WO2015005941A1 - Procédé pour la fabrication d'isoprène d'origine biologique - Google Patents

Procédé pour la fabrication d'isoprène d'origine biologique Download PDF

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WO2015005941A1
WO2015005941A1 PCT/US2013/067031 US2013067031W WO2015005941A1 WO 2015005941 A1 WO2015005941 A1 WO 2015005941A1 US 2013067031 W US2013067031 W US 2013067031W WO 2015005941 A1 WO2015005941 A1 WO 2015005941A1
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Prior art keywords
isobutene
isoprene
acetic acid
biobased
catalyst
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PCT/US2013/067031
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English (en)
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Junming SUN
Changjun Liu
Yong Wang
Colin Smith
Kevin Martin
Padmesh Venkitasubramanian
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Washington State University
Archer Daniels Midland Company
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Publication of WO2015005941A1 publication Critical patent/WO2015005941A1/fr
Priority to US14/683,252 priority Critical patent/US9975818B2/en

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    • 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
    • B01J23/002—Mixed oxides other than spinels, e.g. perovskite
    • 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
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/0201—Impregnation
    • 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
    • C07C1/207—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms from carbonyl compounds
    • C07C1/2072—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms from carbonyl compounds by condensation
    • C07C1/2074—Preparation of hydrocarbons from one or more compounds, none of them being a hydrocarbon starting from organic compounds containing only oxygen atoms as heteroatoms from carbonyl compounds by condensation of only one compound
    • 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
    • C07C2/86—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon
    • C07C2/862—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms
    • C07C2/867—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by condensation between a hydrocarbon and a non-hydrocarbon the non-hydrocarbon contains only oxygen as hetero-atoms the non-hydrocarbon is an aldehyde or a ketone
    • 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
    • C07C41/00—Preparation of ethers; Preparation of compounds having groups, groups or groups
    • C07C41/01—Preparation of ethers
    • C07C41/05—Preparation of ethers by addition of compounds to unsaturated compounds
    • C07C41/06—Preparation of ethers by addition of compounds to unsaturated compounds by addition of organic compounds only
    • 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
    • C07C45/51—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition
    • C07C45/511—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition involving transformation of singly bound oxygen functional groups to >C = O groups
    • C07C45/513—Preparation of compounds having >C = O groups bound only to carbon or hydrogen atoms; Preparation of chelates of such compounds by pyrolysis, rearrangement or decomposition involving transformation of singly bound oxygen functional groups to >C = O groups the singly bound functional group being an etherified hydroxyl group
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
    • C07C51/10—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide
    • C07C51/12—Preparation of carboxylic acids or their salts, halides or anhydrides by reaction with carbon monoxide on an oxygen-containing group in organic compounds, e.g. alcohols
    • 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
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2521/00—Catalysts comprising the elements, oxides or hydroxides of magnesium, boron, aluminium, carbon, silicon, titanium, zirconium or hafnium
    • C07C2521/06—Silicon, titanium, zirconium or hafnium; Oxides or hydroxides thereof
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C2523/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00
    • C07C2523/06—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group C07C2521/00 of zinc, cadmium or mercury
    • 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
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/50—Improvements relating to the production of bulk chemicals
    • Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts

Definitions

  • 61/836,188 (the “ ⁇ 88 application"), filed June 18, 2013 for "Process for Making Biobased Fuel Additives”, concerns the manufacture of alkyl-t-butyl ethers useful as antiknock additives for gasoline, for example, methyl-tert- butyl ether (MTBE) and ethyl-tert-butyl ether (ETBE), from a biobased isobutene product made according to either the '433 or '312 applications.
  • MTBE methyl-tert- butyl ether
  • ETBE ethyl-tert-butyl ether
  • isoprene may be made from isobutene or from MTBE
  • the present application concerns the further refinement of making biobased isoprene from biobased isobutene prepared as described in either or both of the '433 and '312 applications or from MTBE prepared as described in the ⁇ 88 application.
  • Isoprene can also be produced from isopentane by a double dehydrogenation.
