WO2017207106A1 - Procédé et dispositif de fabrication d'éthanol - Google Patents

Procédé et dispositif de fabrication d'éthanol Download PDF

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Publication number
WO2017207106A1
WO2017207106A1 PCT/EP2017/025104 EP2017025104W WO2017207106A1 WO 2017207106 A1 WO2017207106 A1 WO 2017207106A1 EP 2017025104 W EP2017025104 W EP 2017025104W WO 2017207106 A1 WO2017207106 A1 WO 2017207106A1
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WIPO (PCT)
Prior art keywords
ethanol
carbon dioxide
methanol
water
distillation column
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Ceased
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PCT/EP2017/025104
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German (de)
English (en)
Inventor
Andreas Peschel
Andreas Obermeier
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Linde GmbH
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Linde GmbH
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Filing date
Publication date
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Publication of WO2017207106A1 publication Critical patent/WO2017207106A1/fr
Anticipated expiration legal-status Critical
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    • 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
    • C07C29/15—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 oxides of carbon exclusively
    • C07C29/151—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 oxides of carbon exclusively 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
    • C07C29/74—Separation; Purification; Use of additives, e.g. for stabilisation
    • C07C29/76—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment
    • C07C29/78—Separation; Purification; Use of additives, e.g. for stabilisation by physical treatment by condensation or crystallisation

