US20180258060A1 - Process for synthesis of furan derivative using an acid catalyst and preparation thereof - Google Patents
Process for synthesis of furan derivative using an acid catalyst and preparation thereof Download PDFInfo
- Publication number
- US20180258060A1 US20180258060A1 US15/981,264 US201815981264A US2018258060A1 US 20180258060 A1 US20180258060 A1 US 20180258060A1 US 201815981264 A US201815981264 A US 201815981264A US 2018258060 A1 US2018258060 A1 US 2018258060A1
- Authority
- US
- United States
- Prior art keywords
- hmf
- acid catalyst
- catalyst
- fructose
- reaction
- Prior art date
- Legal status (The legal status 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 status listed.)
- Abandoned
Links
- 238000000034 method Methods 0.000 title claims abstract description 79
- 230000008569 process Effects 0.000 title claims abstract description 72
- 239000003377 acid catalyst Substances 0.000 title claims abstract description 53
- 150000002240 furans Chemical class 0.000 title abstract description 18
- 238000002360 preparation method Methods 0.000 title abstract description 5
- 230000015572 biosynthetic process Effects 0.000 title description 30
- 238000003786 synthesis reaction Methods 0.000 title description 29
- 238000006243 chemical reaction Methods 0.000 claims abstract description 138
- 239000003054 catalyst Substances 0.000 claims abstract description 86
- 239000011973 solid acid Substances 0.000 claims abstract description 27
- 239000003960 organic solvent Substances 0.000 claims abstract description 23
- 238000004519 manufacturing process Methods 0.000 claims abstract description 18
- 239000000725 suspension Substances 0.000 claims description 30
- 229920000642 polymer Polymers 0.000 claims description 27
- 239000003795 chemical substances by application Substances 0.000 claims description 9
- YMWUJEATGCHHMB-UHFFFAOYSA-N Dichloromethane Chemical compound ClCCl YMWUJEATGCHHMB-UHFFFAOYSA-N 0.000 claims description 6
- 239000004372 Polyvinyl alcohol Substances 0.000 claims description 6
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims description 6
- 229920002451 polyvinyl alcohol Polymers 0.000 claims description 6
- KEQGZUUPPQEDPF-UHFFFAOYSA-N 1,3-dichloro-5,5-dimethylimidazolidine-2,4-dione Chemical compound CC1(C)N(Cl)C(=O)N(Cl)C1=O KEQGZUUPPQEDPF-UHFFFAOYSA-N 0.000 claims description 5
- 239000001913 cellulose Substances 0.000 claims description 5
- 229920002678 cellulose Polymers 0.000 claims description 5
- XTHPWXDJESJLNJ-UHFFFAOYSA-N chlorosulfonic acid Substances OS(Cl)(=O)=O XTHPWXDJESJLNJ-UHFFFAOYSA-N 0.000 claims description 5
- HEDRZPFGACZZDS-UHFFFAOYSA-N Chloroform Chemical compound ClC(Cl)Cl HEDRZPFGACZZDS-UHFFFAOYSA-N 0.000 claims description 4
- AKEJUJNQAAGONA-UHFFFAOYSA-N sulfur trioxide Chemical compound O=S(=O)=O AKEJUJNQAAGONA-UHFFFAOYSA-N 0.000 claims description 4
- VZGDMQKNWNREIO-UHFFFAOYSA-N tetrachloromethane Chemical compound ClC(Cl)(Cl)Cl VZGDMQKNWNREIO-UHFFFAOYSA-N 0.000 claims description 4
- WSLDOOZREJYCGB-UHFFFAOYSA-N 1,2-Dichloroethane Chemical compound ClCCCl WSLDOOZREJYCGB-UHFFFAOYSA-N 0.000 claims description 3
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 claims description 3
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims description 3
- 229920002338 polyhydroxyethylmethacrylate Polymers 0.000 claims description 3
- 239000000377 silicon dioxide Substances 0.000 claims description 3
- KNKRKFALVUDBJE-UHFFFAOYSA-N 1,2-dichloropropane Chemical compound CC(Cl)CCl KNKRKFALVUDBJE-UHFFFAOYSA-N 0.000 claims description 2
- 239000004952 Polyamide Substances 0.000 claims description 2
- 239000002202 Polyethylene glycol Substances 0.000 claims description 2