  • isoprene is produced by a Prins condensation of a C4 olefin feed with an aldehyde, typically formaldehyde, with the C 4 olefin feed commonly including isobutene or one or more isobutene precursors such as an alkyl-t-butyl ether under conditions which will provide isobutene.
  • the isobutene reacts with formaldehyde to give 4,4-dimethyl-m-dioxane which decomposes to provide the desired isoprene product.
  • WO '247 reports a number of examples of processes of this general character.
  • US 4,511 ,751 describes a process wherein isobutene and/or tertiary butanol and a formaldehyde source are fed, together with water, into an acidic aqueous solution continuously or intermittently while maintaining the reaction pressure in an adequate range and at the same time distilling off the isoprene product and unreacted starting materials, together with water, from the reaction zone.
  • US 4,593,145 is cited for describing a process for producing isoprene, characterized in that an alkyl-t-butyl ether (e.g., methyl-t-butyl ether (MTBE) or ethyl-t-butyl ether (ETBE) as are still commercially manufactured and extensively used as antiknock fuel additives) and a formaldehyde source are fed, together with water, into an acidic aqueous solution continuously or intermittently while maintaining the reaction pressure in an adequate range and at the same time distilling off the product isoprene, unreacted starting materials, isobutene and tertiary butanol, together with water, from the reaction zone.
  • alkyl-t-butyl ether e.g., methyl-t-butyl ether (MTBE) or ethyl-t-butyl ether (ETBE) as are still commercially manufactured and extensively used as antiknock fuel additives
  • MTBE methyl-
  • isoprene from tertiary alkyl ethers (such as MTBE) and an oxygen source by a catalytic process.
  • MTBE tertiary alkyl ethers
  • oxygen source such as MTBE
  • isoprene is produced by passing a mixture of MTBE and air over a mixed oxide catalyst, cracking the MTBE to isobutene and methanol, oxidizing the methanol to formaldehyde and then reacting the isobutene and formaldehyde to produce isoprene.
  • Other references supply isobutene and methanol separately.
  • the methanol is oxidized to formaldehyde alongside methanol generated from the cracking of MTBE, and the formaldehyde so formed reacts with the supplied isobutene plus that isobutene generated from the cracking of MTBE.
  • Still other references supply isobutene and methanol directly rather than generating the same by cracking MTBE, oxidizing the methanol to formaldehyde with an oxygen source in the presence of an oxidation catalyst and then reacting the formaldehyde thus formed with the isobutene feed.
  • the WO'247 application provides a process for making isoprene using isobutanol, especially isobutanol produced using biomass as a primary feedstock, as an isobutene precursor. More particularly, at least 25 mole percent of the carbon implicated in the isobutanol is obtained from renewable resources, whether by the base-catalyzed Guerbet condensation of methanol with ethanol and/or propanol, by hydrogenation of synthesis gas from the gasification of biomass and/or by an amino acid biosynthetic route from carbohydrates from biomass.
  • the at least partly bioderived isobutanol in turn provides at least 10 up to 100 percent of the isobutene, with the balance being provided by t-butanol, another isobutene precursor such as MTBE or from fresh isobutene.
  • the present invention concerns a process for making isoprene wherein a biobased isobutene prepared as described in either of these applications is combined with a formaldehyde source to form a reaction mixture, and the reaction mixture is reacted to provide a product mixture, then isoprene is recovered from the product mixture.
  • the reaction mixture is reacted while distilling away a mixture comprising produced isoprene, water, unreacted starting materials and other low boiling components.
  • the present invention concerns a process for making isoprene wherein MTBE produced from a biobased isobutene in the manner of the "188 application is cracked to provide isobutene and methanol, methanol from the MTBE is oxidized to provide a source of formaldehyde, and the formaldehyde and isobutene are combined to form a reaction mixture.
  • the reaction mixture is reacted to provide a product mixture, then isoprene is recovered from the reaction mxture.
  • the reaction mixture is reacted while distilling away a mixture comprising produced isoprene, water, unreacted starting materials and other low boiling components.