Definitions

  • the invention relates to a process and a plant for the production of ethanol from synthesis gas according to the preambles of the independent claims.
  • ethanol is currently predominantly fermentative from biomass.
  • synthesis gas can also be converted to ethanol by fermentation.
  • Corresponding processes are also referred to as gas fermentation and are described, for example, in Brown, R.C .: “Biorenewable Resources: Engineering New Products from Agriculture”, Arnes, Iowa State Press, 2008.
  • the chemical synthesis of ethanol from synthesis gas is also known. It can be carried out, for example, via the intermediate methanol, which is then homologated to ethanol and possibly other higher alcohols. Corresponding methods are disclosed in US 4,882,360 A and US 2013/0123377 A1. Another route is the conversion of methanol to acetic acid and the subsequent hydrogenation of acetic acid to ethanol. Examples include the so-called TCX and the so-called SaaBre process. The production of ethanol by carbonylation of methanol or the hydration of ethylene is also known.
  • the object of the present invention is to provide a method and a system by means of which or from which a sufficiently pure ethanol product can be formed from a corresponding substance mixture efficiently and with a low expenditure of energy.
  • the object of the present invention is thus to improve known processes for the production of ethanol from synthesis gas.
  • the invention proposes a process for the production of ethanol in which a feed mixture containing hydrogen and carbon monoxide and / or carbon dioxide, ie the components of synthesis gas, to obtain a product mixture containing methanol, ethanol, water, carbon dioxide and compounds boiling lower than carbon dioxide , is subjected to a catalytic ethanol direct synthesis.
  • a separation insert is formed in the context of the present invention, which contains methanol, ethanol, water, carbon dioxide and compounds boiling lower than carbon dioxide.
  • synthesis gas is referred to below, this is understood, as usual, to mean, in the language used here, a gas mixture which contains at least predominantly carbon monoxide and hydrogen.
  • carbon dioxide may also be contained and reacted accordingly.
  • the above-mentioned catalytic ethanol direct synthesis of ethanol is used. This means that in the context of the present invention, ethanol is synthesized at least in part without the formation of removable intermediates from carbon monoxide and hydrogen. Possibly formed in the direct synthesis of ethanol intermediates react at least partially, especially still on the catalyst immediately further to ethanol and therefore can not be separated. A process for the direct synthesis of ethanol therefore differs from the above-mentioned process for the two-stage synthesis of methanol or acetic acid, which are formed as separately handled and especially separable intermediates and then further reacted.
  • a main product of a synthesis is here understood to mean a product which has a molar fraction of more than 10%, in particular more than 10%, more than 20%, more than 30%, more than 40%, more than 50%, more than 60% %, more than 70%, more than 80% or more than 90%, based on all formed in the synthesis
  • Products includes. If, for example, 50% ethanol and 50% methanol are formed in a direct synthesis of ethanol, the ethanol formed is still one or one of the main products of the synthesis.
  • the direct synthesis of ethanol used in the present invention in addition to methanol, preferably only small amounts of others, i. higher, formed alcohols. These therefore preferably form only by-products. However, if necessary, not inconsiderable amounts of methane are formed.
  • the particular product spectrum formed depends essentially on the catalyst used.
  • Product mixture is formed, it is understood that not the complete product mixture must be used to form the separation insert and if appropriate, additional compounds, mixtures and the like can be used in the formation of such a feed mixture.
  • the methanol, the ethanol and the water leaving a residual fraction which is low in methanol, ethanol and water and containing carbon dioxide and lower than carbon dioxide boiling compounds, at least for the most part separated from the separation insert by the separation insert in several cooling steps, in particular gradually by means of a plurality of heat exchangers, as also explained below, is cooled to a temperature level of less than 10 ° C and downstream of the cooling steps each methanol, ethanol and water-containing condensates are separated from the separation insert.
  • an at least predominantly methanol, at least predominantly ethanol and at least predominantly water-containing fraction are formed and at least part of the residual fraction is depleted of carbon dioxide, in particular freed from carbon dioxide.
  • Liquid and gaseous mixtures may be rich or poor in one or more components as used herein, with “rich” for a content of at least 40%, 50%, 60%, 70%, 80%, 90%, 95%, 99% %, 99.5%, 99.9% or 99.99% and “poor” for a content of at most 50%, 25%, 10%, 5%, 1%, 0.1% or 0.01% Molar, weight or volume basis can stand. If a mixture contains "predominantly" one or more components, it is particularly rich in this or that in the sense of the definition just made. The present application is used for the characterization of pressures and
  • pressure levels and temperature levels can be in disjoint areas or in areas that overlap one another.
  • pressure levels also include different pressures that are different
  • distillation in the context of the present invention is carried out in particular in two distillation columns.
  • thermal energy for structural design of distillation columns reference is made to relevant textbooks, for example K. Sattler: Thermal
  • a distillation column is typically always at least one liquid fraction ("bottom liquid”) and a gaseous fraction ("top gas”) in a lower (“swamp”) or upper region ("head”) removable.
  • a distillation column is a separating device which is set up in gaseous or liquid form or in the form of a two-phase mixture with liquid and gaseous fractions, if appropriate also in the supercritical state,
  • Substance mixture to produce each pure substances or mixtures which are enriched or depleted compared to the mixture with respect to at least one component or rich or poor in the above-mentioned sense. Typically they are
  • Distillation columns formed as a cylindrical metal container, which are equipped with internals, such as trays or ordered or disordered packages.