- 229920002873 Polyethylenimine Polymers 0.000 claims description 2
- 229950005499 carbon tetrachloride Drugs 0.000 claims description 2
- 229920000083 poly(allylamine) Polymers 0.000 claims description 2
- 229920002647 polyamide Polymers 0.000 claims description 2
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- 229920001451 polypropylene glycol Polymers 0.000 claims description 2
- 239000001117 sulphuric acid Substances 0.000 claims description 2
- 235000011149 sulphuric acid Nutrition 0.000 claims description 2
- 239000011541 reaction mixture Substances 0.000 abstract description 34
- 235000000346 sugar Nutrition 0.000 abstract description 22
- NOEGNKMFWQHSLB-UHFFFAOYSA-N 5-hydroxymethylfurfural Chemical compound OCC1=CC=C(C=O)O1 NOEGNKMFWQHSLB-UHFFFAOYSA-N 0.000 description 117
- RJGBSYZFOCAGQY-UHFFFAOYSA-N hydroxymethylfurfural Natural products COC1=CC=C(C=O)O1 RJGBSYZFOCAGQY-UHFFFAOYSA-N 0.000 description 116
- 239000005715 Fructose Substances 0.000 description 82
- 229930091371 Fructose Natural products 0.000 description 82
- RFSUNEUAIZKAJO-ARQDHWQXSA-N Fructose Chemical compound OC[C@H]1O[C@](O)(CO)[C@@H](O)[C@@H]1O RFSUNEUAIZKAJO-ARQDHWQXSA-N 0.000 description 80
- 239000002904 solvent Substances 0.000 description 47
- 238000010438 heat treatment Methods 0.000 description 33
- IAZDPXIOMUYVGZ-UHFFFAOYSA-N Dimethylsulphoxide Chemical compound CS(C)=O IAZDPXIOMUYVGZ-UHFFFAOYSA-N 0.000 description 31
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- 238000003756 stirring Methods 0.000 description 27
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 19
- 238000004128 high performance liquid chromatography Methods 0.000 description 19
- ZMXDDKWLCZADIW-UHFFFAOYSA-N N,N-Dimethylformamide Chemical compound CN(C)C=O ZMXDDKWLCZADIW-UHFFFAOYSA-N 0.000 description 16
- JOXIMZWYDAKGHI-UHFFFAOYSA-N toluene-4-sulfonic acid Chemical compound CC1=CC=C(S(O)(=O)=O)C=C1 JOXIMZWYDAKGHI-UHFFFAOYSA-N 0.000 description 16
- 238000002474 experimental method Methods 0.000 description 15
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- 230000035484 reaction time Effects 0.000 description 12
- DKGAVHZHDRPRBM-UHFFFAOYSA-N Tert-Butanol Chemical compound CC(C)(C)O DKGAVHZHDRPRBM-UHFFFAOYSA-N 0.000 description 11
- 229960004592 isopropanol Drugs 0.000 description 11
- 238000003828 vacuum filtration Methods 0.000 description 11
- SECXISVLQFMRJM-UHFFFAOYSA-N N-Methylpyrrolidone Chemical compound CN1CCCC1=O SECXISVLQFMRJM-UHFFFAOYSA-N 0.000 description 10
- 239000000758 substrate Substances 0.000 description 10
- 229910052757 nitrogen Inorganic materials 0.000 description 9
- 239000002253 acid Substances 0.000 description 8
- 150000001720 carbohydrates Chemical class 0.000 description 8
- 238000000926 separation method Methods 0.000 description 8
- 238000007792 addition Methods 0.000 description 7
- LSNNMFCWUKXFEE-UHFFFAOYSA-M Bisulfite Chemical compound OS([O-])=O LSNNMFCWUKXFEE-UHFFFAOYSA-M 0.000 description 6
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- LRHPLDYGYMQRHN-UHFFFAOYSA-N N-Butanol Chemical compound CCCCO LRHPLDYGYMQRHN-UHFFFAOYSA-N 0.000 description 6
- 238000009835 boiling Methods 0.000 description 6
- 238000004064 recycling Methods 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
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- 230000002051 biphasic effect Effects 0.000 description 5
- BTANRVKWQNVYAZ-UHFFFAOYSA-N butan-2-ol Chemical compound CCC(C)O BTANRVKWQNVYAZ-UHFFFAOYSA-N 0.000 description 5
- 230000003197 catalytic effect Effects 0.000 description 5
- 239000000706 filtrate Substances 0.000 description 5
- 229910052500 inorganic mineral Inorganic materials 0.000 description 5
