hydrocarbons into hydrocarbons, ketones and alcohols used as liquid fuels such as gasoline, jet fuel or diesel fuel, and industrial chemicals are provided. The process comprises conversion of mono-oxygenated hydrocarbons such as alcohols, ketones, aldehydes, furans, car- boxylic acids, diols, triols and/or other polyols to C4+ hydrocarbons, alcohols and/or ke- tones by condensation. Oxidized hydrocarbons can originate from any source, but the preferred ones are those derived from biomass. The teaching of the patent differs in the way that there is a catalytic interaction of the oxygenate in the vapor phase with hy- drogen in the presence of a basic condensation catalyst containing a component se- lected from the group consisting of Li, Na, K, Cs, B, Rb, Mg, Ca, Sr, Si, Ba, Al, Zn, Ce, La, Y, Sc, Y, Zr, Ti, hydrotalcite, phosphate, base treated aluminosilicate zeolite, zinc aluminate, base resin, base nitride, alloys or combinations thereof, at condensation temperatures ranging from about 80°C to 500°C and a condensation pressure of at least 0.1 atm, to obtain a C4+ compound, where the C4+ compound includes a member selected from the group consisting of C4+ alcohol, C4+ ketone, C4+ alkane, C4+ alkene, Cs + cycloalkane, G5 + cycloalkene, aryl, condensed aryl, and mixtures thereof.
Furthermore, US 2012198760 A1 and US 9228134 B1 disclose a method and systems for producing distillate fuel from biomass. The invention disclosed therein provides methods, reactor systems and catalysts for converting biomass derived feedstock to Cs + hydrocarbons using heterogeneous catalysts. The product stream can be separated and further processed for use in the chemical industry, or as a clean fuel, or as a mix- ing component for aviation and diesel fuels, or as heavy oils for lubricants and/or liquid fuels.
US 9771533 B2 and US 9932531 B2 disclose systems and processes for the conver- sion of ethylene feedstocks into hydrocarbon fuels. Systems, processes, and catalysts for producing fuels and fuel mixtures containing selected ratios of open and closed chain fuel range hydrocarbons suitable for the production of alternative fuels, including gasolines, jet fuels, and diesel fuels are disclosed. Fuel range hydrocarbons can be produced from feedstocks containing ethylene and ethanol.
US 2020165176 A1 discloses a method for converting ethanol into 1-butene and 2-bu- tene in a single reactor. The document describes simplified processes for producing chemicals in demand, such as butenes, from feedstocks containing ethanol. ln one set of embodiments, this is accomplished in one step where the gas phase ethanol feed is passed over an acidic metal oxide catalyst having a transition metal dispersion of at least 5% on a metal oxide support. The ethanol content in the feed mix can range from 10% to 100% of the feed, and where it is not related to food, the feed ethanol can con- tain water. The method for the production of butene from a feedstock containing etha- nol in one stage is disclosed. The method includes the stage of passing the feedstock containing ethanol in the gas phase over a catalyst 4 wt.% Ag / 4 wt.% ZrOz / SiOz- SBA-16 having a dispersion of the transition metal Ag of not less than 30%, at a tem- perature of 325°C, a pressure of 7 bar and a flow rate of 0.23 h* in the presence of a hydrogen carrier for the direct formation of butenes, with a selectivity equal to or larger than 13% of ethanol, wherein a relatively weak hydrogenation ability of Ag and weakly acidic materials of the carrier provides for maintaining it unchanged.
US 2013144094 A1, US 2013219778 A1, and US 2013237728 A1 disclose methods for direct conversion of oxygenates derived from biomass into hydrocarbons with a longer chain. The longer chain hydrocarbons are characterized by a higher content of naphthenes, which is very useful in distillate range fuels, or more specifically jet and diesel range fuels. Naphthenes help the biomass-derived hydrocarbons meet jet and diesel product specifications while really helping cold flow properties. One of the em- bodiments describes the hydrotreating processes providing for selective conversion of glycols into monoalcohols that can be blended as biofuels. The NiMo and CoMo cata- lysts are active in the reaction and the reaction conditions can also affect the selectivity of the monoalcohols. Oxygenate feedstocks derived from biomass are converted into a variety of fuels, including the hydrocarbons of gasoline, jet and diesel fuels. General methods are proposed including hydrolysis, dehydration, condensation, oligomeriza- tion, and hydrogenation.
US 2015376511 A1 and US 2016108323 A1 provide a method for producing jet fuel hydrocarbons from alcohols derived from cellulose and hemicellulose, such as pen- tanediol and hydroxymethyl tetrahydrofuran, which is also known as tetrahydrofurfuryl alcohol. Alcohols are spliced or dimerized using the Guerbet synthesis, in which longer chain organic molecules are formed using a heterogeneous alcohol condensation cata- lyst. Also disclosed is a method for converting molecules containing one or more func- tional groups of alcohol into larger molecules. Alcohols such as methanol, ethanol, pro- panol and hexanol, and diols/glycols such as propylene glycol and butanediol are fed to a supported metal catalyst, such as a noble metal or solid acid catalyst in the pres- ence of hydrogen at elevated temperatures and pressures, yielding a mixture of hydro- carbon and oxygenate products.
US 8049048 B2 discloses renewable engine fuels. The disclosure provides a renewa- ble engine fuel derived completely from biomass sources. One of the embodiments discloses fully renewable motor fuel comprised of one or more low carbon ethers, one or more furans, pentosan derivatives, one or more aromatic hydrocarbons, one or more C4-C10 straight chain alkanes derivable from polysaccharides and one or more bio-oils. ln addition, the fuel may contain triethanolamine. Such a lower octane renewa- ble fuel may be utilized in, for example, automobile fuel, 100 LL aviation fuel, and tur- bine engines. These fully renewable ethanol fuels can have a wide range of octane numbers and energies and can be effectively used to replace 100 LL aviation fuel (known as AvGas), as well as high octane, rocket, diesel and gas turbine fuel. ln an- other embodiment, there is provided a synthetic, high octane aviation fuel containing isopentane and mesitylene and a process of producing the same from a biomass.
CA 2800057 A1 and US 8852296 B2 disclose renewable engine fuel and a method of producing the same. A non-petroleum, high octane fuel obtained from biomass sources and a method for its production are disclosed. The production method in- cludes the reduction of the biomass feedstock to sugars, the fermentation of sugars using microorganisms or their mutagens to produce ethanol or acetic acid, the conver- sion of acetic acid or ethanol to acetone and the conversion of acetone to mesitylene and isopentane, the main components of the engine fuel. Trimerization of acetone can be carried out in the presence of a catalyst containing at least one metal selected from a group consisting of niobium, iron and manganese. The ethanol can be converted to mesitylene in a dehydration reaction in the presence of a catalyst of zinc oxide or cal- cium oxide, and unreacted ethanol and water separated from mesitylene by distillation. These fuels based on ethanol are renewable and may be formulated to have a wide range of octane values and energy, and may effectively be used to replace 100LL avi- ation fuel (known as AvGas), as well as high octane, rocket, diesel, turbine engine fuels, as well as two-cycle, spark ignition engine fuels. Ethanol can be converted to mesitylene in a dehydration reaction in the presence of a zinc oxide or calcium oxide catalyst, and unreacted ethanol and water are separated from mesitylene by distilla- tion. These ethanol fuels based on biomass are fully renewable, can have a wide range of octane numbers and energies, and can be effectively used to replace 100 LL aviation fuel (known as AvGas), as well as high octane, rocket, diesel, gas turbine fuel, and also fuel for tvvo stroke, spark ignition engines.
US 9447347 B2 teaches production of biofuels via hydrogenolysis condensation. The method disclosed comprises a providing a carbohydrate; reacting the carbohydrate di- rectly with hydrogen in the presence of a hydrogenolysis catalyst to produce a reaction product comprising a polyol; and then processing at least a portion of the reaction product to form a fuel blend.
US 2012156742 A1 teaches a process to produce biofuels from biomass. The docu- ment teaches a method to produce biofuels from biomass by contacting the biomass with an aqueous media to form an extracted biomass, separating at least a portion of an aqueous liquor from the extracted biomass thereby providing the aqueous liquor stream comprising soluble carbohydrates; contacting the aqueous liquor stream with a purification substrate effective for removing sulfur compounds and nitrogen com- pounds thereby producing a treated carbohydrate stream having less than 35% of the sulfur content and less than 35% of the nitrogen content of the untreated aqueous liq- uor feed, based on the untreated aqueous Iiquor stream, then contacting the treated carbohydrate stream with an aqueous phase reforming catalyst to form a plurality of oxygenated intermediates; and processing at least a portion of the oxygenated inter- mediates to form a liquid fuel.
US 9862655 B2 discloses a method and systems for producing jet range hydrocar- bons. Methods and systems for producing jet range hydrocarbons are disclosed. ln an illustrative embodiment, a process for producing jet range hydrocarbons comprises the steps of combining a first stream of G4 olefinic hydrocarbons and a second stream of Cs-Cs olefinic hydrocarbons to produce a third stream of C4-C8 hydrocarbons, oli- gomerizing the third stream of C4-C8 olefinic hydrocarbons to produce a fourth stream of 64-620 olefinic hydrocarbons and separating Cs-Cß hydrocarbons from the fourth stream of C4-C20 olefinic hydrocarbons to produce a second stream of Cs-Cs olefinic hydrocarbons and a fifth stream of olefinic hydrocarbons CQ-Czo. The method further includes the step of hydrogenating a fifth stream of Cg-Czo olefinic hydrocarbons to pro- duce a sixth stream of Cg-Czo paraffinic hydrocarbons of the jet fuel range.
US 2016312131 A1, US 2016312134 A1 provide a process for producing jet-range hy- drocarbons. The disclosed therein for producing hydrocarbons suitable forjet fuel, in- cludes passing a renewable olefin feedstock comprising Cs to Cs olefins to an oli- gomerization reactor containing a zeolite catalyst to produce an oligomerized effluent, separating the oligomerized effluent into at least a light stream, and a heavy olefin stream. At least a first portion of the heavy olefin stream is recycled to the oligomeriza- tion reactor to dilute the renewable olefin feedstock. A portion of the heavy olefin stream may be hydrogenated and separated to provide a hydrocarbon product suitable forjet fuel. Also disclosed are methods and systems for producing jet-range hydrocar- bons. ln an illustrative embodiment, a process for producing jet-range hydrocarbons includes the steps of combining a first stream containing G4 olefinic hydrocarbons and a second stream containing Cs-Cs olefinic hydrocarbons to produce a third stream con- taining C4-C8 hydrocarbons. A step for oligomerizing a third stream containing C4-C8 olefinic hydrocarbons to produce a fourth stream containing C4-C2o olefinic hydrocar- bons. Cs-Cß hydrocarbons separated from the fourth stream containing C4-C2o olefinic hydrocarbons, are sent to the second stream, obtaining a fifth stream containing ole- finic hydrocarbons Cg-Czo. The method further includes the step of hydrogenating a fifth stream containing Cg-Czo olefinic hydrocarbons to obtain a sixth stream containing 69-620 paraffinic hydrocarbons in the jet fuel range.
US 2010146843 A1 and US 2011126448 A1 disc|ose a process, plant, and biofuel for integrated biofuel production. This invention relates to a process, a plant, and a biofuel for integrated biofuel production, such as with butanol, biodiesel, and sugar products. The integrated process includes the step of removing hexose from a feedstock to form a lignocellulosic material. The process also includes the step of converting the hexose to butanol and/or a biodiesel fuel, and the step of depolymerizing lignocellulosic mate- rial to form pentose and a residue. The process also includes the step of converting the pentose to butanol and/or a biodiesel material. The process also includes the step of converting pentose to biogasoline and/or biodiesel fuel.
WO 2014154799 discloses production of middle distillate hydrocarbon composition. A process for the preparation of a middle distillate hydrocarbon composition from eth- ylene is claimed, wherein said process comprises the following steps: (a) feeding an ethylene composition in to an oligomerisation reaction zone containing a supported nickel oligomerisation catalyst to form an oligomerisation product A, wherein the oligo- merisation reaction is operated at a temperature in the range of 30 to 300°C and a pressure of at least 10 bar; (b) separating a light products stream B, a middle distillate product stream C and a heavy products stream D from oligomerisation product A, wherein the light product stream B comprises the fraction of oligomerisation product A, which boils in the Cz-Cs mono-olefin boiling range and a middle distillate product stream C comprising a fraction of oligomerisation product A, which boils above the boiling range of the light product stream B and below the boiling range of the heavy products stream D, and wherein the heavy product stream D comprises the fraction of oligomerisation product A, which boils above the C22 mono-olefin boiling range; (c) re- cycling a portion of the light products stream B to the oligomerisation reaction zone of step (a) of the process; (d) feeding the heavy product stream D and a portion of the light products stream B in to an olefin metathesis reaction zone to produce a metathe- sis product stream E; (e) separating a middle distillate product F from the metathesis product stream E; and (f) hydrogenating the middle distillate product stream C, wherein the middle distillate hydrocarbon composition comprises at least a portion of the hydro- genated middle distillate product stream C and at least a portion of the middle distillate product F.
EP 2285972 A2 teaches a method for treating biomass by irradiation with an electron beam to obtain useful products, including fuel. Plant biomass, animal biomass and ur- ban waste biomass exposed to electron beam irradiation are processed to produce useful products. Cellulosic and lignocellulosic materials, as well as materials containing starch or sugar, can be used as feedstock in the claimed method for processing bio- mass. The irradiated biomass is used to produce ethanol and butanol by fermentation.
WO 2019084518 A1 and US 2019233751 A1 teach a method of preparing cellulosic ethanol having 100% biogenic carbon content as determined by ASTM 6866-18, which includes treating ground corn cobs with electron beam radiation and saccharifying the irradiated ground corn cob to produce sugars. The method also includes fermenting the sugars with a microorganism. The disclosures describe an unblended gasoline de- rived from cellulosic biomass with a research octane number higher than about 87 as determined by ASTM D2699. At the same time, it is indicated that the unblended gaso- line is obtained as a result of catalytic treatment of ethanol obtained from cellulosic bio- mass. ln addition, a jet fuel derived from cellulosic biomass comprising about 25% of aromatic hydrocarbons, about 2.5% of alkenes, about 41% of alkanes, and about 8.5% of oxygenated compounds (wt./wt.) is disclosed.
US 2012271081 A1 discloses a method for the production of C10+ hydrocarbons from heteroatomic organic compounds. The invention relates to a method for producing C10 + hydrocarbons from heteroatomic organic compounds comprising at least one het- eroatom chosen from oxygen, sulfur and halogen, alone or in combination. The method for producing a distillate from organic raw materials containing at least one heteroatom includes the first step of converting the starting organic compounds into olefins. At the second step of conversion, the olefins are oligomerized in the presence of at least 0.5% by weight of oxygen-containing compounds. By virtue of the presence of oxygenates during the oligomerization, this process makes it possible to improve the yield of distillate.
Furthermore, US 2012271085 A1 teaches a method for producing a distillate from a hydrocarbon feed, comprising alcohol condensation. The invention relates to a method for oiigomerizing Gs-G10 olefins into a distillate containing G10 + molecules. According to the disclosure, the oligomerization of Gs-G10 olefins in the presence of at least one al- cohol containing at least two carbon atoms provides for the production of G10+ hydro- carbons.
US 9790444 discloses methods to produce fuels. The disclosure generally relates to the production of fuels, and more specifically, to the catalytic conversion of alcohols into hydrocarbon ketones suitable for use as components in fuels. More specifically, the disclosure refers to the catalytic conversion of an isopropanol + butanol + ethanol (IBE) or acetone + butanol + ethanol (ABE) mixture to ketones suitable for use as a fuel. Blends of ABE or IBE can be obtained by fermentation of biomass or sugars. A method for producing a mixture of hydrocarbon ketones, comprising contacting ace- tone and at least two or more primary alcohols with a catalyst and, optionally, a base to obtain a mixture of hydrocarbon ketones, wherein the catalyst comprises: (i) one or more metals, and (ii) hydrotalcite (HT), lanthanum oxide (La2O3), titanium dioxide (TiO2), or magnesium oxide (MgO), or any combination thereof.
US 9914672 B2 teaches a method for converting alcohols to distillate fuels. A process for the production ofjet and other heavy fuels from alcohols and mixture of alcohols is disclosed. The process may include contacting in a reaction zone at least one G2 to G11 alcohol with a solid catalyst having activity for the simultaneous dehydration of the alcohols to form olefins, isomerization of the olefins to form internal olefins, and oli- gomerization of the olefins produced in situ via dehydration to form an effluent com- prising mono-olefinic hydrocarbons. Preferably, the alcohol feed is a mixture of alco- hols, such as G2 to G7 alcohols or G4 and G6 alcohols, enabling the production of a mix- ture of branched hydrocarbons that may be used directly as a jet fuel without blending. The disclosed method for the production ofjet and other heavy fuel comprises: (i) in the reaction zone, bringing a mixture of two or more alcohols from G2 to G11, including at least one secondary alcohol, into contact with a solid catalyst having activity for de- hydrating alcohols to yield olefins and water; (ii) oligomerization of olefins obtained in situ from the dehydration reaction; and (iii) isomerization of the resulting olefin oligo- mers and olefins to yield internal olefins, to obtain monoolefin hydrocarbons. ln addi- tion, it is taught that G2 to C11 alcohols are obtained by biomass fermentation or bio- mass gasification to synthesis gas followed by a modified Fischer-Tropsch synthesis.
US 9688590 B2 teaches production ofjet and other heavy fuels from isobutanol.
US 8329970 B2 teaches a method for the deoxygenation of materials of biological origin. The disclosure relates to a method for the deoxygenation of materials of biologi- cal origin and particularly to the removal of oxygen from organic compounds derived from biomass with carbon monoxide, to yield linear and branched hydrocarbons suita- ble as biofuels or as blending stocks or components for biofuels, such as gas, gaso- line, diesel fuel and aviation fuel, as well as solvents. The method comprises contact- ing a feedstock with carbon monoxide in the presence of a catalyst comprising a metal selected from a group consisting of ruthenium, manganese, rhodium, rhenium, os- mium, iridium, molybdenum, copper, zinc, palladium, platinum and cobalt, in the pres- ence of water, under alkaline conditions at a temperature from 150 to 350°C. and un- der a pressure from 0.1 to 150 bar, to produce hydrocarbons.
WO 2020093127 A1 teaches a process for producing a renewable isoparaffin com- pound, and use of the renewable isoparaffin compound. The claimed invention relates to a process for producing a renewable isoparaffin compound with a high octane rat- ing, comprising a step of Guerbet reaction between an initial G5 alcohol load, obtained from renewable raw material, and methanol to produce a branched renewable Ca alco- hol; dehydration of the branched renewable Cß alcohol into a Cß olefin; and hydrogena- tion of the G6 olefin into renewable isoparaffin. A renewable isoparaffin compound with a high octane rating, comprising at least 50% carbon of renewable natural origin in its composition, and use of said renewable paraffin in gasolines in general and in special high-performance gasolines, such as aviation gasoline, are also described.
Besides the above-mentioned disclosures, the following documents mentioned below have relevance to the claimed invention. 11 There is a number of patent disclosures dealing with hydroformylation of light olefins, including ethylene and propylene.
GB 1086100 teaches a method for producing aldehydes by olefin hydroformylation: ethylene or propylene is reacted with a mixture of carbon monoxide and hydrogen, as well as an inert gas, in the presence of catalysts containing cobalt at a pressure not ex- ceeding 20 MPa and a temperature of 135°C. The hydrogen content in the total amount of gas in the reactor is 30 to 45 mol.%, and the inert gas is 5 to 15 mol.%. Me- thane, ethane or nitrogen can be used as the inert gas. ln the disclosed hydroformyla- tion process, standard cobalt-containing hydroformylation catalysts such as cobalt ace- tate, cobalt oxide, cobalt naphthenate, cobalt formate, cobalt carbonyl or hydrocar- bonyl, cobalt oleate and cobalt carbonate can be used.
JP 2006160746 discloses a method of hydroformylation, characterized by the addition of an aldehyde to the synthesis stage. The implementation of hydroformylation using an unmodified cobalt complex for a catalyst, as well as the presence of aldehydes in the feedstock, increases the selectivity of the formation of the target product in the range from 0.5 to 20 mol%. The method relates to the hydroformylation of olefins hav- ing from 7 to 25 carbon atoms.
CN 1168129 discloses a method providing for hydroformylation of a hydrocarbon stream comprising a stream containing 27.5 to 75 wt. % ethylene and a total content of olefin up to 80 wt. % based on the total hydrocarbon content. Then, in the presence of a rhodium-containing catalyst, it is contacted with synthesis gas, and the hydroformyla- tion product is recovered. The catalyst was prepared in a 500 ml autoclave equipped with a continuous gas supply system with back pressure control. 201 g of tetraglyme, 15.6 g of triphenylphosphine and 0.70 mg of rhodium were mixed under nitrogen. The catalyst solution was transferred to the autoclave under nitrogen, and the autoclave was purged with nitrogen, and then the gas stream was introduced into the boiler as indicated in Table 1. Then the pressure was set to 1000 kPa (absolute pressure) and the back pressure control was turned on, after which the autoclave and its contents were heated up to 100°C. At a catalyst content of 85 ppm, the conversion of olefins in the hydroformylation reaction reached 65%. 12 CN 101768062 A teaches a hydroformylation process using a water-soluble complex based on rhodium phosphine. The process is carried out in a static mixing reactor and involves the simultaneous formation of propanal and butanal. The invention is a contin- uous process, the aqueous catalyst solution is recirculated by a pump, the space ve- locity of the aqueous catalyst solution in the static mixing reactor is from 0.2 to 1.2 m/s. The residence time of the reaction liquid in the circulation tank is 10-20 seconds. The molar ratio of olefin to hydrogen gas and carbon monoxide in the feed mixture is from 1:(1.0-1.1):(1.0-1.1). The reaction pressure of the hydroformylation is from1.4 MPa to 2.5 MPa, and the reaction temperature is 70 to 110°C. Since hydroformylation is a strongly exothermic reaction, heat removal from the reactor is expected. The degree of olefin conversion according to the claimed hydroformylation method is 96.2%, and the selectivity is 95%.