  • the present invention concerns a process wherein both biobased isobutene and MTBE prepared from biobased isobutene are combined with a formaldehyde source to form a reaction mixture, and the reaction mixture is reacted to provide a product mixture, then isoprene is recovered from the product mixture.
  • the reaction mixture is reacted while distilling away a mixture comprising produced isoprene, water, unreacted starting materials and other low boiling components.
  • wholly biobased butyl rubber is provided by copolymerizing biobased isobutene prepared as described in either of the '433 and '312 applications with biobased isoprene prepared using additional of the same biobased isobutene and a wholly biobased formaldehyde source and/or using a wholly biobased MTBE prepared in the manner of the ⁇ 88 application.
  • Figure 1 schematically depicts a process for making isoprene using biobased isobutene prepared from acetic acid.
  • Figure 2 schematically depicts a process for making isoprene from MTBE prepared from biobased isobutene.
  • Figure 3 schematically depicts a process combining the processes of Figures 1 and 2, for making isoprene using both biobased isobutene and MTBE prepared from biobased isobutene according to the third aspect described above.
  • Figure 4 schematically depicts a process for making a wholly biobased butyl rubber using biobased isobutene and using isoprene prepared from the biobased isobutene and from formaldehyde made from methanol, according to the fourth aspect of the invention described above.
  • Figure 5 schematically depicts a particular embodiment of a process of the type shown in Figure 4.
  • FIG. 1 a process embodiment 10 according to a first aspect is schematically illustrated wherein acetic acid 12 is converted to isobutene 14 in the presence of a catalyst, particularly, a Zn x Zr y O z mixed oxide catalyst, and the isobutene 14 is then reacted with formaldehyde 16 to produce an isoprene product 18.
  • a catalyst particularly, a Zn x Zr y O z mixed oxide catalyst
  • the methanol 20 from which the formaldehyde 16 is obtained (by oxidation according to any of the commercially-practiced or known methods) is wholly biobased in origin, being derived from biological carbon sources rather than from methane from natural gas, for example, a wholly biobased isoprene 18 may be obtained.
  • biobased we mean those materials whose carbon content is shown by ASTM D6866 to be derived from or based in significant part (at least 20 percent or more) upon biological products or renewable agricultural materials (including but not being limited to plant, animal and marine materials) or forestry materials. "Wholly biobased” thus will be understood as referring to materials whose carbon content by ASTM D6866 is entirely or substantially entirely (for example, 95 percent or more) indicated as of biological origin.
  • ASTM Method D6866 similar to radiocarbon dating, compares how much of a decaying carbon isotope remains in a sample to how much would be in the same sample if it were made of entirely recently grown materials. The percentage is called the biobased content of the product.
  • Samples are combusted in a quartz sample tube and the gaseous combustion products are transferred to a borosilicate break seal tube.
  • liquid scintillation is used to count the relative amounts of carbon isotopes in the carbon dioxide in the gaseous combustion products.
  • 13C/12C and 14C/12C isotope ratios are counted (14C) and measured (13C/12C) using accelerator mass spectrometry.
  • Zero percent 14C indicates the entire lack of 14C atoms in a material, thus indicating a fossil (for example, petroleum based) carbon source.
  • One hundred percent 14C after correction for the post-1950 bomb injection of 14C into the atmosphere, indicates a modern carbon source.
  • ASTM D6866 effectively distinguishes between biobased materials and petroleum derived materials in part because isotopic fractionation due to physiological processes, such as, for example, carbon dioxide transport within plants during photosynthesis, leads to specific isotopic ratios in natural or biobased compounds.
  • the 13C/12C carbon isotopic ratio of petroleum and petroleum derived products is different from the isotopic ratios in natural or bioderived compounds due to different chemical processes and isotopic fractionation during the generation of petroleum.
  • radioactive decay of the unstable 14C carbon radioisotope leads to different isotope ratios in biobased products compared to petroleum products.
  • Acetic acid 12 can be obtained by various methods from a number of starting materials, which in turn permits a number of integrated processes to be considered for producing the isoprene 18 with improved utilization of renewable resources.