- 239000011707 mineral Substances 0.000 description 5
- 239000000203 mixture Substances 0.000 description 5
- WQZGKKKJIJFFOK-GASJEMHNSA-N Glucose Natural products OC[C@H]1OC(O)[C@H](O)[C@@H](O)[C@@H]1O WQZGKKKJIJFFOK-GASJEMHNSA-N 0.000 description 4
- GWEVSGVZZGPLCZ-UHFFFAOYSA-N Titan oxide Chemical compound O=[Ti]=O GWEVSGVZZGPLCZ-UHFFFAOYSA-N 0.000 description 4
- VSCWAEJMTAWNJL-UHFFFAOYSA-K aluminium trichloride Chemical compound Cl[Al](Cl)Cl VSCWAEJMTAWNJL-UHFFFAOYSA-K 0.000 description 4
- 230000008901 benefit Effects 0.000 description 4
- 238000006297 dehydration reaction Methods 0.000 description 4
- CHTHALBTIRVDBM-UHFFFAOYSA-N furan-2,5-dicarboxylic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)O1 CHTHALBTIRVDBM-UHFFFAOYSA-N 0.000 description 4
- 239000008103 glucose Substances 0.000 description 4
- 239000002638 heterogeneous catalyst Substances 0.000 description 4
- 150000002402 hexoses Chemical class 0.000 description 4
- 238000007144 microwave assisted synthesis reaction Methods 0.000 description 4
- 239000000376 reactant Substances 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- NWUYHJFMYQTDRP-UHFFFAOYSA-N 1,2-bis(ethenyl)benzene;1-ethenyl-2-ethylbenzene;styrene Chemical compound C=CC1=CC=CC=C1.CCC1=CC=CC=C1C=C.C=CC1=CC=CC=C1C=C NWUYHJFMYQTDRP-UHFFFAOYSA-N 0.000 description 3
- 244000144730 Amygdalus persica Species 0.000 description 3
- NTIZESTWPVYFNL-UHFFFAOYSA-N Methyl isobutyl ketone Chemical compound CC(C)CC(C)=O NTIZESTWPVYFNL-UHFFFAOYSA-N 0.000 description 3
- UIHCLUNTQKBZGK-UHFFFAOYSA-N Methyl isobutyl ketone Natural products CCC(C)C(C)=O UIHCLUNTQKBZGK-UHFFFAOYSA-N 0.000 description 3
- 235000006040 Prunus persica var persica Nutrition 0.000 description 3
- CZMRCDWAGMRECN-UGDNZRGBSA-N Sucrose Chemical compound O[C@H]1[C@H](O)[C@@H](CO)O[C@@]1(CO)O[C@@H]1[C@H](O)[C@@H](O)[C@H](O)[C@@H](CO)O1 CZMRCDWAGMRECN-UGDNZRGBSA-N 0.000 description 3
- 229930006000 Sucrose Natural products 0.000 description 3
- 238000007171 acid catalysis Methods 0.000 description 3
- 150000007513 acids Chemical class 0.000 description 3
- 125000003118 aryl group Chemical group 0.000 description 3
- 239000003729 cation exchange resin Substances 0.000 description 3
- 230000018044 dehydration Effects 0.000 description 3
- 150000004676 glycans Chemical class 0.000 description 3
- 125000004356 hydroxy functional group Chemical group O* 0.000 description 3
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- 238000010926 purge Methods 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
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- 238000011069 regeneration method Methods 0.000 description 3
- 239000011347 resin Substances 0.000 description 3
- 229920005989 resin Polymers 0.000 description 3
- SQGYOTSLMSWVJD-UHFFFAOYSA-N silver(1+) nitrate Chemical compound [Ag+].[O-]N(=O)=O SQGYOTSLMSWVJD-UHFFFAOYSA-N 0.000 description 3
- 239000007787 solid Substances 0.000 description 3
- 229960004793 sucrose Drugs 0.000 description 3
- 150000008163 sugars Chemical class 0.000 description 3
- 238000005292 vacuum distillation Methods 0.000 description 3
- 239000010457 zeolite Substances 0.000 description 3
- JOOXCMJARBKPKM-UHFFFAOYSA-N 4-oxopentanoic acid Chemical compound CC(=O)CCC(O)=O JOOXCMJARBKPKM-UHFFFAOYSA-N 0.000 description 2
- OUDFNZMQXZILJD-UHFFFAOYSA-N 5-methyl-2-furaldehyde Chemical compound CC1=CC=C(C=O)O1 OUDFNZMQXZILJD-UHFFFAOYSA-N 0.000 description 2
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 2
- WCUXLLCKKVVCTQ-UHFFFAOYSA-M Potassium chloride Chemical compound [Cl-].[K+] WCUXLLCKKVVCTQ-UHFFFAOYSA-M 0.000 description 2