CN 102115433 discloses a method for the synthesis of propanal on a catalyst that is rhodium triphenylphosphine. ln this catalyst, the rhodium concentration was 100 ppm and the triphenylphosphine concentration was 2.0%. The synthesis of propanal was carried out at a pressure of 1.5 MPa and a temperature of 80°C. The yield of propanal reached 996%.
RU 2354642 C2 teaches a method of hydroformylation of Cz-Czo olefins, characterized by olefins being hydroformylated in the presence of a catalytic system containing rho- dium, a polyphosphite ligand and a promoting ligand containing phosphorus. General formulas of polyphosphite ligand and the promoting ligand are given.
RU 2561171 C1 discloses a method of continuous, two-stage hydroformylation of C3- C4 olefins and a process unit for producing C4-C5 aldehydes. Hydroformylation of ole- fins is carried out using a recirculating catalyst solution containing a rhodium complex, organophosphorus ligands, product aldehydes, and heavy by-products.
Moreover, RU 2585285 C1 teaches a method for continuous hydroformylation of Cz-Cs olefins using nanofiltration separation of heavy products from a recirculating catalyst solution containing a rhodium complex with a phosphite ligand. The disclosed method 13 makes it possible to reduce the loss of the catalytically active rhodium complex and or- ganophosphorus ligand when removing heavy condensation products of aldehydes.
Also, RU 2602239 C1 teaches a method of Cß-Cg olefin hydroformylation into Cw-Cio alcohols. Hydroformylation of Cß-Cg olefins uses a catalytic system, consisting of a co- balt compound at a concentration of 0.15 to 0.40 wt. % and organophosphorus Iigand, which is a triphenylphosphine in a mo|ar ratio to cobalt in the range of1 to 1.2. The al- cohols are produced at a temperature of 170 to 190°C and a synthesis gas pressure of 5 to 10 MPa. The conversion of Cß-Cg olefins is up to 99%, and the yield of Cw-Cio al- cohols is at least 90%.
RU 2051734 C1 disc|oses a catalyst for the conversion of ethano| into acetone and carbon dioxide, using a catalyst containing zink oxide ZnO 96.5-97.9% and cerium ox- ide CeOz 2.1-3.42%.
RU 0002619951 teaches a tvvo-stage method for propionic aldehyde production. The method includes the stage of carbon dioxide hydrogenation into synthesis gas in the presence of a catalyst containing metallic cobalt supported by organometallic frame- work structure. Metallic rhodium supported by a carrier was used as a catalyst for the hydroformylation. The process was carried out in a two-shelf flow-through reactor at a pressure of 20 to 40 atm by contacting a stationary layer of a catalyst containing co- balt, placed on the upper shelf of the reactor and heated to a temperature of 500°C, with a raw material mixture of H2 and C02 at a volumetric flow rate of gas feed supply of 500-1000 h'1. After that, the reaction gases obtained, heated to a temperature of 500-520°C, containing a mixture of CO + H2 + C02, were mixed with cold ethylene supplied to the inter-shelf space. The resulting gas mixture in a ratio of CO:H2:C2H4 = 1 :(1 -2):1 was supplied to the lower shelf of the reactor at a temperature of 170 to 230°C for interaction with the rhodium-containing catalyst placed there. The proposed method provides for increasing the selectivity of the target product formation up to 58.1%, and the yield up to 20.1 %, ensuring the utilization of the greenhouse gas, C02. lt should be mentioned that the largest scale and most industrially developed method of processing biomass into alcohols is currently the process of ethano| production. 14 Ethanol is currently used in gasoline, both individually and in the form of ethers to in- crease the octane number. However, the wider use of ethanol in gasoline is limited by the oxygen content limit, which is regulated by the relevant standards.
At the same time, it is known that ethanol, as well as 66-66 alcohols, can be obtained by biosynthesis and processed into a motor fuel free of oxygen, see e.g. "6onversions of mixtures of 62-66 olefins to jet fuel and/or diesel fuel in high yield from bio-based al- cohols" WO 2018071905 A1, US 2020010767 A1. The method consists of the produc- tion of 66-616 paraffins by processing 62-66 alcohols obtained by fermentation of car- bohydrates, extracted from biomass. The paraffins thus obtained can be used to pro- duce motor fuel. The method demonstrates the possibility of obtaining hydrocarbons that can be used as components of motor fuel. Moreover, said method directly indi- cates the need to use 62-66 alcohols obtained from biomass in the production of motor fuel. Also, the document proposes to use the oligomerization of 62-66 olefins to obtain higher olefins 612-616. Also, said document proposes to use the hydrogenation of 66- 616 olefins to obtain 66-616 paraffins.
Objects of the invention The tasks to be solved by the present invention are the following: - development of methods for converting ethyl alcohol into higher alcohols, including 66-66 alcohols; - development of methods for producing 66-66 alcohols, primarily branched alcohols; - improvement of the technology of 62-66 olefin hydroformylation, including the goal of increasing the yield of 64-66 branched aldehydes; - development of technology for lower olefin oligomerization into higher olefins, provid- ing for producing fractions of higher branched olefins, with a linear molecule content of not higher than 5%, and free of aromatic and cyclic compounds; - development ofmethods for producing 66-624 branched paraffins, in which the number of the number of the various compounds is not less than 50 and preferably more than 100, and the content of linear molecules does not exceed 5%, and free of aromatic and cyclic compounds; - development of methods for producing 67-616 ethers of branched structure; - development of production methods and compositions of gasoline with RON octane number of at least 95 and free of aromatic compounds; - development of production methods and compositions of kerosene hydrocarbon frac- tions of primarily branched structure, free from aromatic compounds; - development of production methods and compositions of kerosene, containing hydro- carbon fractions of mainly branched structure, and with aromatic compounds content in the range from 8% vol. to 25% vol.; - development of production methods ofdiesel and diesel compositions that do not con- tain aromatic compounds; - development of technology for the manufacture of gasoline, kerosene and diesel using raw materials of biological origin.
Summary of the invention ln order to accomplish one or more of the above objects the following method for pro- ducing from ethanol a motor fuel selected from gasoline, kerosene, and diesel, is pro- vided, which method comprises the following interconnected steps: step 1.1 converting a mixture of ethanol and water into: isopropanol and G5 alcohols; acetaldehyde; a mixture of C1-C4 paraffins and C2-C4 olefins; a mixture of carbon diox- ide and hydrogen; step 1.2 converting the mixture of carbon dioxide and hydrogen, obtained in step 1.1, additional hydrogen, and a mixture of C1-C4 paraffins into synthesis gas; step 1.3 converting ethanol, and Cs-Cs alcohols, including G5 alcohols obtained from step 1.1, into: Cz-Cs olefins, including ethylene and propylene; step 1.4 converting a mixture of unreacted ethanol from step 1.1, isopropanol obtained in step 1.1, ethylene obtained in step 1.3, using a telomerization reaction into second- ary butanol and tertiary Cs-Cs alcohols, the tertiary Cs and G7 alcohols being obtained from the isopropanol, and the tertiary Ca, and Cs alcohols being obtained from the eth- anol, wherein the resulting secondary butanol is directed to step 1.3; step 1.5 converting the Cs-Cß tertiary alcohols, obtained in step 1.4, by dehydration into Cs-Cg olefins; step 1.6 converting a first portion of the Cs-Cs olefins, obtained in step 1.5, by oli- gomerization into C1o-C24 olefins; step 1.7 converting the C1o-C24 olefins, obtained in step 1.6, by hydrogenation using 16 hydrogen obtained from step 1.1, into G1o-G24 paraffins; step 1.8 converting the Synthesis gas, obtained in step 1.2, ethylene obtained in step 1.3, propylene obtained in step 1.3, and the acetaldehyde, obtained in step 1.1, by hy- droformylation and a|do| condensation into a mixture of G3-G4 aldehydes and Gs-Gs al- dols, said mixture of G3-G4 aldehydes and Gs-Gs aldols is thereafter hydrogenated to obtain Gg-Gg alcohols, which alcohols are directed to step 1.3 to obtain Ga-Gs olefins, wherein the acetaldehyde produces G5 alcohol, the ethylene from step 1.3 produces Gs and G6 alcohols, and the propylene from step 1.3 produces G4 and G8 alcohols; and wherein the ethylene and the propylene from step 1.3 produce G7 alcohol; step 1.9 converting the Gz-Gs o|efins from step 1.3, by oligomerization into G6-G24 ole- fins; step 1.10 converting the G6-G24 olefins, obtained in step 1.9, and hydrogen, by hydro- genation into G6-G24 paraffins; step 1.11 converting unreacted Gz-Gs o|efins from step 1.9, and the mixture of G2-G4 o|efins and G1-G4 paraffins, obtained in step 1.1, by aromatization into Gw-Giz aromatic hydrocarbons, hydrogen, and a mixture of G1-G4 paraffins, wherein a first portion of the hydrogen produced is directed to step 1.10, and the remaining second portion of the hydrogen produced and the G1-G4 paraffins mixture are directed to step 1.2; step 1.12 converting the remaining second portion of the mixture of Gs-Gs olefins, ob- tained in step 1.5, and a portion of Gg-Gg alcohols from step 1.3, into Gw-Gie ethers; and, step 1.13 converting the G1o-G24 paraffins, obtained in step 1.7, and the G6-G24 paraf- fins, obtained in step 1.10, into Gß-Gio gasoline, G11-G1s kerosene, and G19-G24 diesel fractions of a motor fuel; converting the G1-G12 aromatic hydrocarbons, obtained in step 1.11, into Gw-Gs gasoline and G9-G12 kerosene fractions of a motor fuel; and con- verting the Gw-Giß ethers, obtained in step 1.12, into Gw-Gio gasoline and G11-G1e diesel fractions of a motor fuel, and also mixing selected fractions thereof, into a motor fuel selected from gasoline, kerosene, and diesel.
A method for producing motor fuel from ethanol has been developed by the present in- ventor, wherein the technological process of ethanol conversion into motor fuel is car- ried out as follows: Ethanol is converted into Gs-Gs alcohols by two different routes. 17 ln one of the routes, a mixture of ethanol and water at 500-515°C is contacted with a heterogeneous Catalyst consisting of the following metal oxides: ZnO 60 to 63% mass; CeOg 1 to 6% mass; MgO 12 to 18% mass; AlzOa 13 to 23% mass, with the propor- tions calculated in terms of metal oxide, yielding a liquid reaction medium, comprised mainly by water and acetone, as well as acetaldedyde and diethylketone. Furthermore, a gaseous reaction medium is obtained, comprised mainly by carbon dioxide and hy- drogen, as well as C2-C4 olefins and C1-C4 paraffins. The acetone and diethylketone are then hydrogenated to yield isopropanol and 3 pentanol alcohol. Acetaldehyde is then used in aldol condensation with propanal to obtain 2-methylbutenal, which is the hydrogenated into 2 methyl butyl alcohol. A mixture of C2-C4 olefins and C1-C4 paraf- fins is used in the process of aromatization to obtain aromatic compounds. Carbon di- oxide and hydrogen are converted into synthesis gas in the presence of Cu or Ni cata- lysts.
After that, ethanol and isopropanol in the presence of ditretamyl peroxide interact with ethylene to form sec-butanol, as well as tertiary Cs-Cs alcohols. ln another route, Cs-Cs alcohols are obtained by hydroformylation of ethylene or pro- pylene, obtained by dehydration of ethanol or propanol in the presence of a gamma AlzOs catalyst, by synthesis gas produced from carbon dioxide and hydrogen. Hydro- formylation of ethylene or propylene is carried out in a heterogeneous reaction medium using a water-soluble Rhodium catalyst. ln this case, the concentration of Rhodium in the aqueous phase is from 30 to 50 ppm. Triphenylphosphine-sulfonic acid sodium salts are used as a ligand: from triphenylphosphine-3-sulfonic acid sodium salt to tri- phenylphosphine-3,3',3"-trisulfonic acid trisodium salt. The process of obtaining propi- onic or butyl aldehydes is carried out at a temperature of 45 to 90°C and a pressure of 1.0 to 3.0 MPa. The obtained acetaldehyde, propionic and n-butyl aldehydes are treated by cross aldol condensation in the presence of a heterogeneous granular cata- lyst, containing at least 93% ZSM-5 modified by 3.5 to 7.0% Zn at a temperature of 100 to 150°C and a pressure of 0.5 to 1.0 MPa. The resulting mixture of aldehydes and Cs-Cs aldoles is then hydrogenated to yield Cs-Cs alcohols. 18 Moreover, it was found that the hydroformylation of ethylene or propylene obtained in the dehydration of ethanol or propanol by synthesis gas produced from carbon dioxide and hydrogen can be performed in a heterogeneous reaction medium using a water- soluble cobalt catalyst. When using a cobalt catalyst, the concentration of the metal in the aqueous phase is from 0.1 % to 1.0%. ln this case, triphenylphosphine-sulfonic acid sodium salts are used as a Iigand: from triphenylphosphine-3-sulfonic acid sodium salt to triphenylphosphine-3,3',3"-trisulfonic acid trisodium salt. Hydroformylation of eth- ylene or propylene is carried out at a temperature of 120 to 145°6 and a pressure of 3.0 to 5.0 MPa. lt was demonstrated, that besides formation of the propionic or butyl aldehydes, the condensation of said aldehydes occurs in the reaction medium to yield 2-methyl pentenal or 2-ethylhexenal. Hydrogenation of the resulting aldehyde and aldol mixtures provide for producing 63-68 alcohol mixtures. 62-68 olefins obtained by dehydration of primary and secondary 62-68 alcohols are oli- gomerized in the presence of a heterogeneous catalyst, containing at least 93% ZSM- 5 modified by 3.5 to 7.0% Zn, or in the presence of a heterogeneous catalyst contain- ing at least 95% ZSM-5 modified by 3.5 to 5.0% Zn and 0.1 to 1.5% 6e, at a tempera- ture of 250-350°6 and a pressure of 2.0-5.0 MPa to obtain 66-624 olefins. The unre- acted 62-65 olefins from the oligomerization reaction are used as a raw material for producing aromatic 61-612 compounds in the presence of a heterogeneous catalyst, containing at least 93% ZSM-5 modified by 3.5 to 7.0% Zn at a temperature of 350 to 450°6 and a pressure of 0.5 to 5.0 MPa. 65-68 olefins, obtained by dehydration of tertiary 65-68 alcohols, are oligomerized in the presence of a heterogeneous catalyst, which is an ion exchange resin in the form of a cation exchanger, for example Amberlite15, at a temperature of 70-120°6 and a pressure of 1.0 to 2.0 MPa to yield 610-624 olefins. The unreacted 65-68 olefins from the oligomerization reaction and a proportional part of the primary and secondary 65- 68 alcohols are used as a source material for producing 61-616 ethers in the presence of an ion-exchange resin in the form of, for example, a cation exchanger, Amberlite15, at a temperature of 70 to 120°6 and a pressure of 1 .0 to 2.0 MPa. 66-624 and 610-624 olefins are hydrogenated in the presence of a heterogeneous cata- lyst, containing oxides NiO, 6uO and 6r2O3 in a molar ratio of 1:1:1, at a temperature 19 of 150 to 200°6 and a pressure of 4.5 to 5.0 MPa to obtain 66-624 and 610-624 paraf- fins. After that, 66-624 and 610-624 paraffins are directed to rectification to obtain 66-610 gasoline, 611-616 kerosene and 619-624 diesel fractions. The isolated gasoline fraction of 66-610 paraffins is blended with 61-610 ethers and/or 67-66 aromatic hydrocarbons to obtain gasoline complying with the current standard EN228, however, with a RON octane number of at least 100 and MON of at least 93. The separated kerosene frac- tion of 611-616 paraffins is blended with 60-612 aromatic hydrocarbons to obtain kero- sene complying with the current standard for Jet A-1. The isolated diesel fraction of 619-624 paraffins is blended with 61-616 ethers to obtain diesel fuel complying with the current standards.
The method developed for producing motor fuel from ethanol, as well as the proposed schematic diagram of the technological process for converting ethanol, provide for es- tablishing industrial production of environmentally friendly kerosene, as well as gaso- line and diesel.
Brief description of the attached drawing Figure 1 shows a block scheme of the inventive process.
Detailed description of the invention Figure 1 shows the inventive scheme developed for conversion of ethanol into motor fuels and, particularly, into kerosene.
The feedstock used for the inventive production of kerosene and other motor fuels is ethanol. Preferred ethanol of the inventive method for the motor fuel production is pro- duced from wood or wastes from humans and their activities. To increase the eco- nomic efficiency of our proposed method for converting ethanol into motor fuel, fusel oils can be used as an additional raw material along with carbon dioxide and methane obtained in the production of ethanol. Also, according to the invention, it is recommended to use electricity obtained from environmentally friendly sources and wastes of plant biomass as the energy resource for the method of the present inven- tion of converting ethanol into motor fuel. lt is known in the prior art, that acetone can be obtained from ethyl alcohol with a high yield, that is, 95% of theoretical yield. The vapors of ethyl alcohol mixed with steam are directed at 400-425°C through the catalyst containing 54% of iron and chromium ox- ides, 8% of copper oxide and 38% of calcium carbonate. The total reaction is de- scribed by the equation: 2 C2H5OH + H20 catalysis, t° -> CHg-CO-CHg + C021 +4H2T As disclosed in one of the prior art references above, RU 2051734 C1, acetone is nearly the only liquid product of the reaction in the presence of catalyst consisting of ZnO, 96.5 to 97.9%, and CeOz, 2.1 to 3.42%.
At step 1.1 of the inventive method for producing motor fuel, an aqueous solution of ethanol is converted into a mixture of acetone, acetaldehyde, diethylketone and and Cs-Cs alcohols in the presence of a specially designed catalyst at a temperature of 500 to 515°C and a pressure of 0.9 to 1.1 MPa. The composition of the catalyst is as fol- lows: ZnO, 60 to 63% mass; CeOg, 1 to 6% mass; MgO, 12 to 18% mass; AI2O3, 13 to 23% mass. Furthermore, part of the ethanol is converted, under these conditions, into carbon dioxide, hydrogen and a mixture of C2-C4 olefins and C1-C4 paraffins.
Conversion of ethanol into a mixture of the products above, in the presence of the cat- alyst used, is unexpected and opens up new possibilities for the production of hydro- carbons that can be used in kerosene. ln a preferred embodiment of the inventive method, a mixture of ethanol and water, the content of which is from 25% to 35% of the total volume of the mixture, contacts at a pressure of 0.5-1 .5 MPa and a temperature of 500-515°C with a heterogeneous cata- lyst consisting of the following metal oxides; ZnO 60-63% mass., CeOg 1-6% mass., MgO 12-18% mass., AlzOs 13-23% mass., with the proportions calculated in terms of metal oxide, wherein a mixture of ethanol with water is supplied to the catalyst at a rate of 0.5-0.9 liters per 1 liter of catalyst per hour. Acetone and diethyl ketone, obtained in the process, are isolated from the reaction mixture, hydrogenated at a temperature of 100-150°C and a pressure of 0.5-0.9 MPa in the presence of catalyst containing oxides CuO and CrzOs in a molar ratio of 1:1 by hydrogen, which is also obtained from a mix- ture of ethanol and water. This yields isopropanol and 3-pentanol. A mixture of Ca-Cs 21 alcohols is used for producing the corresponding olefins by dehydration in the pres- ence of catalyst, gamma AlzOa. lsopropanol, isolated from the reaction medium, is used to obtain tertiary alcohols Cs-Cw and 67+. Moreover, contacting the catalyst con- sisting of the following metal oxides: ZnO 60-63% mass., CeOg 1-6% mass., MgO 12- 18% mass., AlzOs 13-23% mass., with the proportions calculated in terms of metal ox- ide, with a mixture of ethanol and water yields acetaldehyde, which is isolated from the reaction medium and used in the aldol condensation with propanal to obtain 2-methyl butenal. The 2-methyl butenal is then hydrogenated to yield 2-methyl butanol. Particu- lary important for the inventive method is the possibility of converting a mixture of etha- nol and water into carbon dioxide and hydrogen upon contact with the catalyst consist- ing of the following metal oxides: ZnO 60-63% mass., CeOg 1-6% mass., MgO 12-18% mass., AlzOß 13-23% mass., with the proportions calculated in terms of metal oxide. ln step 1.2 of the inventive method said carbon dioxide and hydrogen are converted into water and carbon monoxide in the presence of a catalyst containing 5-10% Cu sup- ported by AI2O3, at a temperature of 550-600°C and a pressure of P = 1.0-5.0 MPa, or, using a catalyst containing oxides NiO, CuO and CrzOs in a molar ratio 1:1:1, are con- verted at a temperature of 900-1000°C and a pressure of P = 0.1-0.5 MPa into a mix- ture of carbon monoxide and hydrogen. The carbon monoxide and hydrogen are used in step 1.2 of the inventive process to produce synthesis gas.
Dehydration of ethanol is carried out at the step 1.3 of the inventive method for olefin production in the presence of a gamma AlzOs catalyst in a continuous flow reactor at 350 to 450°C and a pressure of 0.5 to 3.5 MPa.
Ethylene and water are formed in the dehydration reactor. The reaction mixture from the dehydration reactor enters the rectification column, where ethylene is separated from the obtained water. Water is directed to the production of an aqueous solution of ethanol in the process of acetone production.
Ethylene obtained by dehydration of ethanol is directed to step 1.4 of the inventive pro- cess for performing the reaction of telomerization or to step 1.8 of the inventive pro- cess for performing the reaction of hydroformylation. 22 Propylene, obtained by dehydration of n-propanol or isopropanol, is directed to step 1.8 of the inventive method to perform the reaction of hydroformylation. Ca-Cs alcohols obtained in the inventive method for producing motor fuel, are processed at step 1.3 of the inventive method into the corresponding olefins Cs-Cß in a similar way by using gamma AlzOs as a catalyst. The Cz-Cs olefins obtained at step 1.3 of the inventive method are sent to step 1.9 of the inventive method to carry out the reaction of oli- gomerization into 66-624 olefins.