  • An example is schematically shown in Figure 5, discussed more fully below.
  • acetic acid can be produced from a source of five and six carbon sugars 22 by fermentation.
  • US 6,509,180 and US 8,252,567 seek to improve upon known processes for making ethanol and
  • butanol/hexanol respectively, by means including the fermentation of five and six carbon sugars into acetic acid.
  • the acetic acid is esterified to form an acetate ester which may then be hydrogenated (using hydrogen from, e.g., steam reforming of natural gas, electrolysis of water, gasification of biomass or partial oxidation of hydrocarbons generally) to ethanol.
  • the ethanol formed in this manner can be used to make butanol and hexanol, by subjecting the ethanol with acetate, acetic acid or mixtures thereof to an acidogenic fermentation using, for example, species of the bacteria Clostridium (Clostridium kluyveri ⁇ s mentioned), to produce butyrate, butyric acid, caproate, caproic acid or mixtures thereof.
  • Clostridium Clostridium kluyveri ⁇ s mentioned
  • These materials then in turn are acidified to convert butyrate and caproate to butyric acid and caproic acid, the butyric and caproic acids are esterified and then the butyric and caproic acid esters undergo reduction by hydrogenation, hydrogenolysis or reduction by carbon monoxide to provide butanol and ethanol.
  • the fermentation of five and six carbon sugars to form acetic acid can be accomplished by various organisms. More particularly, homoacetogenic microorganisms are able through fermentation to produce acetic acid with 00% carbon yield; these microorganisms internally convert carbon dioxide to acetate, in contrast to a process for producing ethanol from sugars obtained from biomass, wherein carbon dioxide is produced as a byproduct.
  • Any of the known fermentation methods may, in short, be used to produce acetic acid 12 for conversion to isobutene 14 as shown in Fig. 1, but homoacetogenic fermentation methods are considered preferable in that carbon dioxide is not produced as a byproduct - the carbon dioxide represents a yield loss from the overall process to make isobutene and as a greenhouse gas is undesirable particularly in the context of a process to make a needed product more sustainably from renewable resources.
  • the acetic acid feedstock 12 can be made from ethanol 24, according to any of several known methods employing oxidative fermentation with acetic acid bacteria of the genus Acetobacter.
  • the acetic acid feedstock 12 can be made from methanol 20, through combination with carbon monoxide according to the most industrially used route for making acetic acid, for example, in the presence of a catalyst under conditions effective for the carbonylation of methanol.
  • a catalyst under conditions effective for the carbonylation of methanol.
  • a variety of carbonylation catalysts are known in this regard, see, for example, US 5,672,743; US 5,728, 871 ; US 5,773,642; US 5,883,289; US 5,883,295.
  • the wholly biobased isobutene 14 enabled by the process of the '312 application and formaldehyde 16 may be reacted as schematically shown in Figure 1 to produce isoprene 18 according to any of a number of known methods, including but not limited to those methods summarized above and described more fully in the WO'247 application; US 4,511 ,751 ; US 4,593,145; EP 106323; EP 1614671 ; EP 2157072; GB 1370899; US
  • isoprene 28 from a biobased methyl-t-butyl ether (MTBE) 30 according to a second aspect of the present invention.
  • MTBE biobased methyl-t-butyl ether
  • the biobased MTBE 30 can be combined with air and converted to isoprene as described in US 3,574,780, through passing a mixture of MTBE 30 and air over a mixed oxide catalyst, cracking the MTBE 30 to isobutene and methanol, oxidizing the methanol to formaldehyde and then reacting the isobutene and formaldehyde to produce the isoprene 28.
  • the biobased MTBE 30 in turn is produced by a process as described in the "188 application, from isobutene 32 produced from acetic acid 34 produced as described in the '312 application (using a catalyst, particularly a Zn x Zr y O z mixed oxide catalyst, and especially a Zn x Zr y O z mixed oxide catalyst made as described in the '433 application) and from methanol 36.
  • methanol 36 (beyond that used to form the MTBE 30 and produced therefrom as described in US 3,574,780) and additional isobutene 32 can be supplied alongside the MTBE 30 to make the isoprene 28.