- FAPWRFPIFSIZLT-UHFFFAOYSA-M Sodium chloride Chemical compound [Na+].[Cl-] FAPWRFPIFSIZLT-UHFFFAOYSA-M 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 2
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 2
- 230000002378 acidificating effect Effects 0.000 description 2
- 125000001931 aliphatic group Chemical group 0.000 description 2
- 229920013724 bio-based polymer Polymers 0.000 description 2
- 238000012769 bulk production Methods 0.000 description 2
- 238000006555 catalytic reaction Methods 0.000 description 2
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- 125000004122 cyclic group Chemical group 0.000 description 2
- 238000006210 cyclodehydration reaction Methods 0.000 description 2
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- 235000021433 fructose syrup Nutrition 0.000 description 2
- HYBBIBNJHNGZAN-UHFFFAOYSA-N furfural Chemical compound O=CC1=CC=CO1 HYBBIBNJHNGZAN-UHFFFAOYSA-N 0.000 description 2
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- -1 hexose sugars Chemical class 0.000 description 2
- PHTQWCKDNZKARW-UHFFFAOYSA-N isoamylol Chemical compound CC(C)CCO PHTQWCKDNZKARW-UHFFFAOYSA-N 0.000 description 2
- 239000011968 lewis acid catalyst Substances 0.000 description 2
- AMXOYNBUYSYVKV-UHFFFAOYSA-M lithium bromide Chemical compound [Li+].[Br-] AMXOYNBUYSYVKV-UHFFFAOYSA-M 0.000 description 2
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- IIPYXGDZVMZOAP-UHFFFAOYSA-N lithium nitrate Chemical compound [Li+].[O-][N+]([O-])=O IIPYXGDZVMZOAP-UHFFFAOYSA-N 0.000 description 2
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- VOVZXURTCKPRDQ-CQSZACIVSA-N n-[4-[chloro(difluoro)methoxy]phenyl]-6-[(3r)-3-hydroxypyrrolidin-1-yl]-5-(1h-pyrazol-5-yl)pyridine-3-carboxamide Chemical compound C1[C@H](O)CCN1C1=NC=C(C(=O)NC=2C=CC(OC(F)(F)Cl)=CC=2)C=C1C1=CC=NN1 VOVZXURTCKPRDQ-CQSZACIVSA-N 0.000 description 1
- 239000002105 nanoparticle Substances 0.000 description 1
- PSZYNBSKGUBXEH-UHFFFAOYSA-N naphthalene-1-sulfonic acid Chemical class C1=CC=C2C(S(=O)(=O)O)=CC=CC2=C1 PSZYNBSKGUBXEH-UHFFFAOYSA-N 0.000 description 1
- 230000000269 nucleophilic effect Effects 0.000 description 1
- 229920001542 oligosaccharide Polymers 0.000 description 1
- 150000002482 oligosaccharides Chemical class 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 239000012074 organic phase Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229920000058 polyacrylate Polymers 0.000 description 1
- 239000000843 powder Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000011112 process operation Methods 0.000 description 1
- AZIQALWHRUQPHV-UHFFFAOYSA-N prop-2-eneperoxoic acid Chemical compound OOC(=O)C=C AZIQALWHRUQPHV-UHFFFAOYSA-N 0.000 description 1
- OVARTBFNCCXQKS-UHFFFAOYSA-N propan-2-one;hydrate Chemical compound O.CC(C)=O OVARTBFNCCXQKS-UHFFFAOYSA-N 0.000 description 1
- 230000004224 protection Effects 0.000 description 1
- 230000008707 rearrangement Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 238000007142 ring opening reaction Methods 0.000 description 1
- 239000011780 sodium chloride Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 235000020357 syrup Nutrition 0.000 description 1
- 239000006188 syrup Substances 0.000 description 1
- 238000012360 testing method Methods 0.000 description 1
- 230000009466 transformation Effects 0.000 description 1
- 238000010977 unit operation Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D307/00—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom
- C07D307/02—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings
- C07D307/34—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
- C07D307/38—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members with substituted hydrocarbon radicals attached to ring carbon atoms