Hydroformylation of ethylene, obtained from the dehydration of ethanol at step 1.3 of the inventive method, is carried out at step 1.8 of the inventive method in the presence of either a rhodium or cobalt catalyst. The process of ethylene hydroformylation is car- ried out in a heterogeneous reaction medium using a water-soluble catalyst. When us- ing a rhodium catalyst, the concentration of the metal with respect to the liquid phase is between 30 and 50 ppm. ln this case, triphenylphosphine-sulfonic acid sodium salts are used as a ligand: from triphenylphosphine-3-sulfonic acid sodium salt to tri- phenylphosphine-3,3',3"-trisulfonic acid trisodium salt in a ratio of 30:1 to metallic rho- dium. The process is carried out in the reactor with a stirring device at a temperature of 45 to 90°C and a pressure of 1.0 to 3.0 MPa. The molar ratio of the source gases C2H4:CO:H2 = (1 to 1.1):1:1 is maintained by flow meters. ln a preferred embodiment of the inventive method, in order to reduce catalyst losses, the organic phase, obtained in the process of ethylene hydroformylation, is separated from the aqueous phase, containing dissolved Rh catalysis, using a highly efficient centrifugal separator.
The resulting reaction mass enters a highly efficient centrifugal separator, where it is separated into three phases: a gas phase containing unreacted ethylene, carbon mon- oxide and hydrogen, a liquid organic phase containing mainly propanal and a liquid aqueous phase containing a water-soluble rhodium catalyst. The gas phase and the liquid aqueous phase are returned to the hydroformylation reactor by the metering de- vices.
The liquid organic phase, consisting mainly of propanal, is directed to the reactor filled with a granular catalyst containing at least 93% of ZSM-5 zeolite modified by 3.5 to 23 7.0% Zn, or a granular Catalyst containing at least 95% of ZSM-5 zeolite modified by 3.5 to 5.0% Zn and 0.1-1.5% Ce, where the propanal is converted into 2-methyl-pen- tenal at a temperature of 100 to 150°C and a pressure of 0.5 to 1.0 MPa.
The liquid organic phase, containing mainly 2-methyl-pentenal as well as propanal, is sent to the reactor filled with a granular catalyst comprising NiO, CuO and CrzOs ox- ides in a molar ratio of 1:1:1, where 2-methyl-pentenal and propanal are at a tempera- ture of 150 to 200°C and a pressure of 4.5 to 5.0 MPa converted into 2-methyl-penta- nol and propanol.
Further, the propanal, obtained by hydroformylation, is mixed with acetaldehyde, which is obtained by the inventive process for ethanol conversion into acetone, and is used to produce 2-methyl-butenal. For this, the mixture of acetaldehyde and propanal, in a mo- lar ratio of 1:1, is directed to a reactor filled with a granular catalyst, containing at least 93% of ZSM-5 zeolite modified by 3.5 to 7.0% Zn, or a granular catalyst containing at least 95% of ZSM-5 zeolite modified by 3.5 to 5.0% Zn and 0.1 to 1.5% Ce, where the mixture of source aldehydes is at a temperature of 100 to 150°C and a pressure of 0.5 to 1.0 MPa converted into 2-methyl-butenal. The reaction mass containing 2-methyl- butenal is directed to the reactor filled with a granular catalyst consisting of the oxides NiO, CuO and CrzOa in a molar ratio of 1:1:1, where 2-methyl-butenal is converted into 2-methyl-butanol at a temperature of 100 to 200°C and a pressure of 5.0 to 9.0 MPa.
Hydroformylation of propylene, obtained in step 1.3 of the inventive method by dehy- dration of n-propanol or isopropanol in the presence of a rhodium catalyst is preferably performed as follows. Propanol, obtained by hydrogenation of propanal, or isopropa- nol, obtained by hydrogenation of acetone, are dehydrated. The dehydration of propyl alcohols is carried out using a heterogeneous gamma AlzOs catalyst at a temperature of 350 to 450°C and a pressure of 0.1 to 1.0 MPa. Propylene, obtained by dehydration of propyl or isopropyl alcohols, is separated from water and sent to hydroformylation.
Hydroformylation of propylene is carried out in a heterogeneous reaction medium us- ing a water-soluble rhodium catalyst. When a rhodium catalyst is used for propylene hydroformylation the metal concentration with respect to the liquid phase is from 30 to 24 50 ppm. ln this case, triphenylphosphine-sulfonic acid sodium salts are used as a lig- and: from triphenylphosphine-3-sulfonic acid sodium salt to triphenylphosphine-3,3',3"- trisulfonic acid trisodium salt in a ratio of 30:1 with metallic rhodium. The process is performed in the reactor with a stirring device at a temperature of 70 to 90°C and a pressure of 3.0 to 5.0 MPa. The ratio of the source gases in mo|es C3H6:CO:H2 = (1 - 1.1):1:1 is maintained by flow meters.
To increase the rate of the propylene hydroformylation reaction and to increase the yield of isobutanal, Cg-Cg alcohols are added to the water-soluble Rh catalyst in the volume ratio H20: (Cz-Ca) = (0.95-0.65) :( 0.05-0.35).
Additionally, in order to reduce catalyst losses, the organic phase obtained in the hy- droformylation of propylene is separated from the aqueous phase, containing dissolved Rh catalyst, using a highly efficient centrifugal separator.
The resulting reaction mass is directed to a highly efficient centrifugal separator to sep- arate the reaction mass into three phases: (i) a gas phase containing unreacted propyl- ene, carbon monoxide and hydrogen, (ii) a liquid organic phase containing mainly bu- tanals and (iii) a liquid aqueous phase containing a water-soluble rhodium catalyst. The gas phase and the liquid aqueous phase are returned to the hydroformylation re- actor by metering devices.
The liquid organic phase containing n-butanal and isobutanal in the weight ratio (2-3):1 is transferred to the reactor filled with a granular catalyst, containing at least 93% of ZSM-5 zeolite modified by 3.5 to 7.0% Zn, or a granular catalyst containing at least 95% of ZSM-5 zeolite modified by 3.5 to 5.0% Zn and 0.1 to 1.5% Ce, where at a tem- perature of 100-150°C and a pressure of 0.5-1 .0 MPa, butanal is converted into 2- ethyl-hexenal.
The liquid organic phase, containing mainly 2-ethyl-hexenal, as well as isobutanal, is sent to a reactor filled with a granular catalyst consisting of the oxides NiO, CuO and CrzOa in a molar ratio of 1:1:1, where, at a temperature of 100 to 200°C and a pressure of 5 to 10 MPa, 2-ethyl-hexenal and isobutanal are converted into 2-ethyl hexanol and isobutanol.
Moreover, the inventive method, in a preferred embodiment, provides for obtaining C5- Cß alcohols by cross-aldol condensation of n-butanal, acetaldehyde and propanal in the presence of a heterogeneous catalyst containing at least 93% of ZSM-5 zeo|ite modified by 3.5-7.0% Zn, or a granular catalyst containing at least 93% of ZSM-5 zeo- |ite modified by 3.5-5.0% Zn and 0.1-1.5% Ce. The obtained 2-methyl-butenal, 2-me- thyl-pentenal, 2-methyl-hexenal and 2-ethyl-hexenal are then hydrogenated in the presence of a heterogeneous catalyst consisting of the oxides NiO, CuO and CrzOs in a molar ratio of 1 :1:1 at a temperature of 150-200°C and a pressure P = 4.5-5.0 MPa to yield 2-methyl-butanol, 2-methyl-pentanol, 2-methyl hexanol and 2-ethyl-hexanol.
The fact that a water-soluble cobalt catalyst can be used for hydroformylation of lower Cz-Cß olefins was unexpected. When using a cobalt catalyst, the concentration of the metal with respect to the liquid phase is between 0.1% and 1.0%. Triphenylphosphine- sulfonic acid sodium salts are used as a ligand: triphenylphosphine-3-sulfonic acid so- dium salt to triphenylphosphine-3,3',3"-trisulfonic acid trisodium salt in a ratio (1-30):1 to metallic cobalt. The hydroformylation of ethylene is carried out in a reactor with a stirring device at a temperature of 120 to 140°C and a pressure of 3.0 to 5.0 MPa. The ratio of the source gases in moles: C2H4:CO:H2 is from 1:1:1 to 1:1.5:2.5 and is main- tained by flow meters. ln order to reduce catalyst losses, the organic phase formed during ethylene hydro- formylation is separated from the aqueous phase, in which the Co catalyst is dissolved, using a highly efficient centrifugal separator. The resulting reaction mass is transferred to a highly efficient centrifugal separator for separation into three phases: a gas phase containing unreacted ethylene, carbon monoxide and hydrogen, a liquid organic phase containing mainly propanal, 2-methylpentenal, and also 2-methylpentanal, and a liquid aqueous phase containing a water-soluble cobalt catalyst. The gas phase and the liq- uid aqueous phase are returned to the hydroformylation reactor by metering devices. The fact that 2-methylpentenal and 2-methylpentanal were obtained directly at the hy- droformylation step was unexpected.
The liquid organic phase, containing mainly propanal, as well as 2-methylpentenal and 2-methylpentanal, is transferred to the reactor filled with a granular catalyst, containing oxides of NiO, CuO and CrgOß in a molar ratio of 1:1:1, where at a temperature of 150 26 to 200°C and a pressure of 4.5 to 5.0 MPa, the mixture of aldehydes is converted into a mixture of the corresponding alcohols, that is n-propanol and 2-methylpentanol.
Hydroformylation of propylene is carried out in the reactor with a stirring device at a temperature of 135 to 140°C and a pressure of 3.0 to 5.0 MPa. The molar ratio of the feed gases: CsH6:CO:H2 is from 1:1:1 to 1:1.5:2.5 and is maintained by flow meters. Cz-Cß alcohols are added to the water-soluble cobalt catalyst in the volume ratio H2O:(C2-Cs) = (0.95-0.5):(0.05-0.5) in order to increase the rate of the reaction of pro- pylene hydroformylation and to increase the yield of isobutanal. ln order to reduce cat- alyst losses, the organic phase formed during hydroformylation of propylene is sepa- rated from the aqueous phase, in which the Co catalyst is dissolved, using a highly effi- cient centrifuga| separator. The resu|ting reaction mass is transferred to a highly effi- cient centrifuga| separator for separation into three phases: a gas phase containing un- reacted propylene, carbon monoxide and hydrogen, a liquid organic phase, containing n-butanal, isobutanal, 2-ethylhexenal and 2-ethylhexanal, as well as some amounts of the corresponding alcohols, and a liquid aqueous phase containing a water-soluble co- balt catalyst. The gas phase and the liquid aqueous phase are returned to the hydro- formylation reactor by metering devices. The fact that 2-ethylhexenal and 2-ethylhex- anal and also butyl alcohols and 2-ethyl hexanol were obtained directly in the hydro- formylation step was unexpected.
A mixture of n-butanal and isobutanal is separated by rectification from the liquid or- ganic phase containing n-butanal and isobutanal in a mass ratio of (2-3):1, as well as 2-ethylhexenal and 2-ethylhexanal.
The mixture of n-butanal and isobutanal is directed to the reactor filled with a granular catalyst containing at least 93% of ZSM-5 zeolite modified by 3.5 to 7.0% Zn, or a granular catalyst containing at least 95% of ZSM-5 zeolite modified by 3.5 to 5.0% Zn and 0.1 to 1.5% Ce, where, at a temperature of 100 to 150°C and a pressure of 0.5 to 1.0 MPa, n-butanal is converted into 2-ethylhexenal.
The aldehydes thus obtained are then combined into a general mixture containing iso- butanal, 2-ethylhexenal and 2-ethylhexanal. This mixture of aldehydes is sent to the re- actor filled with a granular catalyst consisting of the oxides NiO, CuO and CrzOs in a 27 molar ratio of 1:1:1, where at a temperature of 150 to 200°C and a pressure of 3.0 to 5.0 MPa, isobutanal, 2-ethylhexenal and 2-ethylhexanal are converted into a mixture of the corresponding alcohols, that is: isobutanol and 2-ethylhexanol.
Moreover, in a preferred embodiment, the inventive method provides for obtaining C3- Cß alcohols as follows. To obtain G5 alcohol, namely: 2-methyl butanol, acetaldehyde along with gaseous feed is supplied at a temperature of 120-140°C and a pressure of P = 2.0-5.0 MPa in a molar ratio (C2H4:CO:H2):(C2H4O) = 1: 0.5 to a water-soluble Co catalyst during the reaction of ethylene hydroformylation by synthesis gas. This yields propanal, 2-methylpentenal and 2-methylpentanal, as well as 2-methylbutenal, which is formed due to the cross aldol condensation of acetaldehyde with propanal. Then the resulting mixture of propanal and aldols Cs-Cß is hydrogenated in the presence of a heterogeneous catalyst consisting of the oxides NiO, CuO and CrzOa in a molar ratio of 1:1:1 at a temperature of 150-200°C and a pressure of P = 4.5-5.0 MPa to obtain a mixture of Cs-Cß alcohols containing 2-methyl butanol. ln a similar way, in order to obtain G7 alcohols, namely 2-methyl hexanol and 2-ethyl pentanol, propanal along with a gaseous feed is supplied, during reaction of propylene hydroformylation by synthesis gas, at a temperature of 135-140°C and a pressure of P = 2, 0-5.0 MPa in a molar ratio (C3H6:CO:H2):(CsH6O) = 1:(0.5-1) to a water-soluble Co catalyst. This yields isobutanal, 2-methylpentenal, 2-methylpentanal, 2-ethyl hexenal, and 2-ethyl hexanal, as well as 2-methyl hexenal and 2-ethyl pentenal, which are formed due to the cross-aldol condensation of n-butanal with propanal. Then the re- sulting mixture of isobutanal and aldoles Cß-Cs is hydrogenated in the presence of a heterogeneous catalyst consisting of the oxides NiO, CuO and CrzOa in a molar ratio of 1:1:1, at a temperature of 150-200°C and a pressure of P = 4.5-5.0 MPa yielding a mixture of C4-C8 alcohols containing, inter alia, 2-methyl hexanol and 2-ethyl pentanol.
Hydroformylation of ethylene and propylene uses synthesis gas obtained by the in- ventive technology. For the production of synthesis gas, carbon dioxide and hydrogen obtained during conversion of ethanol into acetone at the step 1.1 of the inventive method are used. The synthesis gas production process is performed by two methods. ln the first method, a mixture of carbon dioxide and hydrogen in a molar ratio of CO2:H2 = 1:1 is supplied into the reactor, filled with a granular catalyst 5 to 10% Cu supported 28 by AlzOs, at a temperature of 550 to 600°C and a pressure of 3.0 to 5.0 MPa. The car- bon monoxide thus obtained is cooled, isolated from water and directed to step 1.8 of the inventive method, to the hydroformylation reactor. Simultaneously with carbon monoxide, hydrogen is fed into the hydroformylation reactor in a mo|ar ratio of CO:H2 = 1:1. ln the second method, a mixture of carbon dioxide and hydrogen, in a mo|ar ratio of CO2:H2 = 1:(2-3), is supplied into a reactor filled with a granular cata|yst consisting of the oxides NiO, CuO and CrzOß in a mo|ar ratio of 1 :1:1, at a temperature of 950 to 1000°C and a pressure of 0.1 to 0.5 MPa. The mixture of carbon monoxide and hydro- gen thus obtained is cooled, isolated from water, carbon dioxide and methane, and then transferred to the synthesis gas co||ecting tank for the adjustment of the composi- tion. Simultaneously with a mixture of carbon monoxide and hydrogen, hydrogen is fed into the synthesis gas co||ecting tank to adjust the mo|ar ratio to CO:H2 = 1:1. From the synthesis gas co||ecting tank the mixture of carbon monoxide and hydrogen is directed to the hydroformylation reactor at step 1.8 of the inventive method by a compressor at a pressure of 3.0 to 5.0 MPa.
The Cz-Cß alcohols synthesized by the inventive processes can be converted into mo- tor fuel both individually and as mixtures. The main pathway for the conversion of C2- Cg alcohols into higher paraffins is based on the oligomerization of Cz-Cs olefins, which, in turn, are obtained by dehydration of the corresponding alcohols.
According to the invention, it is recommended to use zeolites modified by Zn and Ce, that is a zeolite-containing cata|yst, containing at least 93% ZSM-5 modified by 3.5 to 7.0% Zn, or a zeolite-containing cata|yst, comprising at least 95% ZSM-5 modified by 3.5 to 5.5% Zn and 0.1 to 1.5% Ce as catalysts for Cz-Cs olefin oligomerization. Also, it is recommended to use zeolites modified by Zn and Ce as catalysts for oligomerization of Cz-Cs olefins.
The inventive method for producing motor fuel provides for using a mixture of primary and secondary C2-C5 alcohols, which include Cg-Cs alcohols synthesized from ethanol, as a feedstock. For this, primary and secondary Cz-Cs alcohols are dehydrated using a cata|yst gamma AlzOß in a continuous flow reactor at a temperature of 350-450°C and 29 a pressure of 0.5-3.5 MPa to yield Cz-Cs olefins. Cz-Cs olefins thus obtained are then oligomerized in the presence of a heterogeneous granular catalyst containing at least 93% of ZSM-5 zeolite modified by 3.5-7.0% Zn, or a granular catalyst containing no less than 95% of ZSM-5 zeolite modified by 3.5-5.0% Zn and 0.1-1.5% Ce at a temper- ature of 250-350°C and a pressure of P = 2.5-5.0 MPa.
The Cß-Czo olefins formed in the process of oligomerization are hydrogenated in the presence of a heterogeneous catalyst consisting of the oxides NiO, CuO and CrzOs in a molar ratio of 1 :1:1, at a temperature of 150-200°C and a pressure of P = 4.5-5.0 MPa to obtain a mixture of Cß-Czo paraffins, which are suitable for isolation of, specifi- cally, gasoline and kerosene fractions of motor fuel.
The oligomerization of the individual olefins in the presence of a zeolite-containing cat- alyst, comprising at least 93% ZSM-5 modified by 3.5 to 7.0% Zn, or a zeolite-contain- ing catalyst, comprising at least 95% ZSM-5 modified by 3.5 to 5.5 % Zn and 0.1 to 1.5% Ce, differs significantly from the process where the Amberlite 15 is used. For ex- ample, when the catalyst, comprising at least 93% ZSM-5 modified by 3.5 to 7.0% Zn catalyst is used in the oligomerization of propylene, obtained from propyl alcohol, ole- fins in the range CsH1z, C7H14, CsH16, C9H1s, C10H2o, and S0 On up '(0 C24H4s are Ob- tained. Hydrogenation of the resulting oligomerization products leads to the production of the corresponding paraffins.
The mixture of primary and secondary Cz-Cs alcohols, obtained at the step 1.3 of the inventive method, is sent for dehydration to obtain the corresponding mixture of un- saturated Cz-Cs hydrocarbons. ln turn, unsaturated Cz-Cß hydrocarbons are used at the step 1.9 of the inventive method as a feedstock for the oligomerization process to obtain higher unsaturated 66-624 hydrocarbons or for the aromatization process to ob- tain Cw-Ciz aromatic hydrocarbons. Moreover, a mixture of primary and secondary C2- Cs alcohols, from step 1.3 of the inventive method, is supplied to step 1.12 of the in- ventive method to obtain Cv-Cie ethers.
Primary and secondary Cz-Cs alcohols are dehydrated in the presence of a heteroge- neous catalyst, gamma AlzOs, in a continuous-flow reactor at a temperature of 350 to 450°C and a pressure of 0.5 to 3.5, MPa.
Unsaturated 62-66 hydrocarbons and water are formed in the dehydration reactor. The reaction mixture from the reactor is fed to a separator to separate the unsaturated 62- 66 hydrocarbons from the water formed. The water is sent for utilization, and unsatu- rated 62-66 hydrocarbons are collected in the collecting tank for further processing. Then the mixture of unsaturated 62-66 hydrocarbons from the collecting tank is di- rected to the stage of oligomerization.
The unsaturated 62-66 hydrocarbons obtained at step three of the inventive method by dehydration of the corresponding 62-66 alcohols are directed to the oligomerization re- actor at step nine of the inventive method. Oligomerization of the unsaturated hydro- carbons is performed at a temperature of 250 to 350°6 and a pressure of 2.0 to 5.0 MPa in the presence of a heterogeneous, zeolite-containing catalyst, comprising at least 93% ZSM-5 modified by 3.5 to 7.0% Zn, or a zeolite-containing catalyst compris- ing at least 95% ZSM-5 modified by 3.5 to 5.5% Zn and 0.1 to 1.5% 6e.
Following laboratory tests, it was found that the selected heterogeneous zeolite-con- taining catalyst, comprising at least 93% ZSM-5 modified by 3.5 to 7.0% Zn, or a zeo- lite-containing catalyst, comprising at least 95% ZSM-5 modified by 3.5 to 5.5% Zn and 0.1 to 1.5% 6e are most active in the oligomerization of 62-66 olefins obtained from primary and secondary 62-66 alcohols. ln the course of oligomerization, the unsatu- rated 62-66 hydrocarbons are converted into 66-624 unsaturated hydrocarbons.
The unsaturated 66-624 hydrocarbons are then hydrogenated in the presence of the catalyst consisting of the oxides NiO, 6uO and 6r2O6 in a molar ratio of 1:1:1, at a tem- perature of 150 to 200°6 and a pressure of 3.0 to 5.0 MPa to yield a mixture of 66-624 paraffins. 66-624 paraffins obtained at step 1.9 of the inventive method are a feedstock for the production, at step 1.13 of the inventive method, of motor fuel, primarily kero- sene, as well as gasoline and diesel. lt should be noted that the kerosene, obtained by the inventive method, has a number of unique properties. Studies performed by the inventor, which included mass spec- troscopy, demonstrate that the composition of the kerosene, obtained solely from pro- pylene, contains more than 150 different 66-616 isomers and the linear hydrocarbons content is less than 5.0% mass. Such a kerosene, obtained solely from propylene, does not freeze at a temperature of minus 85°6, and also has a smoke point of more than 30 millimeters. 31 The unreacted at step 1.9 unsaturated Cz-Cs hydrocarbons are used as a feedstock at step 1.11 of the inventive method in the process of aromatization to obtain Cw-Ciz aro- matic compounds.