  • One of the distinguishing features of a distillation column is that the bottoms liquid is partially heated by means of a bottom evaporator, so that a portion is continuously vaporized and rises in gaseous form in the distillation column.
  • a distillation column is also typically with a so-called
  • Top condenser provided, in which at least a portion of the head gas to a
  • Condensate is liquefied and fed as a liquid reflux at the top of the distillation column.
  • part of the top gas can also be used elsewhere, for example as a product.
  • corresponding carbon dioxide removal steps include passing a carbon dioxide-containing gas mixture in a wash column to an amine-containing liquid or liquor.
  • a corresponding amine-containing gas mixture in a wash column to an amine-containing liquid or liquor.
  • Liquid may contain, for example, monoethanolamine (MEA), diethanolamine (DEA), methyldiethanolamine (MDEA) and / or diglycolamine (DGA).
  • MEA monoethanolamine
  • DEA diethanolamine
  • MDEA methyldiethanolamine
  • DGA diglycolamine
  • Regeneration of the amine-containing liquid or liquor can be desorbed from this in a second column, the carbon dioxide after heating and relaxation again.
  • a corresponding desorption of transferred into the amine-containing liquid methanol and ethanol is not readily possible. Methanol and ethanol would have to be distilled off from the amine-containing liquid consuming. Unless the components are separated, they will accumulate in the liquid or liquor and result in deterioration of absorption.
  • the last of the several cooling steps comprises a cooling of the separation insert in a cooled with an organic liquid refrigerant heat exchanger.
  • the aforementioned temperature level of less than 10 ° C can be achieved.
  • the cooling upstream of this last heat exchanger can be achieved.
  • a previous cooling step carried out upstream of the last cooling step comprises cooling of the separation insert in a heat exchanger cooled by cooling water, and that at least one further cooling step of the separation insert is carried out in an air-cooled heat exchanger upstream of the previous cooling step.
  • the cooling step of the separation insert in the air-cooled heat exchanger can also be omitted in certain cases.
  • the present invention is particularly suitable for processes in which the separation insert in the several cooling steps, starting from a
  • Temperature level is cooled from 100 to 250 ° C. This temperature level is typically downstream of an ethanol direct synthesis reactor. The several cooling steps are advantageously carried out in the context of the present invention at a pressure level of initially 20 to 100 bar.
  • the distillation is advantageously carried out at a pressure level of 2 to 10 bar.
  • two operated at different pressure levels distillation columns can be used, whereby a particularly energy-saving separation can be achieved.
  • the condensates for distillation can be fed, in particular, first into a first distillation column in which a bottoms liquid is formed and taken in part as the fraction containing at least predominantly water.
  • the at least predominantly water-containing fraction is that fraction with the highest boiling point, which therefore can be separated comparatively easily and because of the boiling point separation to methanol and ethanol. Residues of methanol and ethanol can also be contained in this fraction.
  • first head gas condensate is deposited, which is partially recycled to the first distillation column and transferred in part to a second distillation column.
  • the first overhead gas fraction still contains a part of the alcohols contained in the top gas of the first distillation column.
  • Recovery is advantageously subjected to the first overhead gas fraction of a second Kopfgasabkühlung downstream of which, leaving a methanol, ethanol and water poor or free gaseous second Kopfgasrestfr hope second head gas condensate is deposited, which is at least partially transferred to the second distillation column. Because the first and the second top gas condensate differ in their compositions, these or their corresponding proportions are advantageously at different heights in the second
  • the distillation column By the explained treatment of the top gas of the first distillation column, ie, only partial condensation after the first top gas cooling and the further condensation after the second top gas cooling, it is possible to operate a heat exchanger used for the first head gas cooling at a temperature level which is higher than the temperature level which is used in a bottom evaporator of the second distillation column. In this way it is possible to thermally couple the heat exchanger used for the first Kopfgasabkühlung and the bottom evaporator of the second distillation column.
  • the second distillation column is to be operated at a lower pressure level than the first distillation column.
  • the sump vaporizer he second distillation column is operated with waste heat of the heat exchanger used for the first Kopfgaskkühlung.
  • the use of a second cooling stage for the recovery of the desired products makes sense. Because the comparatively high temperature in the first head gas cooling causes a loss of the value products methanol and ethanol in the first Kopfgasrestfr neglect, this is the second Kopfgasabkühlung, in particular to a temperature level below the cooling water temperature subjected. However, since the first head gas cooling has already taken place and thus a large part of methanol and ethanol are already separated, and because the temperature has already been considerably reduced by the first head gas cooling, the second head gas cooling is energy-saving, ie. using relatively low refrigerant flows and small building
  • the second distillation column is advantageously operated at a pressure level which is below a pressure level at which the first distillation column is operated.
  • the Pressure difference can be, for example, 1 to 10 bar, with the first
  • Distillation column for example, at 2 to 10 bar and the second distillation column, for example at 1 to 5 bar can be operated.
  • a bottoms liquid is formed therein, which can be taken in part as the at least predominantly ethanol-containing fraction.
  • Top gas from the second distillation column may be subjected to a third overhead gas cooling downstream of which a third top gas condensate is separated leaving a methanol-lean or free third gas overhead gas fraction, which is partly recycled to the second distillation column and partly withdrawn as the at least predominantly methanol-containing fraction ,