  • isobutene 32 and methanol 36 can be supplied directly for oxidation and without a separate step of forming the MTBE 30; the methanol is oxidized to formaldehyde with an oxygen source in the presence of an oxidation catalyst, and the formaldehyde is then reacted with the isobutene feed preferably using the same catalyst to produce the isoprene 28.
  • a process 38 is shown in which acetic acid 40 is converted to isobutene 42 as described in the '312 application.
  • a portion of the isobutene 42 is combined with a corresponding portion of methanol 44 to produce MTBE 46, and at least a portion of the MTBE 46 is converted to isoprene 48 by cracking the MTBE to isobutene and methanol, oxidizing the methanol to formaldehyde and causing the isobutene and formaldehyde to react to form the desired isoprene.
  • the isobutene and formaldehyde thus derived are supplemented in the process 38 by additional isobutene 42 and by
  • formaldehyde 50 separately produced from additional methanol 44 according to known processes.
  • a wholly biobased butyl rubber can be made.
  • Processes for the copolymerization of isobutene and isoprene are well known and have been commercially practiced for years, though some recent examples of published patent applications and/or patents for processes for making such copolymers include EP 1215241 B1 , EP 1449859A1 , EP 1426387B1 , US 7,041,760 and US 7,851,577.
  • any known process for copolymerizing isobutene and isoprene may be used, however.
  • acetic acid 54 (whether obtained by fermentation of five and/or six-carbon sugars 56, from ethanol 58 by oxidative fermentation, from methanol 60 by carbonylation or a combination of these, all as described above) is converted to wholly biobased isobutene 62 by a process as described in the '312 application and summarized below.
  • Wholly biobased isoprene 64 is prepared from formaldehyde 66, with the formaldehyde 66 in turn being prepared by oxidizing a portion of the methanol 60, through cracking of MTBE 68 prepared from wholly biobased isobutene according to the ⁇ 88 application or by a combination of these synthetic methods as previously described.
  • the wholly biobased isobutene 62 and wholly biobased isoprene 64 are then
  • FIG. 5 a non-limiting example 72 is shown of an integrated process for making biobased alternatives to one or more of the valuable products isobutene, isoprene, MTBE and ETBE which have all heretofore been made at least in part through petroleum processing, through use of the core acetic acid to isobutene conversion described in the '312 application.
  • While one example 72 is detailed herein, those skilled in the art and familiar with the known processes for producing methanol, ethanol and acetic acid (some of which have been mentioned above or will be mentioned below) and with the known methods by which the "building block" gases carbon dioxide, carbon monoxide and hydrogen may be generated and used to make one or more of the same methanol, ethanol and acetic acid feeds will undoubtedly be able to conceive of a number of other integrated process schemes which all make use of the core acetic acid to isobutene conversion, but differ in the precise manner or extent to which carbon dioxide, carbon monoxide and hydrogen gases are optimally used.
  • biomass 74 can be a source of five and six carbon sugars 76, which can undergo a fermentation step 78 as earlier mentioned to make acetic acid 80.
  • Some of the sugars can be fermented according to known methods for fermentation of five- and six-carbon sugars to make ethanol 82, with the ethanol 82 in turn being useful for making ETBE 84 by conventionally practiced etherification process technology and/or for making acetic acid 80 as described above.
  • Carbon dioxide generated as a byproduct in the ethanol fermentation can variously be used as suggested by stream 86 in a homoacetogenic fermentation 78 for making the acetic acid 80, or can be used as suggested by stream 88 to make methanol 90.
  • This carbon dioxide (that is, in streams 86 and 88) can be combined for either or both purposes with carbon dioxide from a variety of other sources, for example, with carbon dioxide captured from industrial emissions, generated in the combustion of fossil fuels, sequestered in underground reservoirs or contained in biosynthesis gas 92 from the combustion, gasification or partial oxidation of biomass 74 or of a non-fermentable biomass fraction generated in a fractionation of the biomass 74 to produce fermentable sugars 76.