The unsaturated Cz-Cs hydrocarbons obtained by rectification of the unsaturated C6- C24 hydrocarbons are supplied to step 1.11 of the inventive method to the aromatiza- tion reactor. Furthermore, a mixture of olefins and paraffins C1-C4, obtained at step 1.1 of the inventive method, is fed to the source reaction mixture at step 1.11. Aromatiza- tion of the unsaturated Cz-Cs hydrocarbons is performed at a temperature of 350 to 450°C and a pressure of 0.5 to 2.0 MPa in the presence of a heterogeneous zeolite- containing catalyst, comprising at least 93% ZSM-5 modified by 3.5 to 7.0% Zn in a continuous-flow reactor. The laboratory tests have established that the selected cata- lyst is most active in the aromatization of primary C4-C5 olefins. ln the process of aro- matization, the unsaturated Cz-Cs hydrocarbons are converted into aromatic C7-C12 hy- drocarbons.
Cw-Ciz aromatic hydrocarbons of step 1.11 are sent to step 1.13 of the inventive method for the production of motor fuel. Furthermore, a mixture of gaseous products is produced in the process of aromatization of the unsaturated hydrocarbons Cz-Cs. This mixture of gaseous products, comprised by hydrogen and C1-C4 paraffins, is separated from the liquid phase and sent to step 1.2 of the inventive method for producing syn- thesis gas.
Yet another way of ethanol conversion into motor fuel, developed by the inventor, is to use the reaction of telomerization for producing secondary and tertiary alcohols Ca-Cs. The main source material for this process is ethanol along with secondary alcohols such as iso-propanol or sec-butanol obtained from ethanol. Ethanol and isopropanol are supplied from step 1.1 of the inventive method to step 1.4 for telomerization. Fur- thermore, this process uses, as a raw material, ethylene obtained by dehydration of ethanol at step 1.3 of the inventive method.
The catalyst used in the reaction of telomerization is peroxides of tertiary alcohols, in- cluding tert-butyl or tert-amyl alcohols. The ratio of the catalyst: tert-butyl or tert-amyl alcohol peroxide to ethanol or secondary alcohols by mass is (1 to 2)% mass of tert- butyl or tert-amyl peroxide to (98 to 99)% of ethanol or secondary alcohol. 32 The process is carried out while stirring a liquid mixture of tert-butyl or tert-amyl alcohol peroxide and ethanol or isopropanol or a mixture of these alcohols under a pressure of gaseous ethylene P = 1.0-5.0 MPa at a temperature of 100-130°C. Under these condi- tions, isopropanol is converted into tertiary Cs-Cg alcohols, while ethanol is converted into sec-butanol and tertiary alcohols Cß-Cio. Conversion of ethanol into tertiary alco- hols in this process was unexpected.
The obtained tertiary Cs-Cs alcohols are isolated from the reaction mixture by rectifica- tion. ln the process of rectification, individual tertiary alcohols or tertiary alcohol frac- tions are isolated. The yield of tertiary Cs-Cs alcohols in terms of the reacted source al- cohol reached more than 98% with a conversion rate of the initial alcohol higher than 60%. The yield of the obtained tertiary 68+ alcohols did not exceed 2% mass. The un- reacted source alcohols from telomerization were separated at the rectification stage and returned to the telomerization process or were used in the process of producing ethers. The resulting 68+ tertiary alcohols can be used as oxygen-containing additives in the production of gasoline or diesel.
The mixture of tertiary Cs-Cs alcohols obtained in the processes described above, is sent to step 1.5 of the inventive method for dehydration to obtain the corresponding mixture of unsaturated Cs-Cs hydrocarbons. Dehydration of tertiary Cs-Cs alcohols is carried out in the presence of a new or regenerated heterogeneous catalyst, gamma AlzOs at a temperature of 100 to 150°C and a pressure of 0.5 to 1.5 MPa until reaching the yield of Cs-Cs olefins of at least 99% of the source Cs-Cs alcohols. Then the tem- perature is increased to 350-450°C and primary and/or secondary alcohols Cz-Cs are dehydrated, wherein the process is continued in the presence of the same catalyst at a temperature not exceeding 450°C until reaching the yield of Cz-Cs olefins of not less than 99% of the source primary and/or secondary Cz-Cs alcohols.
Upon completion of the dehydration of primary and/or secondary Cz-Cs alcohols, the catalyst is regenerated.
Cs-Cß unsaturated hydrocarbons and water are obtained in the dehydration reactor. The reaction mixture from the reactor is directed to the separator for separation of the 33 mixture of unsaturated Cs-Cs hydrocarbons from the water obtained. The water is sent for utilization and the unsaturated Cs-Cs hydrocarbons are collected in the collecting tank for further processing. Further, the mixture of unsaturated Cs-Cß hydrocarbons from the collecting tank is directed to step 1.6 of the inventive method for oligomeriza- tion.
The inventor recommend to use ion-exchange resins in the form of cation exchangers, for example, Amberlite15, as catalysts for oligomerization of Cs-Cs olefins. Studies per- formed by the inventor have established that the use of Amberlite 15, as a catalyst in the process of oligomerization, obtains higher unsaturated compounds by way of con- densation of the source o|efin in the form ofdimers, trimers, and so on. That is, higher o|efins with a molecular weight as a multiple of the initial unsaturated compound ap- pear. For example, oligomerization of propylene in the presence of a cation exchanger Amberlite 15 yields o|efins CßHiz, C9H1s, C12H24, and so on up to C24H4s. Hydrogena- tion of the resulting oligomerization products yields the corresponding paraffins.
At the same time the use of Amberlite 15 at the stage of oligomerization along with a mixture of at least two o|efins: propylene and isobutylene, obtained from the corre- sponding alcohols, results in obtaining a mixture of higher olefins. Hydrogenation of said mixture of higher o|efins yields a mixture of higher paraffins in the range C6H14, C7H16, CsH1s, C9H2o, C10H22 and S0 On up '(0 C24H50.
Moreover, the unsaturated Cs-Cs hydrocarbons obtained at step 1.5 by dehydration of tertiary alcohols Cs-Cs are used at step 1.6 of the inventive method as a raw material in the reaction of oligomerization to obtain unsaturated hydrocarbons C1o-C24.
Oligomerization of the unsaturated hydrocarbons Cs-Cs is carried out in the presence of catalyst, ion-exchange resins in the form of cation exchangers, for example Amber- lite15, in a continuous flow reactor at a temperature of 70-120°C and a pressure of 1-2 MPa. Oligomerization of the unsaturated Cs-Cs hydrocarbons yields a mixture of higher unsaturated hydrocarbons C1o-C24.
The unsaturated C1o-C24 hydrocarbons of step 1.6 of the inventive method are then hy- drogenated at step 1.7 in the presence of a catalyst consisting of the oxides NiO, CuO 34 and CrzOß in a molar ratio of 1:1:1, at a temperature of 150 to 200°C and a pressure of 3.0 to 5.0 MPa, to obtain a mixture of C1o-C24 paraffins.
C1o-C24 paraffins obtained at step 1.7 are the source material for the production of mo- tor fuel, first of all, kerosene, as well as gasoline and diesel at step 1.13 of the in- ventive method. The iso-structure of these hydrocarbons obtains kerosene and diesel with unique characteristics, as well as gasoline free of aromatic compounds with oc- tane numbers of at least 95 RON and 91 MON. Studies carried out by the inventor, which included chromatomass spectroscopy, demonstrate that the composition of ker- osene, obtained from tertamyl alcohol, contains more than 60 different Cio-Cis isomers and there are no linear hydrocarbons. This kerosene, obtained from tertamyl alcohol, does not freeze at a temperature of minus 85°C, and also has a smoke point of more than 30 mm.
The inventive method for producing motor fuel provides for using tertiary Cs-Cs alco- hols, synthesized on the basis of ethanol, as a feedstock. For this purpose, Cs-Cß ole- fins are isolated by rectification from the mixture of Cs-Cs olefins of step 1.5, obtained by dehydration of tertiary alcohols Cs-Cs, and oligomerized at step 1.6 of the inventive method at a temperature of 70-120°C and a pressure of P = 1.5-2.0 MPa in the pres- ence of catalyst, ion exchange resins in the form of cation exchangers, for example Amberlite15.
Cio-Cls olefins obtained in the process of oligomerization are hydrogenated in a pres- ence of a heterogeneous catalyst consisting of the oxides NiO, CuO and CrzOs in a molar ratio of 1:1:1, at a temperature of 150-200°C and a pressure of P = 4.5-5.0 MPa to obtain a mixture of Cia-Cia paraffins, which almost entirely is a kerosene fraction of motor fuel.
Furthermore, Cw-Cs olefins isolated from the mixture of Cs-Cs olefins, obtained by de- hydration of tertiary Cs-Cs alcohols, are oligomerized at a temperature of 70-120°C and a pressure P = 1.5-2.0 MPa by using, as catalyst, ion-exchange resins in the form of cation exchangers, for example, Amberlite15. 614-624 olefins obtained as a result of oligomerization are hydrogenated in the pres- ence of a heterogeneous catalyst consisting of the oxides NiO, CuO and CrzOs in a molar ratio of 1:1:1, at a temperature of 150-200°C and a pressure of P = 4.5-5.0 MPa to obtain C14-C24 paraffins. Subsequently, kerosene and diesel fractions of the motor fuel are isolated from said hydrocarbon mixture by rectification.
The inventive method for producing motor fuel from ethanol makes it possible to pro- duce and use oxygen-containing additives, which, when used in gasoline and diesel compositions, improve significantly the quality of said compositions. The main oxygen- containing additives proposed herein to be used to improve properties of gasoline and diesel are ethers. lt is proposed to obtain these ethers by using primary of secondary Cz-Cs alcohols, ob- tained by the inventive method of the motor fuel production. Furthermore, the unsatu- rated Cs-Cg hydrocarbons, obtained by dehydration of tertiary alcohols Cs-Cß, can be used for producing said ethers.
The process for producing ethers is carried out at step 1.12 of the inventive method, in the presence of a catalyst, the ion-exchange resins in the form of cation exchangers, for example Amberlite15, in a continuous-flow reactor at a temperature of 50 to 100°C and a pressure of 0.5 to 1.5 MPa. Cz-Cs primary and secondary alcohols of step 1.3 of the inventive method, that are supplied to step 1.12, interact with Cs-Cs olefins, of step 1.5 of the inventive method, that are supplied to step 1.12, to yield a mixture of Cw-Cie ethers. The mixture of Cw-Ciß ethers is directed to step 1.13 of the inventive method for producing motor fuel.
As described above in the detailed description of the inventive method for ethanol con- version into motor fuel, the inventive technology provides for obtaining mixtures of par- affins in the 66-624 range, consisting mainly of branched hydrocarbons. These paraffin mixtures are separated by rectification into fractions Cß-Cio, Cn-Cis, and 619-624, suit- able for producing gasoline, kerosene and diesel. ln addition, the inventive technology for the production of aromatic compounds from ethanol provides for obtaining mixtures of aromatic hydrocarbons in the range Cv-Ciz. These mixtures of aromatic hydrocar- bons are separated by rectification into fractions Cw-Cs and Cg-Ciz, suitable for produc- ing gasoline and kerosene. Mixing the gasoline fraction of Cß-Cio paraffins with the gasoline fraction of Cw-Cs aromatic hydrocarbons provides for obtaining gasoline meet- ing all the requirements of the EN 228 standard. Mixing the kerosene fraction of C11- Cis paraffins with the kerosene fraction of aromatic C9-C12 hydrocarbons provides for obtaining kerosene meeting all the requirements of the Jet A-1 standard. 36 At the same time, the inventive technology for the production of ethers from ethanol provides for obtaining mixtures of ethers in the range 67-616. These mixtures of 67-616 ethers are separated by rectification into fractions 67-61o and 611-616, suitable for pro- ducing gaso|ine and diesel. Mixing the gaso|ine fraction of 66-619 paraffins with the gaso|ine fraction of 67-610 ethers provides for obtaining gaso|ine meeting requirements of the EN 228 standard and free of aromatic compounds, and with octane ratings RON of at least 100 and MON of at least 93. Mixing the diesel fraction of 619-624 paraffins with the diesel fraction of 611-616 ethers provides for obtaining diesel meeting require- ments of the EN 590 standard and completely free of aromatic hydrocarbons. 66-624 paraffins obtained from primary and secondary 62-66 alcohols at steps 1.8, 1.9 and 1.10 of the inventive method for conversion of ethanol into motor fuel, and 610-624 paraffins obtained from tertiary 66-66 alcohols at steps 1.5, 1.6 and 1.7 of the inventive method, are supplied to step 1.13 for rectification to obtain 66-619 gaso|ine, 611-616 kerosene, and 619-624 diesel fraction of the motor fuel. Moreover, aromatic 67-612 hy- drocarbons obtained from primary and secondary 62-66 alcohols at steps 1.3, 1.9 and 1.11 of the inventive method are supplied to step 1.13 for rectification to yield 67-66 gaso|ine and 69-612 kerosene fractions of the motor fuel. 67-66 aromatic hydrocarbons are used to produce gaso|ine meeting all requirements of the EN 228 standard. 69-612 aromatic hydrocarbons are used to produce kerosene meeting all the requirements of the Jet A-1 standard.
Also, 67-616 ethers, obtained at steps 1.3, 1.4, 1.5 and 1.12 from primary and second- ary 62-66 alcohols, and 66-66 olefins, obtained from tertiary 66-66 alcohols, are sup- plied to step 1.13 for rectification, and are separated into a mixture of 67-61o ethers and a mixture of 611-616 ethers. 67-619 ethers are used to produce a high-quality gaso- |ine, while 611-616 ethers are used to produce a high-quality diesel.
The use of the ethers obtained in the inventive process in the compositions of gaso|ine provides for excluding aromatic compounds from compositions of gaso|ine and for re- ducing the harmful effects of the gaso|ine combustion products on the environment. Up to 22% of ethers by volume are allowed in gaso|ine according to the current standards. However, it is necessary to comply with the oxygen content limit, which for various standards can be not higher that 2.7% by weight or 3.2% by weight. 37 The compositions of gasoline obtained by the invention with an ether content of not more than 20% by volume provide for achieving RON ratings of at least 100 and MON of at least 93, without violating the above requirements for oxygen content.
A distinguishing feature of the inventivew method for obtaining motor fuel from 66-624 paraffins, synthesized from ethanol, is that in order to obtain gasoline fully meeting the requirements of the existing EN 228 standard, the 66-610 paraffin fraction isolated from a mixture of 66-624 paraffins is mixed with a fraction of 61-610 ethers isolated from a mixture of 61-616 ethers, synthesized from ethanol, and/or with a fraction of 61-66 aro- matic hydrocarbons, isolated from a mixture of 61-616 aromatic hydrocarbons, which are also synthesized from ethanol. Wherein the 61-616 ethers required for mixing are obtained by etherification of primary or secondary 62-66 alcohols with 66-66 olefins ob- tained from tertiary 66-66 alcohols.
The esterification process is carried out in the presence of catalyst, which is an ion-ex- change resin in the form of cation exchanger, for example Amberlite15, at a tempera- ture of 70-120°6 and a pressure of P = 1.5-2.0 MPa. For the production of 61-616 ethers are used primary or secondary 62-66 alcohols, obtained from tertiary 66-66 al- cohols, and 66-66 olefins, wherein all raw material for the production of 61-616 ethers is obtained from ethanol.
According to one preferred embodiment of the inventive method, in order for obtaining motor fuel from 66-624 paraffins, synthesized from ethanol, in order to produce diesel fuel that meets all requirements of the existing EN 590 standard, the 619-624 paraffin fraction isolated from a mixture of 66-624 paraffins, is mixed with the fraction of 611-616 ethers, isolated from a mixture of 61-616 ethers, said 61-616 ethers are also synthe- sized from ethanol. Wherein, the 61-616 ethers required for the mixing are produced by etherification of primary or secondary 62-66 alcohols by 66-66 olefins, obtained from tertiary 66-66 alcohols.
The esterification is performed in the presence of catalysts, the ion-exchange resin in the form of cation exchangers, for example Amberlite15, at a temperature of 70-120°6 and a pressure of P = 1.5-2.0 MPa. For the production of 61-616 ethers are used pri- mary or secondary 62-66 alcohols, obtained from tertiary 66-66 alcohols, and 66-66 olefins, wherein all raw material for the production of 61-616 ethers is obtained from ethanol. 38 According to a preferred embodiment of the inventive method, in order to obtain kero- sene meeting all the requirements of the existing standard Jet A-1 from 66-624 paraf- fins (obtained at steps: 1.3, 1.8, 1.9 and 1.10 from primary and secondary alcohols 62- 66), from 610-624 paraffins (obtained at steps: 1.4, 1.5, 1.6 and 1.7 from tertiary 65-66 alcohols), and from aromatic 61-612 hydrocarbons (obtained at steps: 1.3, 1.9 and 1.11 from the primary and secondary 62-66 alcohols), the 611-616 paraffins required in the kerosene composition, obtained at step 1.10 and isoiated from the mixture of 66-624 paraffins at step 1.13, the 611-616 paraffins, obtained at step 1.7 and isoiated from the mixture of 610-624 paraffins at step 1.13, and the aromatic 69-612 hydrocarbons, ob- tained at step 1.11 and isoiated from the mixture of aromatic 61-612 hydrocarbons, are mixed so that the concentration of aromatic 69-612 compounds is in the range of 8- 25% vol, while the resulting kerosene composition comprises at least 100 different hy- drocarbons, and preferably 150 different hydrocarbons, and has a smoke point of min mm and a freezing point of max minus 80°6. lt should be noted that the inventive method for the production of motor fuel provides for using not only ethanol containing a significant amount of water, but also ethanol containing a large amount of fusel oils. Also, the inventive method for ethanol conver- tion into motor fuel can use carbon dioxide and methane, obtained during the produc- tion of ethanol, as an additional raw material.
Moreover, the inventive method is not limited only to the motor fuel production industry. The inventive method for converting ethanol into 66-66 containing aldehydes, ketones, alcohols: primary, secondary and tertiary, olefins, as well as 66-624 containing olefins and branched paraffins may be in demand in the chemical and cosmetic industries.
The implementation of the inventive method for producing motor fuels is demonstrated by the following examples.
Example 1. 6onversion of ethanol into a mixture of higher alcohols and hydrocarbons, as well as into synthesis gas.
The process of converting ethanol into a mixture of higher alcohols and hydrocarbons, as well as into synthesis gas, was carried out in a cascade of reactors filled with appro- priate heterogeneous catalysts. At the first step of the process, an aqueous solution of 39 ethanol was supplied into a one liter volume continuous flow reactor, where the cata- lyst was loaded. The catalyst consists of the following metal oxides: ZnO 60 to 63% mass.; CeOg 1 to 6% mass.; MgO 12 to 18% mass.; AlzOs 13-23 % mass, with the pro- portions calculated in terms of metal oxide. The technological parameters of the pro- cess varied within the following ranges: temperature 500 to 515°C, pressure 0.9 to 1.1 MPa, ethanol concentration in water 59 to 63% wt, load 0.45 to 0.77 kg of ethanol solu- tion in water per 1 liter of catalyst. The gaseous reaction mass obtained as a result of the interaction of ethanol with water was directed to step 1.2 of the process while the liquid reaction mass was directed to step 1.3 of the process.
The gaseous reaction mass, which is a mixture of hydrogen, carbon dioxide, saturated C1-C4 and unsaturated C2-C4 hydrocarbons, was supplied to step 1.2 of the process. This gaseous reaction mass was directed into a one liter volume continuous flow reac- tor filled with a heterogeneous zeolite-containing catalyst, comprising at least 93% ZSM-5 modified by 3.5 to 7.0% Zn catalyst. The technological parameters of the pro- cess varied within the following limits: temperature 350 to 450°C, pressure 0.5 to 1.0 MPa. Under these conditions, the C2-C4 olefins contained in the gaseous reaction mass were converted into aromatic compounds, and the obtained gas mixture was di- rected to the absorber to extract carbon dioxide. The gas mixture, free from carbon di- oxide, with a hydrogen content exceeding 95%, was directed to step 1.3 of the pro- CGSS.
At step 1.3 of the process, acetaldehyde was isolated from the liquid reaction mass ob- tained at step 1.1 of the process. After that the remaining liquid reaction mass was separated into organic and aqueous phases. The aqueous phase, containing unre- acted ethanol, is returned to the process to produce the aqueous ethanol solution. The organic phase, which is a mixture of Cs and G5 ketones and Cs and Cs alcohols, was directed to the step of hydrogenation. To do this, the mixture of oxygen-containing products of ethanol conversion was supplied into a 1-liter continuous flow reactor, equipped with the catalyst consisting of the oxides CuO and CrzOa in a molar ratio of 1:1. The technological parameters of the process varied within the following limits: tem- perature 100 to 150°C, pressure 0.5 to 0.9 MPa. The gas mixture obtained at the sec- ond step of this process was supplied into the reactor loaded with the catalyst, com- prixed by oxides CuO and CrzOs in a molar ratio of 1 :1, along with the mixture of the liquid oxygen-containing products of the ethanol conversion. Under these conditions, the Cs and G5 ketones contained in the liquid organic mixture were converted into the corresponding Cs and G5 alcohols. The residual unsaturated compounds were re- moved from the gas mixture obtained in the presence of the catalyst, comprised by ox- ides CuO and CrzOa in a molar ratio of 1:1, by hydrogenation. This gas mixture is an excellent raw material for synthesis gas production. Table 1 shows the results of a few experiments carried out in accordance with the described technological process for converting a mixture of ethanol and water into a mixture of alcohols, aromatic hydro- carbons, and also into synthesis gas.