  • the present invention further extends to a plant for the production of ethanol, which is adapted to a feed mixture containing hydrogen and carbon monoxide to give a product mixture containing methanol, ethanol, water, carbon dioxide and lower than carbon dioxide boiling compounds, a catalytic ethanol direct synthesis submit.
  • This comprises means adapted to form, using the product mixture, a separation insert which also contains methanol, ethanol, water, carbon dioxide and lower than
  • Contains carbon dioxide boiling compounds. According to the invention is a
  • Separating device is provided which is adapted to separate the methanol, the ethanol and the water leaving a residual fraction which is low in methanol, ethanol and water and contains carbon dioxide and compounds boiling lower than carbon dioxide, at least for the most part from the separation insert by the separation insert is cooled in several cooling steps to a temperature level of less than 10 ° C and downstream of the cooling steps in each case methanol, ethanol and water-containing condensates are separated from the separation insert.
  • means are provided which are designed to form at least predominantly methanol, an at least predominantly ethanol and an at least predominantly water-containing fraction using the condensates by distillation and to deplete at least a portion of the residual fraction of carbon dioxide.
  • a corresponding installation is set up in particular for carrying out a method, as has been explained in detail above, and has corresponding means for this purpose. Reference is therefore expressly made to the features and advantages mentioned above with regard to the method in its embodiments.
  • FIG. 1 illustrates a method according to an embodiment of the invention.
  • FIG. 1 illustrates a method according to an embodiment of the invention in the form of a schematic process flow diagram and is denoted overall by 100.
  • the elements shown in Figure 1 at the same time make up parts of a
  • a product stream is generated by catalytic ethanol direct synthesis (not illustrated) which is used to form a separation feed in the form of a stream a. This becomes a cooling and
  • the stream a has in particular unreacted hydrogen, not
  • the material flow a is initially passed through a heat exchanger HX1, which can be cooled, for example, with air.
  • a liquid phase is formed, which can then be separated off in a separator D1 and withdrawn in the form of a stream b.
  • a gaseous portion is withdrawn from the head of the separator D1 (not separately designated) and passed through a heat exchanger HX2, out, which can be cooled, for example, with water.
  • a liquid phase is formed, which can then be separated in a separator D2 and withdrawn in the form of a stream c.
  • a gaseous portion is withdrawn from the head of the separator D2 (again not separately designated) and passed through a heat exchanger HX3, out, which can be cooled with a suitable coolant. By cooling, a liquid phase is formed at a temperature level of less than 10 ° C, which can then be deposited in a separator D3 and withdrawn in the form of a stream d.
  • a gaseous portion is in the form of a stream e from the head of
  • the stream e is low in methanol, ethanol and water and possibly other liquid secondary components and can be introduced, for example, in a carbon dioxide removal step, without having to recover the valuable products consuming or losing. It consists i.d.R.
  • the streams b to d contain essentially the components methanol, ethanol and water and optionally further liquid secondary components and lighter components dissolved from the gas phase.
  • the thus obtained condensate streams b to d are expanded in throttle bodies V1, V2, V3 and introduced at different heights in a first distillation column C1.
  • the distillation column C1 is operated at a lower pressure than that of the stream a, usually at 2 to 10 bar.
  • the bottom liquid of the first distillation column C1 is water, optionally with heavier impurities, in the form of a stream f, a bottom evaporator in the form of a heat exchanger HX5 and a separator D5 being used.
  • the head gas of the first distillation column C1 the alcohols (especially methanol and ethanol) are obtained with a certain amount of water.
  • the top gas is withdrawn in the form of a stream g, cooled in a heat exchanger HX4 ("first A condensate ("first top gas condensate”) deposited in a separator HX4 is used partly in the form of a stream h as reflux to the first distillation column C.
  • the other part of the condensate is in the form of a stream i at a Throttle V4 further relaxed and introduced into a second distillation column C2.
  • the stream g is only partially condensed in order to be able to operate the heat exchanger HX4 at a higher temperature than that of a bottom evaporator of the second distillation column C2 or its heat exchanger HX8.
  • a thermal coupling of the distillation columns C1 and C2 is possible.
  • this requires the operation of the second distillation column C2 at a lower pressure level than the distillation column C1.
  • the thermal coupling uses the waste heat from the HX4 heat exchanger to operate the HX8 heat exchanger, which makes it possible to increase the energy efficiency of the process.
  • first Kopfgasabkühlung gaseous remainder in the form of a stream k of a further cooling (second Kopfgasabkühlung) in a heat exchanger HX6 to at least one deeper
  • Top gas condensate is optionally expanded via a throttle element V5 and introduced into the second distillation column C2 in the form of a stream I.
  • a gaseous residue of the stream k is poor in alcohols and water and is discharged in the form of a stream m Material stream e combined, thermally recycled or recycled for syngas production.
  • the heat exchanger HX6 is operated at a lower temperature than the heat exchanger HX4.
  • the bottoms liquid of the second distillation column C2 is predominantly ethanol, optionally with a proportion of water, in the form of a stream n, where a
  • the top gas of the second distillation column C2 contains predominantly methanol. It is withdrawn in the form of a stream o, cooled in a heat exchanger HX7 ("third Kopfgasabkühlung") and partially condensed. A condensate deposited in a separator D7 ("third head gas condensate”) is used partly in the form of a stream p as reflux to the second distillation column C1. The other part of the condensate is discharged in the form of a stream q as a product or recycled, for example, in the ethanol direct synthesis. A gaseous residual is withdrawn in the form of a stream r and can be treated similarly to the stream m.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Crystallography & Structural Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