- C07D307/40—Radicals substituted by oxygen atoms
- C07D307/46—Doubly bound oxygen atoms, or two oxygen atoms singly bound to the same carbon atom
-
- 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
- B01J31/00—Catalysts comprising hydrides, coordination complexes or organic compounds
- B01J31/02—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides
- B01J31/06—Catalysts comprising hydrides, coordination complexes or organic compounds containing organic compounds or metal hydrides containing polymers
-
- 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
- B01J37/009—Preparation by separation, e.g. by filtration, decantation, screening
-
- 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
- B01J37/04—Mixing
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07D—HETEROCYCLIC COMPOUNDS
- C07D307/00—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom
- C07D307/02—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings
- C07D307/34—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members
- C07D307/38—Heterocyclic compounds containing five-membered rings having one oxygen atom as the only ring hetero atom not condensed with other rings having two or three double bonds between ring members or between ring members and non-ring members with substituted hydrocarbon radicals attached to ring carbon atoms
- C07D307/40—Radicals substituted by oxygen atoms
- C07D307/46—Doubly bound oxygen atoms, or two oxygen atoms singly bound to the same carbon atom
- C07D307/48—Furfural
- C07D307/50—Preparation from natural products
-
- 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
- B01J2231/00—Catalytic reactions performed with catalysts classified in B01J31/00
- B01J2231/40—Substitution reactions at carbon centres, e.g. C-C or C-X, i.e. carbon-hetero atom, cross-coupling, C-H activation or ring-opening reactions
- B01J2231/42—Catalytic cross-coupling, i.e. connection of previously not connected C-atoms or C- and X-atoms without rearrangement
- B01J2231/4277—C-X Cross-coupling, e.g. nucleophilic aromatic amination, alkoxylation or analogues
- B01J2231/4288—C-X Cross-coupling, e.g. nucleophilic aromatic amination, alkoxylation or analogues using O nucleophiles, e.g. alcohols, carboxylates, esters
-
- 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
- B01J2531/00—Additional information regarding catalytic systems classified in B01J31/00
- B01J2531/001—General concepts, e.g. reviews, relating to catalyst systems and methods of making them, the concept being defined by a common material or method/theory
- B01J2531/002—Materials
- B01J2531/004—Ligands
Definitions
- the subject matter herein in general relates to a process for synthesis of furan derivative using an acid catalyst in monophasic organic solvent.
- the subject matter further relates to acid catalysts and preparation thereof.
- Furan derivatives such as 5-methyl furfural and 5-methyl furfural alcohol as well as hydroxymethyl furfural and furfural are products of saccharide dehydration with high industrial value.
- the 5-hydroxy methyl furfural (5-HMF) is a multipurpose and multi functional organic molecule having wide range of application in various sectors of synthetic organic chemistry e.g. bulk chemicals, fine chemicals, pharmaceuticals, agrochemicals, polymer, and chemical intermediates etc.
- the structure of 5-HMF is shown below:
- the process for 5-HMF synthesis is of great interest in chemical industries due to its potential for production of industrially important bio-based chemicals such as furan 2, 5-dicarboxylic acid (FDCA) which is required for production of bio-based polymer, chemicals and pharmaceuticals etc.