Table 1. Results of experiments on the conversion of a mixture of ethanol and water in the presence of the catalyst consisting of the following metal oxides: ZnO 60 to 63% mass; CeOg 1 to 6% mass; MgO 12 to 18% mass; AlgOg 23 to 13% mass, with the pro- portions calculated in terms of metal oxide. 20193005 24 71.0 510 (1+/-0.1) 32.8 0.788 Supply Ethanol, kg Carbon in Water, kg ethanol, kg 26.480 13.816 15.286 Conversion % Ethanol, kg (%) 91.125 % 24.130 (91.125) 12.590 Consumption Acetaldehyde C1-C4 Cs alcohols, Aromatic C7-C11 Synthesis and isopropanol, hydrocarbons, kg (including kg (including gas kg kg (Carbon in kg (including carbon, kg) carbon, kg) (Carbon in acetaldehyde carbon, kg) carbon and isopropanol, dioxide, Kg) kg) 10.759 (6.452) 1.089 (0.891) 2.346 (1.663) 0. 211 (0.190) 8.920 (3.329) Yield %, 51.25 7.08 13.21 1.51 26.44 *) notes Experiment # Experiment Alcohol Reaction Rate of ethanol Load per 1 duration in concentration, temperature, solution supply, liter of hours % vol. °C ml/min catalyst (Pressure, l/hour of MPa) ethanol solution 41 20190206 24 70.8 515 (1+/-O.1) 37.4 0.898 Supply Ethanol, kg Carbon in Water, kg ethanol, kg 30.106 15.707 17.380 Conversion % Ethanol, kg (%) 84,18 % 25.344 (84.18) 13.223 Consumption Acetaldehyde C1-C4 Cs alcohols, Aromatic C7-C11 Synthesis and isopropanol, hydrocarbons, kg (including kg (including gas, kg kg (Carbon in kg (including carbon, kg) carbon, kg) (Carbon in acetaldehyde carbon, kg) carbon and isopropanol, dioxide, Kg) Kg) 11.056 (6.750) 1.068 (0.878) 2.114 (1.787) 0.222 (0.200) 9.568 (3.587) Yield %, 51.05 6.64 13.51 1.51 27.13 *) notes 20192903 24 65.8 500 (1+/-O.1) 22.1 0.518 Supply Ethanol, kg Carbon in Water, kg ethanol, kg 16.501 8.609 11.419 Conversion % Ethanol, kg (%) 99,01 % 16.337 (99.01) 8.523 Consumption Acetaldehyde C1-C4 Cs alcohols, Aromatic Cv-Cn Synthesis and isopropanol, hydrocarbons, kg (including kg (including gas, kg kg (Carbon in kg (including carbon, kg) carbon, kg) (Carbon in acetaldehyde carbon, kg) carbon and isopropanol, dioxide, Kg) Kg) 6.633 (4.013) 0.677 (O.549) 1.480 (1.045) 0. 819 (O.737) 5.592 (2.097) Yield '3/0, 47.08 6.44 12.26 8.65 24.6 *) notes Note *): the yield of final products is calculated in terms of the carbon contained in ethanol reacted with water according to the Conversion. 42 Example 2. Synthesis gas generation in the presence of copper and nickel catalysts.
Synthesis gas, obtained on the basis of the inventive technology, is used in the inventive process of hydroformylation of ethylene and propylene.
For the production of synthesis gas, carbon dioxide and hydrogen obtained in the conversion of ethanol to acetone are used. Carbon dioxide is disti||ed off from the liquid reaction mass in the process of acetaldehyde distillation. ln addition, carbon dioxide is extracted from the absorbent solution obtained during the purification of hydrogen, which is supplied to the stage of hydrogenation of acetone and other oxygen- containing compounds. The gas mixture leaving the stage of hydrogenation contains more than 90% hydrogen and is an excellent raw material for the production of synthesis gas by the inventive technology. The synthesis gas thus obtained is used in the process of ethylene and propylene hydroformylation.
The synthesis gas production by the inventive technology is carried out by two methods. ln the first method, carbon dioxide and mixture of 90% hydrogen in a molar ratio of CO2:H2 = 1:(1.1-1.5) are fed into a flow reactor filled with a granular catalyst of 5 to 10% Cu supported on AlzOs at a temperature of 550 to 600°C and a pressure of 3.0 to 5.0 MPa. The carbon monoxide obtained in this process is cooled and isolated from water and a mixture of C1-C4 paraffins. The carbon monoxide, free of water, and the mixture of C1-C4 paraffins is directed to the hydroformylation reactor. Simultaneously with carbon monoxide, hydrogen is fed into the hydroformylation reactor in a molar ratio of CO:H2 =1:1. ln the second method, carbon dioxide and hydrogen in a molar ratio of CO2:H2 = 1:(2- 3) are fed into a flow reactor filled with a granular catalyst consisting of the oxides NiO, CuO and CrzOs in a molar ratio of 1:1:1, at a temperature of 950 to 1000°C and a pressure of 0.1 to 0.5 MPa. The mixture of carbon monoxide and hydrogen obtained in this process is cooled, isolated from water, carbon dioxide and methane, and then sent to the synthesis gas collecting vessel to adjust the composition. Simultaneously with the mixture of carbon monoxide and hydrogen, hydrogen is fed into the synthesis gas collecting vessel to adjust the molar ratio of CO:H2 = 1:1. From the synthesis gas collecting vessel the mixture of carbon monoxide and hydrogen in a molar ratio of 43 CO:H2 = 1:1 is sent to the hydroformylation reactor by a Compressor at a pressure of 3.0 to 5.0 MPa.
Example 3. Obtaining di tert-amyl peroxide.
Under vigorous stirring, tert-amyl alcohol is added to an aqueous solution of 70% sulfuric acid, cooled to a temperature of 0 to 5°C, in a molar ratio of H2SO4:(CHs)2C(OH)CH2CH3 = 1:1 _ After adding the entire amount of tert-amyl alcohol the resulting reaction mass is stirred at a temperature of 0 to 5°C for 10 to 15 minutes.
Then, an aqueous solution of 27% hydrogen peroxide is added to the resulting tert- amyl sulfate at a temperature of 0 to 5°C, with vigorous stirring, in a molar ratio of tert- amyl sulfate to hydrogen peroxide: (CHs)2C(HSO4)CH2CHs:H2O2 = 1:0.5. After adding the entire amount of 27% hydrogen peroxide, the reaction mixture is further stirred at a temperature of 5 to 20°C for 60 minutes.
After the stirring is finished the reaction mass is divided into two layers. The upper layer, containing the formed di-tert-amyl peroxide is separated from the aqueous acidic layer and washed under stirring by a 10% aqueous solution of potassium carbonate and then by water to pH of 7. The crude di-tert-amyl peroxide washed from acid and alkali to neutral reaction is distilled under vacuum, at a pressure of 10 to 15 mm Hg, to collect the fraction boiling at 40 to 45°C. The yield of di tert-amyl peroxide after distillation is not less than 65%.
Example 4. Radical addition of ethylene to isopropanol. ln a 2000 ml volume reactor, a steel autoclave of type "PARR", were placed 470 ml of isopropyl alcohol (369 g, 6.15 mol) and 4 g ofdi-tert-amyl peroxide. The reactor was purged 3 times by nitrogen at 5 atm and 2 times by ethylene at 5 atm. After purging, 12 to 15 liters of ethylene was fed into the reactor and the internal temperature was increased to 130 to 135°C. Absorbtion of ethylene begins at this temperature. While ethylene was being absorbed an additional amount of ethylene was fed in at a rate of 0.1 to 0.2 liters per minute to maintain the pressure in the system at 12 to 14 atm. About 30 to 32 liters of ethylene were absorbed during 4 hours of reaction. Then the reactor was cooled and an additional 4 g of di-tert-amyl peroxide was added. the 44 autoclave was reheated to 130 to 135°C while maintaining the pressure in the system at 12 to 14 atm by feeding in ethylene. During 4 hours of reaction, an additional 20 to 22 liters of ethylene were absorbed. After cooling the reactor, 4 g of di-tert-amyl peroxide were added again and the experiment was repeated. During the entire experiment 84 liters, (105 g) of ethylene were consumed and 600 ml (480 g) of the product were obtained.
The mixture of alcohols in the amount of 600 ml thus obtained in the reaction of telomerization was subjected to distillation. After distillation at atmospheric pressure and a temperature of 80 to 90°C, 250 ml of isopropyl alcohol were obtained. The subsequent distillation yielded 340 ml of tertiary alcohols boiling at 100 to 250°C and 10 ml of tertiary alcohols boiling at a higher temperature, which remained in the bottoms. The yield of tertiary alcohols obtained from the reacted isopropyl alcohol, ethylene and tert-amyl peroxide was more than 99%.
The yield of tertiary Cs-Cv alcohols was about 80%, and the yield of tertiary Cg-Cn alcohols was about 17.1 %. According to GLC analysis, the following was obtained: tert-amyl alcohol 57.4%; tert-heptyl alcohol 226%; tert-nonyl alcohol 11.4%, tert- undecyl alcohol 5.7% and tert-C11+ alcohols 2.9%. The conversion of isopropyl alcohol reached about 50%. These experiments were carried out with a "deficiency" of ethylene in order to avoid formation of heavier telomeres.
Example 5. Radical addition of ethylene to ethyl alcohol. 408 ml (322 g, 7.0 mol) of ethyl alcohol and 45 ml (37 g, 0.21 mol) ofdi tert-amyl peroxide were placed in a 2000 ml volume reactor, a steel autoclave of type "PARR". The reactor was purged 3 times by nitrogen at 5 atm and 2 times by ethylene at 5 atm. Then, 12 liter (0.5 mol) of ethylene was fed into the reactor and the internal temperature was increased to 130 to 135°C. At this temperature absorbtion of ethylene begins. While ethylene was being absorbed at 130 to 135°C, an additional amount of ethylene was fed in at a rate of 0.1 to 0.3 liters per minute to maintain the pressure in the system at 12 to 14 atm. During 8 hours of the reaction, about 95 liters, (119 g, 4.25 mol) of ethylene were absorbed. Then the reactor was cooled, the reaction mixture was unloaded and transferred to distillation. The above experiment was repeated twice. ln total, 1224 ml, (966 g, 21 mol) of ethyl alcohol and 135 ml, (111 g, 0.64 mol,) of di tert-amyl peroxide were consumed to perform the reaction of telomerisation, while 285 liter (356 g, 12.71 mol) of ethylene were absorbed. ln total, 1793 ml (1433 g) of alcohol mixture was obtained.
The mixture of alcohols in the amount of 1793 ml obtained as a result of the telomerization reaction was distilled. Distillation at atmospheric pressure and a temperature of 80°C yielded 776 ml (612 g, 13.3 mol) of ethyl alcohol. Further distillation at atmospheric pressure and a temperature of 98°C yielded 450 ml (364 g, 4.95 mol) of sec-butyl alcohol. Further distillation at atmospheric pressure additionally yielded 528 ml (425 g) of tertiary Cs-Cs alcohols boiling between 102 and 180°C, and 30 ml (25 g) of tertiary alcohols boiling at higher temperatures, which remained in the bottoms.
The yield of secondary butyl alcohol and tertiary alcohols obtained from the reacted ethyl alcohol, ethylene and di-tert-amyl peroxide was more than 99%. The yield of secondary butyl alcohol was 44.3%. The yield of tertiary Cs-Cg alcohols was 51 .8%, and the yield of tertiary Cio-Ciz alcohols was about 3.0%. The rate of ethyl alcohol conversion was about 37%.
Example 6. Hydroformylation of ethylene in the presence of a rhodium catalyst.
The process of ethylene hydroformylation is carried out in a heterogeneous reaction medium using a water-soluble rhodium catalyst.
During hydroformylation of ethylene in the presence of a rhodium catalyst, the concentration of metal with respect to the aqueous phase is from 30 to 50 ppm. Triphenylphosphine-3-sulfonic acid sodium salt is used as a ligand in a ratio of 30:1 to metallic rhodium.
The process of obtaining propionic aldehyde is carried out at a temperature of 45 to 90°C and a pressure of 1.0 to 2.5 MPa. The ratio of the source gases: C2H4:CO:H2 = (0.9-1):1:1 is maintained by flow meters. The resulting reaction mass is directed to a highly efficient separator where it is separated into three phases: a gas phase containing non-reacted ethylene, carbon monoxide and hydrogen, a liquid organic phase containing mainly propanal, and a liquid aqueous phase containing a water- 46 soluble rhodium catalyst. The gas phase and the liquid aqueous phase are returned to the hydroformylation reactor by metering devices.
An aqueous solution of the catalyst was loaded into a 2000 ml volume reactor with a highly efficient stirring device. The catalyst was then activated as follows. Synthesis gas was supplied in the ratio CO:H2 = 1:1 into the reactor whilst stirring the catalyst solution until a pressure of 1 .0 MPa was reached, after which the heating was switched on and the temperature was increased to 60 to 70°C. The catalyst solution was stirred for one hour at this temperature. Upon completion of catalyst activation, an automatic mode of the reaction temperature and pressure limit control was switched on at the instrument panel, which terminates supply of the reaction gases to the reactor. To prevent heating of the reaction mixture to a temperature critical for catalyst operation, the reactor is equipped with a refrigerator providing for removal of the excess heat. Water is used as the refrigerant. The gas supply rates for ethylene, carbon monoxide, and hydrogen were set at the flow meters installed on the gas supply lines into the reactor, and after that the gas supply to the reactor was switched on. After reaching the required volume of liquid reaction mass in the reactor, the pump was turned on to provide continuous pumping of the excess reaction mass to the separator. The separator separated the vapour and liquid phases, as well as separated the liquid phase into an organic phase containing propionic aldehyde and an aqueous phase containing dissolved catalyst.
The optimum temperature for the process of hydroformylation is 45 to 90°C at a pressure of 1.0 to 2.5 MPa. With a decrease in temperature below 45°C, a significant decrease in the yield of the target aldehyde was observed in all experiments. With an increase of temperature above 90°C, a decrease in conversion was also observed, however it was less significant. The experiments were carried out in the range of pressures of 1.0-2.5 MPa. lt should be noted that all experiments were performed using one and the same sample of catalyst developed by the inventor. During the study, the catalyst was repeatedly separated from the reaction products and returned to the process. lts total service life exceeded 9000 hours. The catalyst demonstrated high selectivity in the experiments on ethylene hydroformylation. Conversion of the reaction gases at the optimal technological parameters exceeded 99.0%, the selectivity for aldehyde was higher than 99.5%. 47 Example 7. Aldol condensation of propanal and obtaining propyl and 2-methylpentyl alcohols.
Propanal obtained in the hydroformylation of ethylene by synthesis gas in the presence of a rhodium catalyst was supplied at a temperature of 100 to 150°6 and a pressure of 0.5 to 1.0 MPa into a one-liter flow reactor |oaded with a granular catalyst containing at least 93% of ZSM-5 zeolite modified by 3.5 to 7.0% Zn. These conditions provide for aldol condensation of propanal and obtaining 2-methyl pentenal and 66+ products of propanal condensation. The reaction mass obtained in the process of aldol condensation was supplied for hydrogenation into a flow reactor, where the catalyst containing oxides NiO, 6uO and 6r2O6 in a molar ratio of 1:1:1 was |oaded. Simultaneously with the reaction mass of the aldol condensation process, hydrogen is also supplied to the said reactor, equipped with catalyst consisting of the oxides NiO, 6uO and 6r2O6 in a molar ratio of 1:1:1, at a temperature of 90 to 130°6 and a pressure of 4.0 to 5.0 MPa.
By way of hydrogenation, 2-methyl pentenal as well as the unreacted propanal and the resulting 66+ products of condensation are converted into 2-methylpentanol, propyl alcohol, and 66+ alcohols, respectively.
The rate of propanal conversion into 2-methyl pentenal in the process of aldol condensation was at least 50%. The total yield of the corresponding alcohols, propyl, 2-methyl pentyl, and 66+ alcohols, in the hydrogenation of a mixture of propanal, 2- methyl pentenal, and 66+ products of propanal condensation, exceeded 99%.
Example 8. Hydroformylation of ethylene using a cobalt catalyst.
The hydroformylation of ethylene is performed in a heterogeneous reaction medium in the presence of a water-soluble cobalt catalyst.
During hydroformylation of ethylene in the presence of a cobalt catalyst, the concentration of metal in relation to the aqueous phase is from 0.1 % to 0.15%. Triphenylphosphine-3,3',3"-trisulfonic acid trisodium salt is used in the weight ratio :1 to metallic cobalt as a ligand.
The process of obtaining propionic aldehyde is performed at a temperature of 120 to 140°6 and a pressure of 3.0 to 5.0 MPa. The ratio of the source gases: 62H4:6O:H2 = 48 (0.9-1):1:1 is maintained by flow meters. The resulting reaction mass is directed to a highly efficient separator for separation into three phases: a gas phase containing unreacted ethylene, carbon monoxide and hydrogen, a liquid organic phase containing resulting products of chemical conversions; propanal, 2-methyl pentenal, 2-methyl pentanal and 66+ products of propanal condensation, and a liquid aqueous phase containing a water-soluble cobalt catalyst. The liquid aqueous phase is returned to the hydroformylation reactor by metering pump. The gas phase is directed to the stage of synthesis gas production.
The liquid organic phase from the separator is directed to the rectification column for isolation of the reaction products: propanal, 2-methyl pentenal, 2-methyl pentanal and 66+ products of propanal condensation, as well as water dissolved in this organic phase.
The organic products isolated at the rectification column were sent to hydrogenation to obtain the corresponding alcohols. lsolated at the rectification column water, dissolved in organic matter, accumulates at the bottom of the column and is periodically pumped into the hydroformylation reactor by a pump.
An aqueous solution of the catalyst was put in a 2000 ml reactor with a highly efficient stirring device. The catalyst was then activated. The activation was done as follows. Synthesis gas was supplied into the reactor in the ratio CO:H2 = 1:1, while stirring the catalyst solution, until a pressure of 2.0 MPa was reached. Then the heating was switched on and the temperature was increased to 120 to 130°C. The catalyst solution was stirred at this temperature for two hours. Upon completion of catalyst activation, an automatic mode of reaction temperature and pressure limit control was switched on at the instrument panel, which terminates supply of the reaction gases to the reactor. To prevent heating of the reaction mixture to the critical temperature of catalyst operation, the reactor is equipped with a refrigerator for removal of the excess heat. Water is used as a refrigerant. The gas supply rates for ethylene, carbon monoxide, and hydrogen were set at the flow meters installed on the gas supply lines into the reactor, and then the gas supply to the reactor was switched on. After reaching the required volume of liquid reaction mass in the reactor, the pump was turned on to provide continuous pumping of the excess reaction mass to the separator. The separator separated the vapor and liquid phases, and also separated the liquid phase into an organic phase containing propanal; 2-methyl pentenal; 2-methyl pentanal and 49 66+ products of propanal condensation, and into water, in which the Catalyst is dissolved.
The optimum temperature for the hydroformylation process is 120 to 130°6. A decrease in temperature below 120°6 results in a significant decrease in the yield of the target products in all experiments. An increase of the temperature above 130°6 also results in a decrease of the conversion rate, though less significant. The experiments were carried out over the pressure range of 3.0 to 5.0 MPa. lt should be noted that all experiments were carried out on one and the same sample of the inventive catalyst. During the study, the catalyst was repeatedly isolated from the reaction products and returned back to the process. lts total service life exceeded 1200 hours. The catalyst demonstrated high selectivity in the experiments on ethylene hydroformylation. Conversion of the reaction gases at optimal technological parameters was higher than 98.0%, the selectivity for propanal reached 99.0%, and the selectivity for the totality of the products of propanal aldol condensation, that is 2- methyl pentenal, 2-methyl pentanal and the products of 66+ propanal condensation reached 50%.
Example 9. Obtaining propyl, 2-methylpentyl and 66+ alcohols.
Propanal, 2-methyl pentenal, 2-methyl pentanal and the products of 66+ propanal condensation, obtained in the hydroformylation of ethylene by synthesis gas in the presence of a cobalt catalyst, were supplied at a temperature of 150 to 200°6 and a pressure of 4.0 to 5.0 MPa into a continuous flow, one liter reactor where a granular catalyst consisting of the oxides NiO, 6uO and 6r2O6 in a molar ratio of 1:1:1, is loaded. Simultaneously with propanal, 2-methyl pentenal, 2-methyl pentanal and the 66+ products of propanal condensation, hydrogen is also supplied into the reactor. By way of hydrogenation, propanal, 2-methyl pentenal, 2-methyl pentanal, and the 66+ propanal condensation products are converted into propyl, 2-methylpentyl, and 66+ alcohols, respectively. The total yield of the corresponding alcohols: propanol, 2- methyl-pentanol, and 66+ alcohols in the process of hydrogenation of a mixture of propanal, 2-methyl pentenal, 2-methyl pentanal, and 66+ propanal condensation products exceeded 99%.
Example 10. Hydroformylation of propylene in the presence of a cobalt Catalyst.
The process of propylene hydroformylation is performed in a heterogeneous reaction medium using a water-soluble cobalt catalyst. During hydroformylation of propylene in the presence of a cobalt catalyst, the concentration of metal in relation to the aqueous phase is from 0.25%mass. to 0.5% mass. Triphenylphosphine-3-sulfonic acid sodium salt is used as a ligand in a weight ratio of 7:1 to metallic cobalt. To increase the rate of the propylene hydroformylation, as well as to increase the yield of isobutanal, ethanol is added to the water-soluble cobalt catalyst in the volume ratio of H2O:C2H5OH = (0.75-0.65):( 0.25-0.35).
The process of obtaining butyric aldehydes is carried out at a temperature of 135°C to 140°C and a pressure of 3.0 to 5.0 MPa. The ratio of the source gases: C3H6:CO:H2 = (0.9:1):1:1 is maintained by flow meters. The resulting reaction mass is directed to a highly efficient separator where it is separated into three phases: vapor, liquid organic and liquid water phase. The vapor phase containing the unreacted propylene, carbon monoxide and hydrogen is sent to the stage of synthesis gas production.