  • a biomass fractionation process as described in any of several commonly-assigned, copending applications, namely, published applications WO 2011/097065 and WO 2011/097075 both to Binder et al., as well as Patent Cooperation Treaty Applications Ser. No. PCT/US2012/056593, filed Sept. 21, 2012 for "C C 2 Organic Acid treatment of Lignin Biomass to
  • the methanol 90 can variously be combined with biobased isobutene 94 (from acetic acid 80) for forming the MTBE fuel additive 96, combined with carbon monoxide 98 from biosynthesis gas 92 (or from the electrolytic cleavage of C0 2 from any of the sources mentioned above in connection with the generation of the methanol 90) to produce acetic acid 80 and/or used to make formaldehyde 100, with the latter being useful for combining with isobutene 94 to make isoprene 102.
  • the isoprene 102 and isobutene 94 can then be used to make a butyl rubber product 104, if desired.
  • MTBE 94 can be oxidatively cracked to produce additional of the formaldehyde 100 and isobutene 94.
  • the acetic acid 80 is converted to isobutene 94 as taught in the '312 application, preferably using a Zn x Zr y O z mixed oxide catalyst.
  • the Zn x Zr y 0 2 mixed oxide catalyst can be made by a "hard template” or "confined space synthesis” method generally of the character used by Jacobsen et al., "Mesoporous Zeolite Single Crystals", Journal of the American Chemical Society, vol. 122, pp. 7116-7117 (2000), wherein nanozeolites were prepared.
  • the same carbon black (BP 2000, Cabot Corp.) may be used as a hard template for the synthesis of nanosized
  • the BP 2000 template Prior to use, the BP 2000 template is dried, for example, at 180 °C overnight.
  • Nanosized white powders are obtained, having a mean particle size of less than 10 nanometers.
  • nanosized Zn x Zr y O z mixed oxide catalysts made by a hard template method are further described by Sun et al., in "Direct Conversion of Bio-ethanol to Isobutene on Nanosized Zn x Zr y O z Mixed Oxides with Balanced Acid-Base Sites", Journal of the American Chemical Society, vol. 133, pp 11096-11099 (2011), along with findings related to the character of the mixed oxide catalysts formed thereby and the performance of the catalysts for the ethanol to isobutene conversion, given certain Zn/Zr ratios, residence times and reaction temperatures.
  • the Zn x Zr y O z mixed oxide catalysts may be made as described in the '433 application, by a process broadly comprising, in certain embodiments, forming a solution of one or more Zn compounds, combining one or more zirconium-containing solids with the solution of one or more Zn compounds so that the solution wets the zirconium-containing solids to a state of incipient wetness, drying the wetted solids, then calcining the dried solids.
  • a solution is formed of one or more Zr compounds, the solution is combined with one or more Zn-containing solids so that the solution wets the Zn-containing solids to a state of incipient wetness, the wetted solids are dried and then the dried solids are calcined.
  • the Zn x Zr y O z mixed oxide catalysts are characterized by a Zn/Zr ratio (x:y) of from 1 :100 to 10:1 , preferably from 1 :30 to 1:1 , especially 1 :20 to 1 :5, and still more preferably 1 :12 to 1 :10.
  • any range of values is given for any aspect or feature of the mixed oxide catalysts or any process described for using the mixed oxide catalysts
  • the given ranges will be understood as disclosing and describing all subranges of values included within the broader range.
  • the range of 1 :100 to 10:1 will be understood as disclosing and describing not only the specific preferred and more preferred subranges given above, but also every other subrange including a value for x between 1 and 10 and every other subrange including a value for y between 1 and 100.
  • the catalysts made by the alternative, incipient wetness method are consistent in their particle size with the catalysts described in the Jacobsen et al. article, namely, comprising aggregates of less thanIO nm- sized particles with a highly crystalline structure.
  • the Zn oxide component is again highly dispersed on the Zr oxide component.
  • the Zn x Zr y O z mixed oxide catalysts are characterized as low sulfur catalysts, containing less than 0.14 percent by weight of sulfur.