- Furans 2, 5-dicarboxylic acid derived polymers have potential replacements for the petro-based terephthalic acid polymer.
- the huge replacement of petro based polymer by bio-based polymer provide great platform of green chemistry in the sector of polymer industry.
- the key role for these replacement is synthesis of 5-HMF and therefore 5-HMF synthesis occupy nutshell position for synthesis of bio-based products.
- the synthetic chemistry of 5-HMF begins with hexose sugars, glucose and fructose, more specifically from fructose via acid catalyzed cyclodehydration reaction. Since the synthetic chemistry applications for 5-HMF production is directed towards the development of acid catalysis. A number of acid catalysts like mineral acids, inorganic acids, and solid acids have been employed for this purpose. But the synthetic process for production of 5-HMF by acid catalysis suffers from many technical problems in terms of yield, selectivity, process feasibility and process economics. Due to complex chemical properties between reaction substrate, catalyst used for dehydration and reaction products separation, number of issues are raised during synthesis of 5-HMF.
- Yugen zhang report ( ChemSusChem, 2011, 12, 1745-1748) disclosed the synthesis of 5-HMF in isopropyl alcohol with aqueous HCl as a catalyst.
- halogenated corrosive HCl as a catalyst in aqueous condition resulted in product separation problem as well as recovery of catalyst with difficulty in handling during large scale production.
- US2007757461 discloses use of mineral acid, zeolites, silica-, silica-alumina, and titania-based supports functionalized by acid groups, cation exchange resin, Lewis acid, heteropolyacid, in biphasic reactor, having aqueous and organic phase of 1-butanol, DCM, MIBK, 2-butanol, and mixtures thereof.
- the invention also employs modifier such as DMSO, DMF, N-methyl pyrrolidinone (NMP), which are difficult to separate and non eco-friendly.
- aqueous biphasic solvents and ionic liquids are used for the synthesis of 5-HMF in presence of acid catalyst.
- procedures become complicated and require large amounts of organic solvents for extraction. This leads to substantial increase in the process cost and unit operation for the bulk production of 5-HMF. This necessitates the optimization of solvent and catalytic systems that would be cost effective as well as provide ease of process operation.
- WO2011124639 recites claims to the use of mineral and Lewis acid catalyst such as aqueous HCl, AlCl 3 respectively by using salt, NaCl, LiCl, LiBr, LiNO 3 , KCl, KBr, KNO 3 , FeCl 3 , etc. in biphasic organic solvent, wherein the biphasic organic solvent consisted of mixture of water and methyl isobutyl ketone (MIBK).
- MIBK methyl isobutyl ketone
- the disclosed process of the invention resulted in low yield (52%) and selectivity (less than 65%).
- the process also employs halogenated catalyst and salts which cause corrosion problems as well as environmental hazards.
- Microwave assisted reaction for synthesis of 5-HMF has gained significance as it leads to reduction in reaction time, increases selectivity and also results in reduction of energy consumptions.
- Thomas S. Hansen and co-workers ( Carbohydrate Research, 2009, 344, 2568-2572) reported microwave assisted synthesis of 5-HMF by using Aq. HCl catalyst at 200° C. temp with only 52% HMF yield.
- Xinhua Qi, and co-workers Ind. Eng. Chem. Res. 2008, 47, 9234-9239
- HMF synthesis by employing strong acidic cation-exchange resin catalyst and a mixed organic solvent system comprising acetone and DMSO in ratio of 70:30 w/w under microwave heating condition. The reaction resulted in 80% yield with a reaction time period of 10-30 min.
- WO2012/015616 A1 claims for microwave assisted synthesis of 5-HMF by using catalyst amberlyst and H 2 SO 4 in 5-30 min reaction time with 0-69.47% yield by using DMSO solvent. These methods of the microwave assisted synthesis for 5-HMF also reflect earlier predicaments of lower yield, selectivity, use of non-green solvent systems and higher cost economics that affect scaling up of the processes adversely.