The liquid organic phase obtained in the chemical conversion, containing butanal, isobutanal, 2-ethyl hexenal, 2-ethyl hexanal, and the 08+ products of butanal condensation, is transferred from the separator to the rectification column. The rectification column is used to separate the following reaction products: butanal, isobutanal, 2-ethyl hexenal, 2-ethyl hexanal, 68+ products of butanal condensation, and water dissolved in this organic phase.
The liquid aqueous phase containing the water-soluble cobalt catalyst is returned back to the hydroformylation reactor by metering pump.
Organic products isolated by rectification were sent to hydrogenation to obtain the corresponding alcohols. lsolated by the distillation column water, dissolved in organic matter, accumulated in the bottom of the column and was periodically supplied by the pump to the hydroformylation reactor.
The experiments were carried out as follows. An aqueous solution of the catalyst was loaded into a 2000 ml reactor with an integrated highly efficient stirring device. The catalyst was then activated, it was done as follows. Synthesis gas was supplied in the ratio CO:H2 = 1:1 into the reactor whilst stirring of the catalyst solution until a pressure of 2.0 MPa was reached, after which the heating was switched on and the temperature was increased to 140°C. The Catalyst solution was stirred for two hours at this temperature. Upon completion of the catalyst activation, an automatic mode of control of reaction temperature and pressure limit was switched on at the instrument panel, which terminated supply of the reaction gases to the reactor. To prevent heating of the reaction mixture to the critical temperature of catalyst operation, the reactor is equipped with a refrigerator for removal of the excess heat. Water is used as a refrigerant. The gas supply rates for propylene, carbon monoxide, and hydrogen were set at the flow meters installed on the gas supply lines to the reactor and the gas supply was switched on. After reaching the required volume of liquid reaction mass in the reactor, the pump was turned on to provide continuous pumping of the excess reaction mass to the separator. The separator separated the vapor and liquid phases, as well as separated the liquid phase into an organic phase containing butanal, isobutanal, 2-ethyl hexenal, 2-ethyl hexanal, and the 08+ products of 2-ethyl hexanal condensation, and into an aqueous phase containing dissolved catalyst. lt should be noted that the ratio of butanal and isobutanal formed in the reaction mass during the entire experiment was within the ratio (n-C4HsO):(iso-C4H8O) = (2-3):1.
The optimum temperature for the hydroformylation process is 138 to 140°C. The experiments were performed over the pressure range of 3.0 to 5.0 MPa. lt should be noted that all experiments were performed by using one and the same sample of the developed catalyst. ln the course of the studies performed by the inventor, the catalyst was repeatedly separated from the reaction products, and returned back to the process. lts total service life exceeded 240 hours. The catalyst demonstrated high selectivity in the experiments on the hydroformylation of propylene. Conversion of the reaction gases at the optimal technological parameters was above 98.0%, the selectivity for butyric aldehydes reached 99.0%. Moreover, the selectivity for the totality of the products of n-butanal aldol condensation: 2-ethyl hexenal, 2-ethyl hexanal, and the 08+ products of the 2-ethyl hexanal condensation exceeded 60%.
Example 11. Obtaining butyl, isobutyl, and 2-ethylhexyl alcohols.
Butanal, isobutanal, 2-ethyl hexenal, and 2-ethyl hexanal, obtained in the hydroformylation of propylene by synthesis gas in the presence of a cobalt catalyst, were isolated from the reaction mixture by rectification. The mixture of oxygen- containing products thus obtained was supplied at a temperature of 90 to 130°C and a pressure of 4.0 to 5.0 MPa to a one-liter flow reactor where a granular Catalyst, containing oxides NiO, 6uO and 6r2O6 in a molar ratio of 1:1:1 was loaded. Hydrogen was also fed to the reactor simultaneously with butanal, isobutanal, 2-ethyl hexenal and 2-ethyl hexanal. ln the course of hydrogenation, butanal, isobutanal, 2-ethyl hexenal, and 2-ethyl hexanal are converted to butyl, isobutyl, and 2-ethyl hexyl alcohols, respectively. The total yield of the corresponding alcohols, that is butyl, isobutyl, and 2-ethyl hexyl alcohol exceeded 99%.
Example 12. Obtaining kerosene from propyl alcohol.
Propyl alcohol is dehydrated in contact with the gamma AI2O6 catalyst at a temperature of 350 to 400°6 and a pressure of 1.0 to 2.0 MPa. The obtained propylene (66H6) is separated from water and directed at a temperature of 250-350°6 and a pressure of 3.0-5.0 MPa into a continuous flow reactor, equipped with the granular catalyst, containing at least 93% of ZSM-5 zeolite modified by 3.5 to 7.0% Zn, or a granular catalyst containing at least 95% of ZSM-5 zeolite modified by 3.5 to 5.0% Zn and 0.1 to 1.5% 6e. These conditions provide for oligomerization of propylene to yield 66-624 olefins. Unreacted propylene is separated by distillation from the reaction mass of the oligomerization process and returned back to the process. The reaction mass, free of the source propylene, is directed for hydrogenation to a continuous flow reactor equipped with the granular catalyst consisting of the oxides NiO, 6uO and 6r2O6 in a molar ratio of 1:1:1. Simultaneously with the products of oligomerization, hydrogen at 120-150°6 and a pressure of4.0-5.0 MPa is supplied to the hydrogenation. The process of hydrogenation provides for the conversion of the unsaturated 66-624 compounds obtained at the stage of oligomerization into 66-624 paraffins. The reaction mass obtained at the stage of hydrogenation goes to rectification for separation into kerosene, as well as gasoline and diesel fractions.
Table 2 shows the main properties of the kerosene fraction free of aromatic compounds.
Table 2. Jet fuel characteristics of Example 12.
Acid Number ASTM D 3242 mg KOH/g Max 0.015 0,003 Density at 15°C ASTM D 4052 kg/m 3 775 - 840 762,5 Mono-Aromatics Content ASTM D 6379 % vol Min 8 Max 25 < 0.1 Olefines ASTM D 1319 % vol 0,3 Distillation IBP ASTM D 86 °C 161,7 Temperature @ 10% rec. ASTM D 86 °C Max 205 177,0 Temperature @ 50% rec. ASTM D 86 °C 183,8 Temperature @ 90% rec. ASTM D 86 °C 234,2 Distillation FBP ASTM D 86 °C Max 300 250,9 Residue ASTM D 86 % vol Max 1.5 1,2 Loss ASTM D 86 % vol Max 1.5 0,2 Sulphur Content ASTM D 5453 mg/kg Max 0.3 O 1 < _ Flash Point Abel IP 170 °C Min 38 50,0 Freezing Point ASTM D 2386 °C Max minus 47 < minus 81 Gum, Existent ASTM D 381 mg/100ml Max 7 < 1 Smoke Point ASTM D 1322 mm Min 25 33 Water Reaction ASTM D 1094 1b Water Separation Index (MSEP) ASTM D 3948 Min 85 98 Particulate Contaminant Lab. Test ASTM D 5452 mg/I Max 10 0,43 Copper strip corrosion ASTM D 130 2hl100°C class 1 1A Color(Saybolt) ASTM D 156 Min 25 30 Conductivity (no antistatic agent) ASTM D 2624 pS/m Max 600 < 1 JFTOT ASTM D 3241 2.5h 260°C, Max 25 < 1 mmHg JFTOT ASTM D 3241 Rating Max 85 23 JFTOT ASTM D 3241 ml 465 JFTOT ASTM D 3241 °C Min 325 325 BOCLE ASTM D 5001 WSD mm Max 0.85 0,84 Specific Energy ASTM D 3338 MJ/kg Min 42.8 44,06 ASTM D 445 Max 8.0 Viscosity @-20°C mmz/s 4,895 The study performed by the inventor using chromatography-mass spectroscopy demonstrates, that the composition of kerosene, obtained solely from propylene, contains more than 160 different Cs-Ciß isomers, wherein 4.7 wt. % of those are linear hydrocarbons.
Example 13. Obtaining kerosene from isobutyl alcohol. lsobutyl alcohol obtained by hydroformylation of propylene and subsequent hydrogenation of the resulting isobutyraldehyde is dehydrated in contact with the gamma AlzOs catalyst at a temperature of 350 to 400°C and a pressure of 1.0 to 2.0 MPa. The isobutylene (C4H8) obtained is separated from water and supplied at a temperature of 250 to 350°C and a pressure of 3.0 to 5.0 MPa into a continuous flow reactor, equipped with granulated catalyst containing at least 95% zeolite ZSM-5 modified by 3.5-5.0% Zn and 0.1-1.5% Ce. These conditions provide for oligomerization of isobutylene to yield Cs-Czo olefins. The unreacted isobutylene is distilled off the reaction mass obtained by oligomerization and returned back to the process. The reaction mass, free from the source isobutylene, is supplied for hydrogenation to the continuous flow reactor, equipped with catalyst consisting of the oxides NiO, CuO, and CrzOa in a molar ratio 1:1 :1. Simultaneously with olefins obtained by oligomerization, hydrogen is supplied into the hydrogenation reactor at a temperature of 120 to 150°C and a pressure of 4.0 to 5.0 MPa. By means of hydrogenation, the unsaturated Cs-Czo compounds obtained at the stage of oligomerization are converted into Cs-Czo paraffins. The reaction mass obtained at the stage of hydrogenation is directed to rectification for separation into kerosene, as well as gasoline and diesel fractions.
Example 14. Obtaining kerosene from tert-amyl alcohol.
Tert-amyl alcohol (2-methyl-2-butanol) is dehydrated in contact with gamma Al2Os Catalyst at a temperature of 100-150°6 and a pressure of 1.0 to 2.0 MPa. The pentenes (65H10) obtained are separated from water and supplied at a temperature of 100-150°6 and a pressure of 1 .0 to 2.0 MPa into a continuous flow reactor, equipped with an ion-exchange resin in the form of a cation exchanger Amberlite 15, as catalyst. These conditions provide for oligomerization of pentenes to yield 610-620 olefins. The unreacted pentenes are distilled off the reaction mass obtained by oligomerization and returned back to the process. The reaction mass, free of the source pentenes, is supplied for hydrogenation into a continuous flow reactor, equipped with the catalyst comprised by oxides NiO, 6uO, and 6r2O3 in a molar ratio 1:1 :1. Simultaneously with the oligomerization products, hydrogen at a temperature of 120 to 150°6 and a pressure of 4.0 to 5.0 MPa is supplied to the hydrogenation reactor. The unsaturated 610-620 compounds obtained at the oligomerization stage are hydrogenated into 610- 620 paraffins. The yield of 610-620 paraffins in terms of oligomerized pentenes is above 98%. The reaction mass obtained at the stage of hydrogenation is then separated by rectification into kerosene, as well as gasoline and diesel fractions, free of aromatic compounds. The iso- structure of the 610-620 paraffins provides for producing kerosene and diesel demonstrating unique properties, as well as gasoline with octane number RON of at least 95 and an octane number MON of at least 91. Results of the studies by using chromatography-mass spectroscopy demonstrate, that the kerosene obtained from tert-amyl alcohol contains 45 different 610-615 isomers and is free of linear hydrocarbons. Kerosene, obtained from tert-amyl alcohol, does not freeze at minus 85°6, and has a Smoke point of 33 millimeters.
Example 15. Obtaining kerosene from 2-methyl-1-pentanol. 2-methyl pentyl alcohol is dehydrated in contact with the catalyst gamma Al2Os at a temperature of 350 to 450°6 and a pressure of 1 .0 to 2.0 MPa. The hexenes (60H12) obtained by dehydration of alcohol are separated from water and supplied at a temperature of 250 to 350°6 and a pressure of 3.0 to 5.0 MPa into a continuous flow reactor, equipped with the catalyst containing at least 95% of ZSM-5 zeolite modified by 3.5 -5.0% Zn and 0.1-1.5% 6e. Oligomerization of the source hexenes yielding 612- 624 olefins is performed in the presence of the said catalyst at the specified process parameters. The unreacted hexenes are distilled off the reaction mixture and returned back to the process. The reaction mass, free of the source hexenes, is directed for hydrogenation to a continuous flow reactor, equipped with the catalyst consisting of the oxides NiO, 6uO, and 6r2O3 in a molar ratio of 1:1:1. Simultaneously with the 612-624 olefins, hydrogen at a temperature of 120 to 150°6 and a pressure of4.0 to 5.0 MPa is supplied to the hydrogenation reactor. The 612-624 o|efins obtained at the oligomerization stage are converted into 612-624 paraffins. The yield of 612-624 paraffins in terms of oligomerized hexenes is above 98%. The reaction mass obtained at the stage of hydrogenation is directed to rectification, where it is separated into kerosene and diesel fractions.
Example 16. Obtaining kerosene from terthexyi alcohol.
Terthexyl alcohol (3-methyl-3-pentanol) is dehydrated in contact with the catalyst gamma AI2O3 at a temperature of 100-150°6 and a pressure of 1.0 to 2.0 MPa. The hexenes (66H12) formed are separated from water and supplied at a temperature of 100-150°6 and a pressure of 1.0 to 2.0 MPa into a continuous flow reactor, equipped with an ion-exchange resin in the form of a cation exchanger Amberlite 15, as the catalyst. Oligomerization of the source hexenes yielding 612-618 o|efins is carried out in the presence of the ion-exchange resin in the form of a cation exchanger Amberlite 15 as the catalyst at the specified process parameters. Unreacted hexenes are distilled off the reaction mass obtained by oligomerization and returned back to the process. The reaction mass, free of the source hexenes, is supplied for hydrogenation to a continuous flow reactor, equipped with the catalyst consisting of the oxides NiO, 6uO, and 6r2O3 in a molar ratio of 1 :1:1. Simultaneously with the 612-618 olefins, hydrogen is supplied to the hydrogenation reactor at a temperature of 120 to 150°6 and a pressure of 4.0 to 5.0 MPa. The 612-618 o|efins obtained at the stage of oligomerization are hydrogenated into 612-618 paraffins. The mixture of 612-618 paraffins thus obtained is a kerosene fraction, free of aromatic compounds. The yield of 612-61s paraffins, in terms of oligomerized hexenes, exceeds 98%. Results of the studies, performed by using chromatography-mass spectroscopy, demonstrate that kerosene, obtained from tert-hexyl alcohol, contains 48 different 612-618 isomers and is free of linear hydrocarbons.
Example 17. Obtaining kerosene from 3-ethyl-3-pentanol. 3-ethyl-3-pentanol is dehydrated in contact with the Catalyst gamma AlzOs at a temperature of 100-150°C and a pressure of 1 .0 to 2.0 MPa. The heptenes (C7H14) obtained are separated from water and supplied at a temperature of 100-150°C and a pressure of 1.0 to 2.0 MPa into a continuous flow reactor, equipped with an ion- exchange resin in the form of a cation exchanger Amberlite 15, as catalyst. Oligomerization of the source heptenes is carried out in the presence of the ion- exchange resin in the form of a cation exchanger Amberlite 15 catalyst with the specified process parameters, to yield C14-C21 olefins. Unreacted heptenes are distilled off the reaction mass obtained by oligomerization, and returned back to the process. The reaction mass, free of the source heptenes, is supplied for hydrogenation in a continuous flow reactor, equipped with the catalyst consisting of the oxides NiO, CuO, and CrzOs in a molar ratio of 1 :1:1. Simultaneously with the C14-C21 olefins, hydrogen is supplied to the hydrogenation reactor at a temperature of 120 to 150°C and a pressure of 4.0 to 5.0 MPa. The C14-C21 olefins obtained at the oligomerization stage are hydrogenated into C14-C21 paraffins. The reaction mass obtained at the stage of hydrogenation is directed to rectification, and is separated into kerosene and diesel fractions, free from aromatic compounds. The yield of Ciz-Cis paraffins, in terms of oligomerized hexenes, exceeds 98%. Results of the studies, performed by using chromatography-mass spectroscopy, demonstrate that kerosene, obtained from tert- hexyl alcohol, contains 48 different 612-618 isomers and is free of linear hydrocarbons.
Example 18. Obtaining kerosene from tert-heptyl alcohol. 2-Methyl-hexanol-2 (dimethyl butyl carbinol) is dehydrated in contact with the catalyst gamma AlzOs at a temperature of 100-150°C and a pressure of 1 .0 to 2.0 MPa. The obtained heptenes (C7H14) are separated from water and supplied at a temperature of 100-150°C and a pressure of 1 .0 to 2.0 MPa into a continuous flow reactor, equipped with the catalyst, an ion-exchange resin in the form of a cation exchanger Amberlite 15. These conditions provide for oligomerization of heptenes yielding C14-C21 olefins. The unreacted heptenes are distilled off the reaction mass obtained in the process of oligomerization, and returned back to the process. The reaction mass, free from the source heptenes, is supplied for hydrogenation to a continuous flow reactor, equipped with the catalyst consisting of the oxides NiO, CuO, and CrzOa in a molar ratio of 1:1:1.
Simultaneously with the oligomerization products, that is the 614-621 olefins, hydrogen at a temperature of 120 to 150°6 and a pressure of 4.0 to 5.0 MPa is supplied into the hydrogenation reactor. The 614-621 olefins obtained at the oligomerization stage are converted into 614-621 paraffins. The reaction mass obtained at the stage of hydrogenation is directed to rectification, and is separated into kerosene and diesel fractions, free of aromatic compounds. The yield of 614-621 paraffins, in terms of oligomerized heptenes, exceeds 95%. Results of the studies, performed by using chromatography-mass spectroscopy, demonstrate that kerosene, obtained from tertheptyl alcohol, contains 28 different 614-616 isomers and is free of linear hydrocarbons.
Example 19. Obtaining kerosene from 2-ethyl-hexyl alcohol. 2-ethyl-hexyl alcohol (2-ethyl-hexanol-1) is dehydrated in contact with the catalyst gamma AI2O6 at a temperature of 350 to 400°6 and a pressure of 0.5 to 2.0 MPa to yield octenes. The octenes (66H16) are separated from water and supplied at a temperature of 150 to 200°6 and a pressure of 1.0 to 2.0 MPa into a continuous flow reactor, equipped with the granular catalyst containing at least 95% of ZSM-5 zeolite modified by 3.5-5.0% Zn and 0.1-1.5% 6e. These conditions provide for oligomerization of octenes to yield 616-624 olefins. Unreacted octenes are distilled off from the reaction mass obtained by oligomerization, and returned back to the process. The reaction mass, free of the source octenes, is supplied for hydrogenation to a continuous flow reactor, equipped with the catalyst consisting of the oxides NiO, 6uO, and 6r2O6 in a molar ratio of 1 :1:1. Simultaneously with the 616-624 olefins, hydrogen is supplied into the hydrogenation reactor at a temperature of 250 to 350°6 and a pressure of 4.0 to 5.0 MPa. The 616-624 olefins obtained at the oligomerization stage are hydrogenated into 616-624 paraffins. The yield of 616-624 paraffins, in terms of oligomerized octenes, exceeds 95%. Then the reaction mass obtained at the stage of hydrogenation is separated by rectification into kerosene and diesel fractions. Aromatic compounds content in these fractions does not exceed 5.0% mass.
Example 20. Obtaining kerosene from a mixture of tert-amyl and tert-hexyl alcohols.
A mixture of tert-amyl and tert-hexyl alcohols in a molar ratio of 1:1 is dehydrated in contact with the Catalyst gamma AlzOs at a temperature of 100-150°C and a pressure of 1.0 to 2.0 MPa. The resulting mixture of o|efins (C5H1o + C6H12) is separated from water and supplied at a temperature of 100 to 150°C and a pressure of 1.0 to 2.0 MPa into a continuous flow reactor, equipped with the ion-exchange resin in the form of a cation exchanger Amberlite 15, as catalyst. These conditions provide for oligomerization of pentenes and hexenes to yield C1o-C24 o|efins. The unreacted pentenes and hexenes are distilled off from the reaction mass obtained by oligomerization and returned back to the process. The reaction mass, free of the source pentenes and hexenes, is supplied for hydrogenation to a continuous flow reactor, equipped with the catalyst consisting of the oxides NiO, CuO, and CrzOs in a molar ratio of 1:1:1. Simultaneously with the products of oligomerization, hydrogen at a temperature of 120 to 150°C and a pressure of 4.0 to 5.0 MPa is supplied to the hydrogenation reactor. The unsaturated C1o-C24 compounds obtained at the oligomerization stage are hydrogenated into C1o-C24 paraffins. After that the reaction mass obtained at the stage of hydrogenation is separated by rectification into kerosene, as well as gasoline and diesel fraction, free of aromatic compounds.
The yield of 610-624 paraffins, in terms of oligomerized pentenes and hexenes, exceeds 99%. Results of the studies, performed by using chromatography-mass spectroscopy, demonstrate that kerosene, obtained from tert-amyl and tert-hexyl alcohols, contains 78 different Cio-Czo isomers and is free of linear hydrocarbons.
Example 21. Obtaining kerosene from a mixture of tert-amyl, tert-hexyl and tert-heptyl alcohols.
A mixture of tert-amyl, tert-hexyl and tert-heptyl alcohols in a molar ratio of 1:1:1 is dehydrated in contact with the catalyst gamma AlzOa at a temperature of 100-150°C and a pressure of 1.0 to 2.0 MPa. The resulting mixture of o|efins (C5H1o + CßHiz + C1H14) is separated from water and supplied at a temperature of 100 to 150°C and a pressure of 1.0 to 2.0 MPa into a continuous flow reactor, equipped with the ion- exchange resin in the form of a cation exchanger Amberlite 15, as catalyst. These conditions provide for oligomerization of pentenes, hexenes and heptenes to yield C10- C24 o|efins. The unreacted pentenes, hexenes and heptenes are distilled off from the reaction mass obtained by oligomerization, and returned back to the process. The reaction mass, free of the source pentenes, hexenes and heptenes, is directed for hydrogenation to a continuous flow reactor, equipped with the catalyst consisting of the NiO, 6uO, and 6r2O3 in a molar ratio of 1:1:1. Simultaneously with the products of oligomerization, hydrogen at a temperature of 120 to 150°6 and a pressure of 4.0 to 5.0 MPa is supplied to the hydrogenation reactor. The unsaturated 610-624 compounds obtained at the oligomerization stage are hydrogenated into 610-624 paraffins. After that, the reaction mass obtained at the stage of hydrogenation is separated by rectification into 611-618 kerosene, and 619-624 diesel fractions, free of aromatic compounds. The yield of 610-624 paraffins, in terms of o|igomerized 65-67 olefins, exceeds 99%. Results of the studies, performed by using chromatography-mass spectroscopy, demonstrate that kerosene, obtained from tert-amyl, tert-hexyl, and tert- heptyl alcohols, contains 101 different 610-620 isomers and is free of linear hydrocarbons.