  • catalysts made by the incipient wetness method would desirably be substantially sulfur-free, preferably including less than 0.01 percent by weight of sulfur and more preferably including less than 0.001 weight percent of sulfur. It was postulated that the reduced sulfur content enabled by the incipient wetness method as compared to the hard template method contributed significantly to the much improved stability observed for the incipient wetness method catalysts of the '433 application for the ethanol to isobutene process.
  • any combination of zinc and zirconium materials and any solvent can be used that will permit the zinc and zirconium components to mix homogeneously whereby, through incipient wetness impregnation, one of the zinc or zirconium components are well dispersed on a solid of the other component for subsequent drying and conversion to the oxide forms through calcining.
  • low sulfur catalysts can also be made by the incipient wetness method starting with zinc and zirconium compounds that are sulfur-free or substantially sulfur-free, then doping in a desired sulfur content into the Zn x Zr y O z mixed oxide catalysts used in certain embodiments of the acetic acid to isobutene process of the '312 application.
  • drying step can be accomplished in a temperature range of from 60 degrees Celsius to 200 degrees Celsius over at least 3 hours, while the calcination can take place at a temperature of from 300 degrees Celsius to 1500 degrees Celsius, but more preferably a temperature of from 400 to 600 degrees Celsius is used.
  • the calcination time can be from 10 minutes to 48 hours, with from 2 to 10 hours being preferred.
  • low sulfur catalysts as described could be prepared by a hard template method as described in the Jacobsen et al. publication, except that a suitably very low sulfur content carbon is used for the hard template to realize a low sulfur content in the finished catalyst.
  • the acetic acid to isobutene process can be conducted continuously in the gas phase, using a fixed bed reactor or flow bed reactor.
  • the reaction temperature may be in a range from 350 to 700 degrees Celsius, preferably, in a range from 400 to 500 degrees Celsius
  • the WHSV can be in a range from 0.01 hr "1 to 10 hr " ⁇ preferably from 0.05 hr "1 to 2 hr '1 .
  • Acetic acid/water solutions with steam to carbon ratios from 0 to 20, preferably from 2 to 5 can be used to provide acetic acid to the catalyst.
  • An inert carrier gas such as nitrogen, can be used.
  • Ethanol to isobutene runs were conducted with the catalysts thus prepared in a fixed-bed stainless steel reactor, having an inside diameter of 5 millimeters. A given amount of catalyst was packed between quartz wool beds. A thermocouple was placed in the middle of the catalyst bed to monitor the reaction temperatures. Before beginning the reaction, the catalyst beds were first pretreated by flowing 50 ml/minute of nitrogen at 450 degrees Celsius through the catalyst over a half hour, then a mixture of ethanol/water at steam to carbon ratios from 1 to 5 was introduced into an evaporator at 180 degrees Celsius by means of a syringe pump and carried into the reactor by the flowing nitrogen carrier gas. Meanwhile, the product line was heated to in excess of 150 degrees Celsius before a cold trap, to avoid condensing the liquid products in the product line.
  • [0057JA Shimadzu 2400 gas chromatograph equipped with an auto sampling valve, HP-Plot Q column (30 m, 0.53 mm, 40 pm) and flame ionization detector was connected to the line between the reactor outlet and cold trap to collect and analyze the products in the effluent gas.
  • an online micro-GC MicroGC 3000A equipped with molecular sieves 5A, plot U columns and thermal conductivity detectors was used to analyze the product gases specifically, using nitrogen as a reference gas.
  • MicroGC MicroGC 3000A equipped with molecular sieves 5A, plot U columns and thermal conductivity detectors
  • a number of additional catalysts were prepared by first drying commercial zirconium hydroxide at 120 degrees Celsius for more than 5 hours. Calculated amounts of Zn(N0 3 )2 (from Sigma-Aldrich, more than 99.8 percent purity) were dissolved in water to form a series of clear solutions. The dried zirconium hydroxide (also from Sigma-Aldrich, more than 99.8 percent purity) was then mixed with the solutions in turn by incipient wetness, in order to form wet powders impregnated with Zn in certain proportions to the zirconium in the form of the dried zirconium hydroxide powder.