- WO2014180979 discloses a process for the synthesis of 5-hydroxymethyl furfural (HMF) from saccharides. In particular it discloses a process for the dehydration of monosaccharides having 6 carbon atoms (hexoses), disaccharides, oligosaccharides and polysaccharides deriving therefrom to yield highly pure 5-hydroxymethyl furfural (HMF) in high yield.
- HMF 5-hydroxymethyl furfural
- the present disclosure relates to a process for preparing a furan derivative, the process comprising the steps of: a) contacting a sugar with a monophasic organic solvent to obtain a reaction mixture; and b) subjecting the reaction mixture to a temperature in the range from 100° C. to 180° C., in presence of an acid catalyst, for a time period in the range of 0.5 min to 4.0 h to obtain at least 70% conversion of the sugar to a single furan derivative, wherein the acid catalyst is selected from the group consisting of homogenous acid catalyst, heterogeneous solid acid catalyst, and combinations thereof.
- the present disclosure also relates to a process for preparing a heterogeneous solid acid catalyst, the process comprising the steps of: contacting a sulfonating agent with a polymer in presence of an organic solvent to obtain a reaction suspension; agitating the reaction suspension at a temperature in the range of 35° C. to 100° C. for a time period in the range of 30 min to 4 hrs to obtain a suspension of heterogeneous acid catalyst; and isolating the suspension of heterogeneous acid catalyst to obtain a heterogeneous solid acid catalyst.
- DIC A T refers to the solid acid catalyst disclosed in the present invention and developed at DBT-ICT Centre for Energy Biosciences, Institute of Chemical Technology.
- Various solid acid catalysts prepared by using different polymeric support and disclosed in the present invention, and further disclosed in the present invention are:
- saccharides used herein refers to sugars having composition according to formula (CH 2 O)n consisting of monosaccharide, disaccharides and/or polysaccharides.
- formula (CH 2 O)n consisting of monosaccharide, disaccharides and/or polysaccharides.
- sacchars has been interchangeably used in this disclosure with the word “saccharides”.
- Ratios, concentrations, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited.
- a temperature range of about 70° C. to about 180° C. should be interpreted to include not only the explicitly recited limits of about 70° C. to about 180° C., but also to include sub-ranges, such as 90° C. to 110° C., 120° C. to 160° C., and so forth, as well as individual amounts, including fractional amounts, within the specified ranges, such as 82° C., 121.6° C., and 168.3° C., for example.
- the present disclosure is directed to a process for synthesis of a furan derivative, more particularly 5-hydroxy methyl furfural (5-HMF), from sugars with a short time microwave assisted or conventional heating reaction, by using homogeneous or heterogeneous-solid acid catalyst.
- the use of the acid catalyst in monophasic organic solvent system for the synthesis of 5-HMF provides excellent catalytic activity, selectivity, conversion, rate of production and yield of product.
- DIC A T a heterogeneous-solid acid catalyst
- the use of a heterogeneous-solid acid catalyst, DIC A T, in the present invention provides the convenience of a simple process for separating the catalyst from the reaction mixture.
- the reaction products and catalyst are easily separated from reaction mixture by conventional methods such as simple solvent distillation and filtration procedures.
- the process for preparing a furan derivative as disclosed herein comprises the steps of a) contacting a sugar with a monophasic organic solvent to obtain a reaction mixture; and b) subjecting the reaction mixture to a temperature in the range from 100° C. to 180° C., in presence of an acid catalyst, for a time period in the range of 0.5 min to 4.0 h to obtain at least 70% conversion of the sugar to a single furan derivative, wherein the acid catalyst is selected from the group consisting of homogenous acid catalyst, heterogeneous solid acid catalyst, and combinations thereof.
- the present disclosure further relates to a process for preparing a heterogeneous solid acid catalyst, the process comprising the steps of: a) contacting a sulfonating agent with a polymer in presence of an organic solvent to obtain a reaction suspension; b) agitating the reaction suspension at a temperature in the range of 35° C. to 100° C. for a time period in the range of 30 min to 4 hrs to obtain a suspension of heterogeneous acid catalyst; and c) isolating the suspension of heterogeneous acid catalyst to obtain a heterogeneous solid acid catalyst.
- the furan derivative prepared by the disclosed process is 5-hydroxy methyl furfural (5-HMF).