Example 22. Obtaining kerosene from a mixture of propyl and 2-methyl pentyl alcohols.
A mixture of propyl and 2-methyl pentyl alcohols in a molar ratio (1 .0-1 .5):1 is dehydrated in contact with the catalyst gamma AlzOa at a temperature of 350 to 450°6 and a pressure of 1.0 to 2.0 MPa. The resulting mixture of olefins (63H6 + 66H12) is separated from water and supplied at a temperature of 250 to 350°6 and a pressure of 3.0 to 5.0 MPa into a continuous flow reactor, equipped with the granular catalyst containing at least 95% of ZSM-5 zeolite modified by 3.5 -5.0% Zn and 0.1-1.5% 6e. These conditions provide for oligomerization of propylene and hexenes to yield 66-624 olefins. The unreacted propylene and hexenes are distilled off from the reaction mass obtained by oligomerization, and returned back to the process. The reaction mass, free from the source propylene and hexenes, is supplied for hydrogenation to a continuous flow reactor, equipped with the catalyst consisting of the NiO, 6uO, and 6r2Os in a molar ratio of 1:1:1. Simultaneously with the oligomerization products, hydrogen at a temperature of 120-150°6 and a pressure of4.0-5.0 MPa is supplied to the hydrogenation reactor. The unsaturated 66-624 compounds obtained at the oligomerization stage are hydrogenated into 66-624 paraffins. The reaction mass obtained at the stage of hydrogenation is then separated by rectification into 611-618 61 kerosene, as well as 66-616 gasoline and 619-624 diesel fractions, with aromatic compounds content of not more than 5.0% mass.
Example 23. Obtaining kerosene from a mixture of propyl, isobutyl, 2-methyl pentyl and 2-ethyl hexyl alcohols.
A mixture of propyl, isobutyl, 2-methyl pentyl and 2-ethyl hexyl alcohols in a molar ratio of (1 .0-1 .5):1 :1 :(1 .0-1 .5) is dehydrated in contact with the catalyst gamma AI2O6 at a temperature of 350 to 450°6 and a pressure of 1.0 to 2.0 MPa. The resulting mixture of o|efins (66H6 + 64H6 + 66H12 + 66H16) is separated from water and directed at a temperature of 250 to 350°6 and a pressure of 3.0 to 5.0 MPa into a continuous flow reactor, equipped with the granular catalyst containing at least 95% of ZSM-5 zeolite modified by 3.5-5.0% Zn and 0.1-1.5% 6e. These conditions provide for oligomerization of propylene, isobutylene, isohexenes and isooctenes to yield 66-624 o|efins. The unreacted propylene and isobutylene are distilled off from the reaction mass obtained by oligomerization and returned back to the process. The reaction mass, free from the source propylene and isobutylene, is supplied for hydrogenation to a continuous flow reactor, equipped with the catalyst consisting of the oxides NiO, 6uO, and 6r2O6 in a molar ratio of 1:1:1. Simultaneously with the oligomerization products, hydrogen at a temperature of 120 to 200°6 and a pressure of 4.0 to 5.0 MPa is supplied to the hydrogenation reactor. The unsaturated 66-624 compounds obtained at the oligomerization stage are hydrogenated into 66-624 paraffins. Said 66-624 paraffins are separated by rectification into 611-618 kerosene, 66-61o gasoline and 619- 624 diesel fractions. Tables 3, 4, and 5 demonstrate the properties of the hydrocarbon fractions obtained by the inventive process, and having an aromatic compound content of not more than 5% mass. The yield of 66-624 paraffins, in terms of oligomerized 6s- 66 o|efins, exceeds 99%.
Results of the studies, performed by using chromatography-mass spectroscopy, demonstrate that kerosene, obtained from propyl, isobutyl, 2-methyl pentyl and 2-ethyl hexyl alcohols, contains 134 different 66-616 isomers, wherein 4.2% mass of those are linear hydrocarbons. 62 Table 3. Properties of gasoline of Example 23.
EN ISO 5164 Min 95 96.5 EN ISO 5163 Min 85 92.3 EN ISO 3405 OC Min 30 30.6 EN ISO 3405 % vol 20 - 52 22.6 EN ISO 3405 % vol 46 - 72 46.8 EN ISO 3405 % vol Min 75 85.7 EN ISO 3405 OC Max 210 180.8 EN ISO 3405 % vol Max 2.0 1.2 EN 13016 kPa Min 45 Max 100 56.7 EN ISO 3675 3 720 - 775 kg/m 731.6 EN ISO 22854 % vol Max 18.0 < 0.3 EN ISO 22854 % vol Max 1.0 < 0.1 EN ISO 22854 % vol Max 35 < 0.5 EN ISO 22854 % mass Max 3.7 < 0.1 EN ISO 2160 rating class 1 1A EN ISO 20846 mg/kg Max 10.0 < 0.1 EN ISO 6246 mg/100mI Max 5 1.5 EN ISO 6246 mg/100mI Max 5 < 1.0 Table 4. Properties of Jet of Example 23.
Acid Number ASTM D 3242 mg KOH/g Max 0,015 0,004 63 Table 4. Properties of Jet of Example 23.
Density at 15°C ASTM D 4052 kg/m 3 775 - 840 780.6 Mono-Aromatics Content ASTM D 6379 % vol Min 8 Max 25 < 1.0 Poly Aromatic Content EN 12916 % W/W < 0.1 Olefines ASTM D 1319 % vol 1.0 Distillation IBP ASTM D 86 °C 168.5 Temperature @ 10% rec. ASTM D 86 °C Max 205 179.6 Temperature @ 20% rec. ASTM D 86 °C 192.4 Temperature @ 50% rec. ASTM D 86 °C 203.9 Temperature @ 90% rec. ASTM D 86 °C 234.4 Distillation FBP ASTM D 86 °C Max 300 241.4 Residue ASTM D 86 % vol Max 1.5 1.1 Loss ASTM D 86 % vol Max 1.5 0.6 Sulphur Content ASTM D 5453 mg/kg Max 0.3 < 0.1 Flash Point Abel IP 170 °C Min 38 53.5 Freezing Point ASTM D 2386 °C Max minus 47 < minus 85 Gum, Existent ASTM D 381 mg/100ml Max 7 < 0.1 Smoke Point ASTM D 1322 mm Min 25 32.0 Water Reaction ASTM D 1094 1b Water Separation Index (MSEP) ASTM D 3948 Min 85 92 Particulate Contaminant Lab. Test ASTM D 5452 mg/I Max 10 0.72 Copper strip corrosion ASTM D 130 2h/100°C class 1 1A Color (Saybolt) ASTM D 156 Min 25 30 64 Table 4. Properties of Jet of Example 23.
Conductivity (no antistatic agent) ASTM D 2624 pS/m Max 600 <1 JFTOT 260°C, 2.5h ASTM D 3241 mmHg Max 25 <1 JFTOT ASTM D 3241 Rating Max 85 41 JFTOT ASTM D 3241 ml 460 JFTOT ASTM D 3241 °C Min 325 325 BOCLE ASTM D 5001 WSD mm Max 0.85 0.67 Specific Energy ASTM D 3338 MJ/kg Min 42.8 43.86 Viscosity@-20°C ASTM D 445 mmZ/s Max 8.0 5,631 Table 5. Properties of diesel of Example 23.
Cetane Number EN ISO 4264 Min 51 59.2 Cetane Index (Calculated) ISO 6245 Min 46 64.6 Density at 15°C ISO 12185 kg/m3 800 - 845 814.1 Mono-Aromatics Content SS-EN 12916 % vol Max 8.0 4.7 Poly Aromatic Content SS-EN 12916 % vol Max 8.0 < 0.02 Fractional composition: ISO 3405 recovered at 180°C, ISO 3405 % vol Max 10 < 0.1 recovered at 250°C, ISO 3405 % vol Max 65 19.7 recovered at 340°C, ISO 3405 % vol Min 95 > 98.0 95% vol. recoveredat at temperature ISO 3405 °C Max 360 291.6 Sulphur content ISO 20846 mg/kg Max 10 3 Flash point EN ISO 2719 °C Min 55 88.0 Table 5. Properties of diesel of Example 23.
Ash content ISO 6245 % mass Max 0.010 0,001 Water content EN ISO 12937 % mass Max 0.020 0,0028 Particulate matter EN 12662 mg/kg Max 24 6.5 Copper strip corrosion ASTM D rating class 1 1A Cold Filtration Plugging Point EN 116 °C Max minus 44 minus 48 Cloud point EN 23015 °C Max minus 34 < minus 52 Viscosity@ 40°C, ISO 3104 MM2/c 1.500 - 4.000 3,000 Oxidation Stability 20 h ISO 12205 g/m3 Max 25 2 HFRR Wear Scar (Lubricity) ISO 12156 im: Max 460 443 Example 24. Obtaining tertamyl ethyl ether from tert-amyl and ethyl alcohols.
Tert-amyl alcohol (2-methyl-2-butanol) produced on the basis of the inventive technology is dehydrated in contact with the catalyst gamma AlzOs at a temperature of 100-150°C and a pressure of 1 .0 to 2.0 MPa. The obtained pentenes (C5H1o) are separated from water, mixed with ethyl alcohol (CzHsOH) in a molar ratio of 1 :(1 .1-1 .5) and supplied at a temperature of 50 to 100°C and a pressure of 0.5-1 .0 MPa to a continuous flow reactor, equipped with the ion-exchange resin in the form of a cation exchanger Amberlite 15, as catalyst. The load on the catalyst is 0.5 to 1.0 liters of a solution of pentenes in ethyl alcohol per 1.0 liter of catalyst, the contact time of a solution of pentenes in ethyl alcohol with the ion-exchange resin in the form of a cation exchanger Amberlite 15, as catalyst is 30 to 60 minutes. The reaction mass obtained at the stage of etherification is directed to rectification, where ethyl alcohol is separated from ethyl tert-amyl ether. The rate of conversion of pentenes into ethyl tert-amyl ether exceeds 99%. The unreacted ethyl alcohol is returned back to the process to the stage of mixing with pentenes. Tert-amyl ethyl ether is used to obtain a standard gasoline free of aromatics. 66 Example 25. Obtaining a standard gasoline containing ethers.
To obtain a standard gasoline free of aromatic compounds, the gasoline fraction of paraffins, produced on the basis of the inventive technology was used, and tertamyl ethy| ether, produced by the method of the previous example. The gasoline fraction of paraffins, containing Cs-C1o hydrocarbons, is mixed with tertamyl ethy| ether in any volume ratio that does not violate the limits for oxygen content in gasoline prescribed by the relevant standards. Concentrations of 15%-22% by volume of tertamyl ethy| ether in the final mixture with Cs-C1o paraffins are preferred for gasolines produced by the inventive technology. Table 6 shows the main properties of gasoline that is free of aromatic compounds. Gasoline prepared from the gasoline fraction of paraffins and tertamyl ethy| ether, produced on the basis of the inventive technology, is characterized by high octane numbers. A content of 20.0% by volume of tertamyl ethy| ether and 80.0% by volume of the gasoline fraction, as shown in the Example 23, provides the octane number RON = 100.9 MON = 93.8. The oxygen content of such gasoline is less than 3.0% wt.
Table 6. Properties of gasoline of Example 25.
EN iso 5164 iviin 95 100.9 EN iso 5163 iviin 65 93.6 EN iso 3405 OC iviin 30 32.4 EN iso 3405 % voi 10 - 50 25.4 EN iso 3405 % voi 35 - 71 37.6 EN iso 3405 % voi iviin 60 63.3 EN iso 3405 OC iviax 210 177.5 EN iso 3405 % voi iviax 2.0 1.1 67 Table 6. Properties of gasoline of Example 25.
EN 13016 kPa Min 45 Max 100 59.0 EN ISO 3675 kg/m3 720 - 775 737.3 EN ISO 22854 % vol Max 18.0 < 0.1 EN ISO 22854 % vol Max 1.0 < 0.1 EN ISO 22854 % vol Max 35 < 0.5 EN ISO 22854 % mass Max 3.7 2.99 EN ISO 2160 rating class 1 1A EN ISO 20846 mg/kg Max 10.0 < 0.1 EN ISO 6246 mg/100mI Max 5 0.6 EN ISO 6246 mg/100mI Max 5 < 0.5 Example 26. Obtaining ethers from tertiary Cs-Cß alcohols and ethanol.
A mixture of tertiary Cs-Cs alcohols, obtained by telomerization, were sent to rectification for isolation of tertiary Cs-Cß alcohols. The Cs-Cß tertiary alcohols were then dehydrated to yield the corresponding Cs-Cß olefins. The obtained Cs-Cß olefins were cooled and supplied at a temperature of 50 to 100°C and a pressure of 0.5-1 .0 MPa into a continuous flow reactor, equipped with the ion-exchange resin in the form of a cation exchanger Amberlite 15, as Catalyst. Along with Cs-Cß olefins, ethyl alcohol was supplied to the reactor in a molar ratio (C5H1o + C6H12):C2H5OH = 1:(1.0-1.1). The Contact time of the Cs-Cß olefin solution in ethyl alcohol with the ion-exchange resin in the form of a cation exchanger Amberlite 15, as Catalyst is 30 to 60 minutes. The reaction mass obtained at the stage of etherification is sent to rectification for separation of the unreacted ethyl alcohol from tertamyl ethyl and terthexyl ethyl ethers. The rate of Conversion of Cs-Cß olefins into ethyl tertamyl and ethyl terthexyl ethers exceeds 99%. The unreacted in the etherification reaction ethyl alcohol is returned back to the process to the stage of mixing with Cs-Cß olefins. Ethyl tertamyl and ethyl terthexyl ethers are used for producing gasoline with an octane number of at least 100. 68 Example 27. Obtaining gasoline with octane number of at least 100 and oxygen content of not more than 2.7% mass.
To produce gasoline with an octane number of at least 100 and an oxygen content of not higher than 2.7% mass, it is necessary to use Cs-Cio gasoline fraction of paraffins, obtained by the inventive technology, as well as tertamyl ethyl and terthexyl ethyl ethers, obtained as described in the previous Example. Furthermore, to produce gasoline with an octane number of at least 100 and an oxygen content of not more than 2.7 wt%, it is necessary to use Cw-Cg aromatic compounds obtained by the inventive technology. The gasoline fraction of paraffins, containing Cs-Cio hydrocarbons, is mixed with tertamyl ethyl and terthexyl ethyl ethers in any volume ratio, which does not violate limits on oxygen content in gasoline stipulated by the relevant standard EN228. Preferred volumetric concentrations for gasolines with an octane number of at least 100 are 15%-25% of tertamyl ethyl and terthexyl ethyl ethers in the final composition with Cs-Cio paraffins and Cw-CQ aromatics.
Table 7 shows main properties of gasoline with an octane number of at least 100 and an oxygen content of not more than 2.7% mass.
Table 7. Properties of gasoline of Example 27.
EN ISO 5164 EN ISO 5163 Min 85 93.6 EN ISO 3405 OC Min 30 36.4 EN ISO 3405 % vol 10 - 50 17.9 EN ISO 3405 % vol 35 - 71 42.7 EN ISO 3405 % vol Min 60 84.1 EN ISO 3405 OC Max 210 178.4 EN ISO 3405 % vol Max 2.0 1.2 69 Table 7. Properties of gasoline of Example 27.
EN 13016 kPa 45 - 100 58.0 EN ISO 3675 kg/m3 720 - 775 757.6 EN ISO 22854 % vol Max 18.0 < 0.1 EN ISO 22854 % vol Max 1.0 < 0.1 EN ISO 22854 % vol Max 35 7.5 EN ISO 22854 % mass Max 2.7 2.65 EN ISO 2160 rating class 1 1A EN ISO 20846 mg/kg < 0.1 EN ISO 6246 mg/100mI Max 5 0.6 EN ISO 6246 mg/100mI Max 5 < 0.5 Example 28 Obtaining of ethers from tertiary Cw-Cs alcohols and n-butyl alcohols A mixture of tertiary Cs-Cs alcohols, obtained by telomerization, was sent for rectification to isolate tertiary Cw-Cs alcohols. The tertiary alcohols were then dehydrated to yield the Corresponding Cw-Cs olefins. The Cw-Cs olefins thus obtained were Cooled and supplied at a temperature of 50 to 100°C and a pressure of 0.5-1 .0 MPa into a Continuous flow reactor, where the ion-exchange resin in the form of a Cation exchanger Amberlite 15, as Catalyst was loaded. Along with the Cw-Cs olefins, n- butyl alcohol, obtained by the inventive technology, was supplied into the reactor in a molar ratio (C7H14 + CsH1e):C4H9OH = 1:(1.0-1.1). The Contact time of the Cr-Cs olefin solution in n-butyl alcohol with the ion-exchange resin in the form of a Cation exchanger Amberlite 15, as Catalyst is 30 to 60 minutes. The reaction mass obtained in the etherification process was direCted to rectification, where n-butyl alcohol was separated from tert-heptyl butyl and tert-octyl butyl ethers. The rate of Cw-Cs olefin Conversion into tert-heptyl butyl and tert-octyl butyl ethers exCeeds 99%. The unreaCted in the etherification reaction butyl alcohol, is separated by rectification in the rectification column and returned back to the process to the stage of mixing with Cw-Cs olefins. Tert-heptyl butyl and tert-octyl butyl ethers are used to produce diesel, containing oxygenated hydrocarbons.
Example 29. Producing a standard diesel fuel containing oxygenated hydrocarbons.
To produce a standard diesel fuel comprising oxygen-containing hydrocarbons, it is necessary to use diesel fraction of 619-624 paraffins, produced by the inventive technology. Furthermore, tert-heptyl butyl and tert-octyl butyl ethers shall be used as oxygen-containing hydrocarbons of this diesel fuel. The method for producing tert- heptyl butyl and tert-octyl butyl ethers is described in the previous example. The diesel fraction of paraffins, containing C19-C24 hydrocarbons, was mixed with tert-heptyl butyl and tert-octyl butyl ethers in any ratio that does not violate requirements of the relevant standards for diesel fuels. Preferred concentration for diesel fuels, produced by the invenitive technology, is from 5% to 15% by volume of the total of tert-heptyl butyl and tert-octyl butyl ethers in the final mixture with C19-C24 paraffins. Table 8 shows main properties of the diesel fuel containing a mixture of tert-heptyl butyl and tert-octyl butyl ethers in the amount of 10% by vol. of the final mixture with C19-C24 paraffins.
Table 8. Properties of diesel fuel of Example 29.
Cetane Number EN ISO 4264 Min 51 54.6 Cetane Index (Calculated) ISO 6245 Min 46 61.7 Density at 15°C ISO 12185 kg/m3 800 - 845 817 0 Mono-Aromatics Content SS-EN 12916 % vol Max 8.0 3.5 Poly Aromatic Content SS-EN 12916 % vol Max 8.0 < 0.01 Fractional composition: ISO 3405 recovered at 180°C, ISO 3405 % vol Max 10 < 0.1 recovered at 250°C, ISO 3405 % vol Max 65 29.9 71 Table 8. Properties of diesel fuel of Example 29. recovered at 340°C, ISO 3405 % vol Min 95 > 98 95% vol. recovered at a temperature ISO 3405 °C Max 360 314.3 Sulphur Content ISO 20846 mg/kg Max 10 < 2 Flash Point EN ISO 2719 °C Min 55 88.5 Åsh Content ISO 6245 % mass Max 0.01 < 0.001 Water Content EN ISO 12937 % mass Max 0.020 0.0102 Particulate Matter EN 12662 mg/kg Max 24 0.76 Copper strip corrosion ASTM D rating class 1 1A Cold Filtration Plugging Point EN 23015 °C Max minus 32 minus 33 Cloud Point EN 116 °C Max minus 22 minus 31 Viscosity@ 40°C, ISO 3104 MM2/c 1.500 - 4.000 2,852 Oxidation Stability 20 h ISO 12205 g/m3 Max 25 18 HFRR Wear Scar (Lubricity) ISO 12156 pm Max 460 396 Example 30. Producing ethers from tertiary Cw-Cs alcohols and 2-ethyl hexyl alcohol.
A mixture of tertiary Cs-Cg alcohols, obtained by telomerization, was sent to rectification to isolate the tertiary Cw-Cs alcohols. The isolated alcohols were then dehydrated to obtain the corresponding Cw-Cs olefins. The Cw-Cs olefins obtained were cooled and supplied at a temperature of 50 to 100°C and a pressure of 0.5 to 1.0 MPa to a continuous flow reactor, where the catalyst, which is an ion exchange resin, in this case the cation exchanger Amberlite 15, was loaded. Along with the Cw-Cs olefins, 2- ethyl hexyl alcohol, obtained by the inventive technology, was supplied to the reactor in a molar ratio (C7H14 + CsH1e):CsH17OH = 1:(1.1-1.5). The contact time of the solution of Cw-Cs olefins in 2-ethyl hexyl alcohol with the catalyst, which is an ion exchange resin, 72 in this case the cation exchanger, is 45 to 60 minutes. The reaction mass obtained at the stage of etherification was directed to rectification, where 2-ethyl hexyl alcohol was separated from the obtained tert-heptyl 2-ethyl hexyl and tert-octyl 2-ethyl hexyl ethers.