  • the wetted powders were then dried at 80 degrees Celsius for 4 hours, followed by calcination at the temperature indicated in Table 1 below for 3 hours, to obtain a series of Zn x Zr y O z catalysts by an incipient wetness method.
  • These catalysts were used to convert ethanol to isobutene in the manner of Example 1.
  • Particular reaction conditions whether the reaction temperature, WHSV or steam to carbon ratio, for example, were varied to compare the effect on the selectivities to acetone and isobutene at full conversion of the ethanol.
  • some amount of sulfur was purposely doped into the catalyst to assess the effect of sulfur at those certain levels on the selectivities to acetone and to isobutene.
  • the catalyst for example 28 was doped with 10 ppm of sulfur, while for example 29 the catalyst was doped with 50 ppm of sulfur and for example 30 with 200 ppm (by weight).
  • additional Zn x Zr y O z mixed oxide catalysts were prepared both by the incipient wetness method (IW in Table 2 below) but also by the prior art hard template method (HT), and these were evaluated and the products analyzed using the same apparatus and method described above but under different sets of reaction conditions (as summarized in Table 2 below).

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Abstract

L'invention porte sur des procédés pour la fabrication d'isoprène d'origine biologique, consistant à combiner de l'isobutène d'origine biologique, préparé à partir d'acide acétique en présence d'un catalyseur, avec une source de formaldéhyde pour former un mélange réactionnel et faire réagir le mélange réactionnel pour produire de l'isoprène d'origine biologique. Dans certains modes de réalisation, de l'oxyde de méthyle et de tert-butyle préparé par réaction du même isobutène d'origine biologique avec du méthanol sert de source de formaldéhyde, qui est craquée par oxydation pour produire du formaldéhyde ainsi que de l'isobutène destiné à être converti en l'isoprène d'origine biologique.
PCT/US2013/067031 2012-10-31 2013-10-28 Procédé pour la fabrication d'isoprène d'origine biologique WO2015005941A1 (fr)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150210607A1 (en) * 2012-10-31 2015-07-30 Archer Daniels Midland Company Use of byproduct acetic acid from oxidative methods of making acrylic acid and/or methacrylic acid
US10633320B2 (en) 2018-01-04 2020-04-28 Gevo, Inc. Upgrading fusel oil mixtures over heterogeneous catalysts to higher value renewable chemicals

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US4511751A (en) * 1982-10-14 1985-04-16 Kuraray Company, Ltd. Process for producing isoprene
US20100216958A1 (en) * 2009-02-24 2010-08-26 Peters Matthew W Methods of Preparing Renewable Butadiene and Renewable Isoprene
US20110172475A1 (en) * 2010-01-08 2011-07-14 Gevo, Inc. Integrated methods of preparing renewable chemicals
US20130115653A1 (en) * 2011-11-09 2013-05-09 Thesis Chemistry, Llc Method for producing biobased chemicals from woody biomass

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4511751A (en) * 1982-10-14 1985-04-16 Kuraray Company, Ltd. Process for producing isoprene
US20100216958A1 (en) * 2009-02-24 2010-08-26 Peters Matthew W Methods of Preparing Renewable Butadiene and Renewable Isoprene
US20110172475A1 (en) * 2010-01-08 2011-07-14 Gevo, Inc. Integrated methods of preparing renewable chemicals
US20130115653A1 (en) * 2011-11-09 2013-05-09 Thesis Chemistry, Llc Method for producing biobased chemicals from woody biomass

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20150210607A1 (en) * 2012-10-31 2015-07-30 Archer Daniels Midland Company Use of byproduct acetic acid from oxidative methods of making acrylic acid and/or methacrylic acid
US9156746B2 (en) * 2012-10-31 2015-10-13 Washington State University Use of byproduct acetic acid from oxidative methods of making acrylic acid and/or methacrylic acid
US10633320B2 (en) 2018-01-04 2020-04-28 Gevo, Inc. Upgrading fusel oil mixtures over heterogeneous catalysts to higher value renewable chemicals

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