Abstract

L'invention concerne un procédé (100) de fabrication d'éthanol, selon lequel un mélange de charge contenant de l'hydrogène ainsi que du monoxyde de carbone et/ou du dioxyde de carbone est soumis à une synthèse directe d'éthanol catalytique (2), ce qui permet d'obtenir un mélange de réaction contenant du méthanol, de l'éthanol, de l'eau, du dioxyde de carbone et des composés dont la température d'ébullition inférieure à celle du dioxyde de carbone, le mélange de réaction permettant d'obtenir une charge de séparation contenant du méthanol, de l'éthanol, de l'eau, du dioxyde de carbone et des composés dont la température d'ébullition est inférieure à celle du dioxyde de carbone. L'invention prévoit que le méthanol, l'éthanol et l'eau soient séparés, au moins pour une grande fraction, de la charge de séparation en laissant une fraction résiduelle qui est pauvre en méthanol, éthanol et eau et qui contient du dioxyde de carbone et des composés de température d'ébullition inférieure à celle du dioxyde de carbone, la charge de séparation étant refroidie en plusieurs étapes de refroidissement et amenée à un niveau de température de moins de 10 °C et, en aval des étapes de refroidissement, des condensats contenant respectivement du méthanol, de l'éthanol et de l'eau sont séparés de la charge de séparation, les condensats permettant la formation par distillation d'une fraction contenant majoritairement du méthanol, d'une fraction contenant majoritairement de l'éthanol et d'une fraction contenant au moins majoritairement de l'eau; et au moins une partie de la fraction résiduelle étant enrichie en dioxyde de carbone. L'invention concerne également un objet correspondant.
PCT/EP2017/025104 2016-06-01 2017-05-04 Procédé et dispositif de fabrication d'éthanol Ceased WO2017207106A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102016006707.1 2016-06-01
DE102016006707.1A DE102016006707A1 (de) 2016-06-01 2016-06-01 Verfahren und Anlage zur Herstellung von Ethanol

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WO2017207106A1 true WO2017207106A1 (fr) 2017-12-07

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Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090069452A1 (en) * 2007-09-07 2009-03-12 Range Fuels, Inc Methods and apparatus for producing ethanol from syngas with high carbon efficiency

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4882360A (en) 1984-07-30 1989-11-21 The Dow Chemical Company Process for producing alcohols from synthesis gas
BR112013000301B1 (pt) 2010-07-05 2018-06-26 Haldor Topsoe A/S Processo para a preparação de etanol e álcoois superiores

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20090069452A1 (en) * 2007-09-07 2009-03-12 Range Fuels, Inc Methods and apparatus for producing ethanol from syngas with high carbon efficiency

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