The rate of 67-68 olefin conversion into tert-heptyl 2-ethyl hexyl and tert-octyl 2-ethyl hexyl ethers exceeds 90%. A mixture of 2-ethyl hexyl alcohol and unreacted 67-68 olefins was iso|ated in the rectification column and returned back to the process to the etherification stage. Tert-heptyl 2-ethyl hexyl and tert-octyl 2-ethyl hexyl ethers are used to produce diesel fuel, comprising in the composition oxygen-containing hydrocarbons in an amount of not less than 20% vol.
Example 31. Producing diesel fuel, comprising in the composition oxygen-containing hydrocarbons in the amount of not less than 20% vol.
To produce diesel fuel comprising in the composition oxygen-containing hydrocarbons in the amount of not less than 20% vol., it is necessary to use the 619-624 paraffin fraction obtained by the inventive technology. Furthermore, to produce said diesel fuel, it is necessary to use tert-heptyl butyl and tert-octyl butyl ethers, as well as tert-heptyl 2-ethyl hexyl and tert-octyl 2-ethyl hexyl ethers. Methods for producing said ethers are described in the Examples 28 and 30.
The paraffin fraction, containing 619-624 hydrocarbons, was mixed with tert-heptyl butyl and tert-octyl butyl ethers, as well as tert-heptyl 2-ethyl hexyl and tert-octyl 2-ethyl hexyl ethers. The mixing was performed in a manner providing for compliance of the properties of the resulting hydrocarbon mixtures with the requirements of the current standards for diesel motor fuel. Preferred concentration for diesel fuels produced by the inventive technology and comprising said ethers is from 10% to 20% by volume of the total of all ethers in the final mixture with 619-624 paraffins. Table 9 shows the main properties of diesel fuel, containing not less than 20% vol. of oxygen-containing hydrocarbons. 73 Table 9. Properties of diesel fuel of Example 31 Cetane Number EN ISO 5165 Min 51 59.8 Cetane Index (Calculated) EN ISO 4264 Min 46 66.2 Density at 15°C EN ISO 12185 kg/m3 820 - 845 820.8 Mono-Aromatics Content SS-EN 12916 % vol Max 8.0 < 0.1 Carbon Residue Micro (10%) ISO 10370 % mass Max 0.30 < 0.02 Fraetional composition: EN ISO 3405 recovered at 250°C, EN ISO 3405 % vol Max 65 33.3 recovered at 350°C, EN ISO 3405 % vol Min 85 > 98.5 95% vol. recovered at a EN ISO 3405 °C Max 360 temperature 314.8 Sulphur Content EN ISO 20846 mg/kg Max 10 < 2 Flash Point EN ISO 2719 °C Min 55 88.0 Ash Content EN ISO 6245 % mass Max 0.010 < 0.001 Water Content EN ISO 12937 % mass Max 0.020 11 Particulate Matter EN 12662 mg/kg Max 24 16 Copper strip corrosion EN ISO 2160 rating class 1 1A Cold Filtration Plugging Point EN 23015 °C Max minus 38 minus 40 Cloud Point EN 116 °C Max minus 28 minus 39 Viscosity@ 40°C, EN ISO 3104 mmZ/C 1.500 - 4.000 2,988 Oxidation Stability 20 h EN ISO 12205 g/m3 Max 25 22 HFRR Wear Scar (Lubricity) ISO 12156 pm Max 460 419 Example 32. Obtaining a 100% biological kerosene from ethanol, in full compliance of all requirements of the current standard Jet A1. 74 A mixture of tert-amyl, tert-hexyl, tert-heptyl and tert-octyl alcohols in a molar ratio of 1:1:1:1 is dehydrated in contact with the gamma AlzOs Catalyst at a temperature of 100 to 150°C and a pressure of 1.0 to 2.0 MPa. The resulting mixture of o|efins (C5H1o + C6H12 + C7H14 + CsHiß) is separated from water and supplied at a temperature of 100 to 150°C and a pressure of 1.0 to 2.0 MPa to a continuous flow reactor, where the catalyst, which is an ion exchange resin, in this case the cation exchanger Amberlite 15, is loaded. Under these conditions, pentenes, hexenes, heptenes and octenes are oligomerized yielding C1o-C24 o|efins. The unreacted pentenes, hexenes, heptenes and octenes are distilled from the reaction mass obtained by oligomerization and returned back to the process. The reaction mass, free of the source pentenes, hexenes, heptenes and octenes, is directed for hydrogenation to a continuous flow reactor, where the catalyst consisting of the oxides NiO, CuO and CrzOa in a molar ratio of 1:1:1 is loaded. Along with the oligomerization products, hydrogen is supplied to the hydrogenation reactor at a temperature of 120 to 150°C and a pressure of 4.0 to 5.0 MPa. ln the course of hydrogenation, the unsaturated C1o-C24 compounds obtained at the oligomerization stage are converted into C1o-C24 paraffins. The reaction mass obtained at the stage of hydrogenation is directed to the rectification, where it is separated into kerosene and diesel fractions, free of aromatic compounds.
The unsaturated Cz-Cs hydrocarbons obtained at the stage of dehydration of the corresponding Cz-Cs alcohols are supplied to the aromatization reactor. Aromatization of the unsaturated hydrocarbons is carried out at a temperature of 350 to 450°C and a pressure of 0.5 to 2.0 MPa in a continuous operation reactor in the presence of the inventive heterogeneous zeolite-containig catalyst, comprising at least 93% of ZSM-5 modified by 3.5 to 7.0% Zn. ln the course of aromatization, the unsaturated Cz-Cs hydrocarbons are converted into aromatic compounds Cv-Ciz. The reaction mass obtained at the stage of aromatization is isolated from the gaseous products, which are a mixture of hydrogen and C1-C4 paraffins, and directed to rectification, where it is separated into two fractions: Cw-Cs aromatic hydrocarbons and C9-C12 aromatic hydrocarbons. The Cw-Cs aromatic hydrocarbons are used to produce gasoline, while the C9-C12 aromatic hydrocarbons are used to produce kerosene. The C11-C1s kerosene paraffins fraction isolated from C1o-C24 paraffins is mixed with the aromatic compounds in such a way that the concentration of the aromatic hydrocarbons in the final composition of kerosene is in the range from 8% vol. to 25% vol. Table 10 shows the main properties of the 100% biological kerosene produced from ethanol, which is in full compliance with all requirements of the current standard Jet A1.
Table 10. Properties of Jet of Example 32 Property Metod Unit Limit Result for Jet of Example 32 Acid Number ASTM D 3242 mg KOH/g Max 0.015 0,007 Density at 15°C ASTM D 4052 kg/m3 775 - 840 789.5 Mono-Aromatics Content ASTM D 1319 % volume Min 8 Max 25 9.8 Poly Aromatics Content EN12916 %W/\N < 0.1 Olefines ASTM D 1319 % vol 1.8 Distillation IBP ASTM D 86 °C 169,9 Temperature @ 10% rec. ASTM D 86 °C Max 205 183,1 Temperature @ 20% rec. ASTM D 86 °C 187,2 Temperature @ 50% rec. ASTM D 86 °C 201,4 Temperature @ 90% rec. ASTM D 86 °C 223,0 Distillation FBP ASTM D 86 °C Max 300 235,3 Residue ASTM D 86 % vol Max 1.5 1,5 Loss ASTM D 86 % vol Max 1.5 0,2 Sulphur Content ASTM D 5453 mg/kg Max 0.3 < 0.1 Flash Point Abel ASTM D 56 °C Min 38 51.0 Freezing Point ASTM D 2386 °C Max minus 47 < minus 85 Gum, Existent ASTM D 381 mg/100ml Max 7 < 1 Smoke Point ASTM D 1322 mm Min 25 35 Water Reaction ASTM D 1094 1b Water Separation Index (MSEP) ASTM D 3948 Min 85 97 Particulate Contaminant Lab. Test ASTM D 5452 mg/I Max 10 0.36 Copper strip corrosion ASTM D 130 2h/100°C class 1 1A 76 Table 10. Properties of Jet of Example 32 Property Metod Unit Limit Result for Jet of Example 32 Color (Saybolt) ASTM D 156 Min 25 30 Conductivity (no antistatic agent) ASTM D 2624 pS/m Max 600 <1 JFTOT 2.5h 260°C ASTM D 3241 mm Hg Max 25 <1 JFTOT Rating ASTM D 3241 nm Max 85 9 JFTOT ASTM D 3241 ml 447 JFTOT ASTM D 3241 °C Min 325 325 BOCLE ASTM D 5001 WSD mm Max 0.85 0.69 Specific Energy ASTM D 3338 MJ/kg Min 42.8 43.75 Viscosity@-20°C ASTM D 445 mmZ/S Max 8.0 4,893

Claims (15)

1. A method for producing from ethanol a motor fuel selected from gasoline, kerosene, and diesel, comprising the following interconnected steps: step 1.- isopropanol and G5 alcohols; converting a mixture of ethanol and water into: - acetaldehyde; - a mixture of C1-C4 paraffins and C2-C4 olefins; - a mixture of carbon dioxide and hydrogen; step 1.2 1.1, additional hydrogen, and a mixture of C1-C4 paraffins into synthesis gas; converting the mixture of carbon dioxide and hydrogen, obtained in step step 1.3 from step 1.1, into: converting ethanol, and Cs-Cs alcohols, including G5 alcohols obtained - Cg-Cg olefins, including ethylene and propylene; step 1.4 obtained in step 1.1, ethylene obtained in step 1.3, using a telomerization reaction into converting a mixture of unreacted ethanol from step 1.1, isopropanol secondary butanol and tertiary Cs-Cs alcohols, the tertiary Cs and Cr alcohols being obtained from the isopropanol, and the tertiary Ca, and Cs alcohols being obtained from the ethanol, wherein the resulting secondary butanol is directed to step 1.3; step 1.5 dehydration into Cs-Cg olefins; converting the Cs-Cß tertiary alcohols, obtained in step 1.4, by step 1.6 oligomerization into C1o-C24 olefins; converting a first portion of the Cs-Cs olefins, obtained in step 1.5, by step 1.7 using hydrogen obtained from step 1.1, into 610-624 paraffins; converting the C1o-C24 olefins, obtained in step 1.6, by hydrogenation step 1.8 converting the synthesis gas, obtained in step 1.2, ethylene obtained instep 1.3, propylene obtained in step 1.3, and the acetaldehyde, obtained in step 1.1, by hydroformylation and aldol condensation into a mixture of G3-G4 aldehydes and Gs- Gs aldols, said mixture of Gs-G4 aldehydes and Gs-Gs aldols is thereafter hydrogenated to obtain Gg-Gg alcohols, which alcohols are directed to step 1.3 to obtain Ga-Gs olefins, wherein the acetaldehyde produces G5 alcohol, the ethylene from step 1.3 produces Gs and G6 alcohols, and the propylene from step 1.3 produces G4 and G8 alcohols; and wherein the ethylene and the propylene from step 1.3 produce G7 alcohol; step 1.9 converting the Gz-Gs o|efins from step 1.3, by oligomerization into G6-G24 o|efins; step 1.10 converting the G6-G24 olefins, obtained in step 1.9, and hydrogen, by hydrogenation into G6-G24 paraffins; step 1.11 G4 o|efins and G1-G4 paraffins, obtained in step 1.1, by aromatization into G1-Gconverting unreacted Gz-Gs o|efins from step 1.9, and the mixture of G2- aromatic hydrocarbons, hydrogen, and a mixture of G1-G4 paraffins, wherein a first portion of the hydrogen produced is directed to step 1.10, and the remaining second portion of the hydrogen produced and the G1-G4 paraffins mixture are directed to step 1.2; step 1.12 converting the remaining second portion of the mixture of Gs-Gs olefins, obtained in step 1.5, and a portion of Gz-Gs alcohols from step 1.3, into Gw-Gie ethers; and, step 1.13 converting the G1o-G24 paraffins, obtained in step 1.7, and the G6-Gparaffins, obtained in step 1.10, into Gß-Gio gasoline, G11-G1s kerosene, and G19-G24 diesel fractions of a motor fuel; converting the G7-G12 aromatic hydrocarbons, obtained in step 1.11, into Gw-Gs gasoline and G9-G12 kerosene fractions of a motor fuel; and converting the Gw-Giß ethers, obtained in step 1.12, into Gw-Gio gasoline and G11-G1ß diesel fractions of a motor fuel, and also mixing selected fractions thereof, into a motor fuel selected from gasoline, kerosene, and diesel.
2. The method for producing motor fuel from ethanol in accordance with claim 1,wherein, in step 1.1, a mixture of ethanol and water having a water content within 25% - 35% of the total volume of the mixture, is contacted, at a pressure of 0.5-1 .5 MPa and a temperature of 500-515°C, with a heterogeneous catalyst consisting of the following metal oxides: ZnO 60-63% mass, CeOz 1-6% mass, MgO 12-18% mass; and AI2O3 13-23% mass, with the proportions calculated in terms of metal oxide, wherein the mixture of ethanol and water is supplied to the catalyst at a space velocity of 0.5-0.9 h* thereby producing acetone; the resulting acetone is isolated from the reaction mixture and hydrogenated at a temperature of 100-150°C and a pressure of 0.5-0.9 MPa in the presence of a catalyst consisting of CuO and CrzOs in a molar ratio of 1:1, by hydrogen obtained from the mixture of ethanol and water, thereby resulting in the isopropanol.
3. The method for producing motor fuel from ethanol in accordance with claim 2, wherein, in step 1.4, the isopropanol reacts in the presence ofditertamyl peroxide at a pressure of P = 1.0 -5.0 MPa and a temperature of 100-130°C with the ethylene and is thereby converted into the tertiary G5 and Cr alcohols.
4. The method for producing motor fuel from ethanol in accordance with claim 2, wherein, in step 1.4, the unreacted ethanol from step 1.1 reacts in the presence ofdi- tert-butyl peroxide or di-tert-amyl peroxide under a pressure of P = 1.0-5.0 MPa and at a temperature of 100-130°C with the ethylene to obtain sec-butanol, which is then reacted with ethylene and is converted into the tertiary Ca and Cs alcohols.
5. The method for producing motor fuel from ethanol in accordance with claim 1, wherein, in step 1.8, the ethylene or propylene is converted in the hydroformylation in the presence of a water-soluble Rh catalyst, with a concentration of metal in relation to the aqueous phase of from 30 ppm to 50 ppm, at a temperature of 70-90°C and a pressure of P=1.0-5.0 MPa into propanal or n-butanal and isobutanal, thereafter a mixture of propanal, n-butanal, and acetaldehyde, obtained in step 1.1, is converted by cross-aldol condensation in the presence of a heterogeneous catalyst containing at least 93% of ZSM-5 zeolite modified by 3.5-7.0% Zn, or a granular catalyst containing at least 95% of ZSM-5 zeolite modified by 3.5-5.0% Zn and 0.1-1.5% Ce into a mixture of Cs-C4 aldehydes and Cs-Cs aldols, thereafter the mixture of Cs-C4 aldehydes and Cs-Cß aldols is hydrogenated in the presence of heterogeneous catalyst consisting of NiO, CuO, and CrzOs in a molar ratio of 1:1:1, at a temperature of 150-200°C and apressure of P=4.5-5.0 MPa, to obtain the mixture of Cs-Cs alcohols.
6. The method for producing motor fuel from ethanol in accordance with claim 5, wherein Triphenylphosphine-sulfonic acid sodium salts, namely: from Triphenylphosphine-3-sulfonic acid sodium salt to Triphenylphosphine-3,3',3"- trisulfonic acid trisodium salt in a weight ratio (10-30):1 to metal Rh are used as a ligand in the step 1.8 in the hydroformylation of the ethylene or propylene for obtaining the water-soluble catalyst.
7. The method for producing motor fuel from ethanol in accordance with claim 6, wherein, in order to increase the reaction rate and the yield of isobutanal in step 1.8, the hydroformylation of propylene by synthesis gas is carried out in the presence of a water-soluble Rh catalyst prepared in accordance with claim 6; Cz-Cs alcohols are added to said catalyst in a volume ratio H2O:(C2-Cs) = (0.95-0.65):(0.05-0.35), while the ratio of butanal and isobutanal obtained in the reaction medium is in the range (n- C4H8O):(iso-C4H8O) = (2-3):
8. The method for producing motor fuel from ethanol in accordance with claim 1, wherein, in step 1.8, the ethylene or propylene is converted in the hydroformylation reaction in the presence of a water-soluble Co catalyst, with a concentration of Co metal in relation to the aqueous phase of from 0.1 % to 1.0%, at a temperature of 120- 140°C and a pressure of P=2.0-5.0 MPa, into propanal, 2-methylpentenal and 2- methylpentanal or into n-butanal, 2-ethylhexenal, 2-ethylhexanal and isobutanal, and thereafter the mixture of C3-C4 aldehydes and Cß-Cs aldols are in the presence of a heterogeneous catalyst consisting of NiO, CuO and CrzOs in a molar ratio of 1 :1:1, at a temperature of 150-200°C and a pressure of P = 4.5-5.0 MPa hydrogenated to obtain the mixture of Cs-Cs alcohols.
9. The method for producing motor fuel from ethanol in accordance with claim 8, wherein, in step 1.8, Triphenylphosphine-sulfonic acid sodium salts, namely: from Triphenylphosphine-3-sulfonic acid sodium salt to Triphenylphosphine-3,3',3"- trisulfonic acid trisodium salt are used as a ligand in a weight ratio (1-30):1 to metal Co in the hydroformylation of ethylene or propylene for obtaining the water-soluble Co catalyst.
10. The method for producing motor fuel from ethanol in accordance with claim 9, wherein, in order to increase the reaction rate and the yield of isobutanal in step 1.8, in the hydroformylation of propylene 62-66 alcohols are added to the catalyst in a volume ratio H2O:(62-66) = (0.95- 0.5):(0.05-0.5), wherein the ratio of butanal and isobutanal obtained in the reaction medium is in the range of (n-64H6O):(iso-64H6O) = (2-3):
11. The method for producing motor fuel from ethanol in accordance with claim 1, wherein, in step 1.9, the 62-66 olefins are oligomerized in the presence of a heterogeneous catalyst containing at least 93% of ZSM-5 zeolite modified by 3.5 - 7.0% Zn, or a heterogeneous catalyst containing at least 95% of ZSM-5 zeolite modified by 3.5-5.0% Zn and 0.1-1.5% 6e at a temperature of 250-350°6 and a pressure of P=4.5-5.0 MPa to obtain the 66-624 olefins, wherein unreacted 62-66 olefins are separated by rectification from the 66-624 olefins and directed to step 1.11; wherein, in step 1.10, hydrogenation of 66-624 olefins is carried out in the presence of a heterogeneous catalyst consisting of NiO, 6uO and 6r2O6 in a molar ratio of 1:1:1, at a temperature of 150-200°6 and a pressure of P = 4.5-5.0 MPa to obtain the 66-624 paraffins; and wherein, in step 1.13, the 66-624 paraffins are rectified to isolate the 66-61o paraffin gasoline fraction, the 611-616 paraffin kerosene fraction, and the 619-624 paraffin diesel fraction of a motor fuel.
12. The method for producing motor fuel from ethanol in accordance with claim 11, wherein, in step 1.11, the unreacted 62-66 olefins are aromatized together in a mixture with 62-64 olefins and 61-64 paraffins, in the presence of a heterogeneous catalyst containing at least 93% of ZSM-5 zeolite modified by 3.5-7.0% Zn at a temperature of 350-450°6 and a pressure of P = 0.5-2.0 MPa to yield the aromatic 67-612 compounds, and, wherein, in step 1.13, the aromatic 61-612 compounds are rectified to isolate the 67-66 aromatic compound gasoline fraction, and the 69-612 aromatic compound kerosene fraction of a motor fuel.
13. The method for producing motor fuel from ethanol in accordance with claim 1, wherein, in step 1.6, the 66-66 olefins are oligomerized using an ion-exchange resin inthe form of a cation exchanger, preferably Amberlite 15, as a Catalyst, at a temperature of 70-120°6 and a pressure P = 1.0-2.0 MPa, and, wherein, in step 1.7, the 610-624 olefins are hydrogenated in the presence of a heterogeneous catalyst consisting of NiO, 6uO and 6r2O6 in a molar ratio of 1:1:1 at a temperature of 150-200°6 and pressure P = 4.5-5.0 MPa to obtain the mixture of 619- 624 paraffins, and, wherein, in step 1.13, the 610-624 paraffins are rectified to iso|ate the 611-616 paraffin kerosene fraction, and the 619-624 paraffin diesel fraction of a motor fuel, wherein remaining 610 paraffins are mixed with the 66-610 paraffin gasoline fraction of a motor fuel, obtained in step 1.13 by rectification of the 66-624 paraffins.
14. The method for producing motor fuel from ethanol in accordance with claim 13, wherein, in step 1.12, the etherification is carried out on a mixture of the 66-66 olefins and the 62-66 alcohol using as a catalyst an ion exchange resin in the form of a cation exchanger, preferably Amberlite 15, at a temperature of 70-120°6 and pressure P = 1.5-2.0 MPa, to yield the 61-616 ethers, and, wherein, in step 1.13, the 61-616 ethers obtained, are rectified to iso|ate a 61-69 ether fraction for producing gasoline, and a 610-616 ether fraction for producing diesel.
15. The method for producing motor fuel from ethanol in accordance with claim 1, wherein, in step 1.13, in order to obtain kerosene fully complying with the requirements of the current Jet A-1 standard, 611-616 paraffins are isolated from the 66-624 paraffins mixture obtained from step 1.10, 611-616 paraffins are isolated from the mixture of 61o- 624 paraffins obtained in step 1.7, and aromatic 69-612 hydrocarbons, are isolated from the 61-612 aromatic hydrocarbons mixture obtained in the step 1.11, and the isolated 611-616 paraffins and aromatic 69-612 hydrocarbons are mixed so that the concentration of aromatic 69-612 hydrocarbons is in the range of 8-25% vol, and so that the resulting kerosene will contain at least 100 different hydrocarbons, and preferably 150 different hydrocarbons, have a Smoke Point of minimum 30 mm, and a Freezing Point of maximum minus 80°6.
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