- Saccharides are used as substrates for synthesis of furan derivatives.
- saccharide sources used for the disclosed process include, but are not limited to hexose and pentose sugars, polysaccharides comprising at least one hexose, corn syrup, high fructose corn syrup, cane sugar molasses, fructose, fructose syrup, crystalline fructose, crude fructose; purified fructose, high fructose concentration, fructose syrup or combinations thereof.
- the substrate is a hexose sugar.
- the sugar is selected from the group consisting of glucose, fructose, sucrose, and combinations thereof.
- the sugar is fructose.
- the form of fructose is anhydrous.
- the sugar is in amorphous form.
- the sugar is in crystalline form.
- the solvent as used in the process disclosed herein is a monophasic organic solvent.
- the solvent is selected from the group consisting of alcohols with the formula R—OH, N, N-Dimethyl formamide, Dimethyl sulfoxide, esters, and 1, 4-dioxane.
- the solvent is an alcohol with the formula R—OH, wherein R ranges from C 1 to C 15 , more preferably C 1 to C 4 .
- the C 1 to C 4 alcohol is selected from the group consisting of methanol, ethanol, n-propanol, iso-propanol, sec-butanol, tert-butanol, and combinations thereof.
- the C 1 to C 4 alcohol is isopropanol.
- the monophasic organic solvent has a boiling point less than 100° C.
- the reaction mixture for preparing a furan derivative comprises a sugar and a low boiling point organic solvent.
- concentration of sugar in the reaction mixture is in the range of 1-50% (w/v), preferably 1-10% (w/v).
- water content in the reaction mixture is in the range of 0 to 20%, preferably 0 to 6% w/w.
- the reaction is carried out at a temperature in the range of 100-180° C. In one implementation, contacting the reaction mixture with microwave radiation to bring it to a temperature in the range of 100° C. to 180° C. for a desired time is sufficient to convert at least 70% of the reactant into the desired product. In another implementation, contacting the reaction mixture with microwave radiation to bring it to a temperature in the range of 100° C. to 180° C. for a desired time is sufficient to convert at least 90% of the reactant into the desired product.
- the reaction is carried out at a temperature in the range of 100-180° C.
- contacting the reaction mixture with a conventional heater bringing it to a temperature in the range of 100° C. to 180° C. for a desired time is sufficient to convert at least 70% of the reactant into the desired product.
- contacting the reaction mixture a conventional heater bringing it to a temperature in the range of 100° C. to 180° C. for a desired time is sufficient to convert at least 90% of the reactant into the desired product.
- process for synthesis of 5-HMF is carried out in a microwave reactor, wherein the temperature is in the range of 100-180° C. In another implementation, the preferred temperature is in the range of 110-150° C. under microwave heating condition. In one implementation, the process provides the use of microwave reactor with frequency of 2.45 GHz, and power ranging between 10-400 watts. In one implementation, the reaction mixture is stirred at the rotational speed ranging between 200-800 rpm. In another implementation, the reaction mixture is stirred at the rotational speed ranging between 400-650 rpm. In one implementation, the reaction is carried under microwave heating conditions for 30-300 seconds. In another implementation, the reaction is carried under microwave heating conditions for 30-120 seconds.
- the process for synthesis of 5-HMF is carried out by means of conventional heating under pressure in the range of 5-50 bar. In another implementation, conventional heating is done under pressure in the range of 5-30 bar. In one implementation, the reaction mixture is heated to a temperature in the range of 100-180° C. In another implementation, the reaction mixture is heated to a temperature in the range of 100-150° C. The temperature was maintained by proportional-integral-derivative (PID) heating temperature controller. In one implementation, reaction time under conventional heating is in the range of 0.5-5 hrs. In one implementation, reaction time under conventional heating is in the range of 0.5-4 hrs. In one implementation, reaction time under conventional heating is in the range of 0.5-3 hrs. In one implementation, the agitation of reaction mixture is carried out by four pitch bladed impeller at a rotational speed in the range of 100-800 rpm.
- PID proportional-integral-derivative
- conversion of the sugar by the process disclosed herein is in the range of 45-100%. In another implementation, conversion of the sugar by the process disclosed herein is in the range of 95-100%.
- the yield of furan derivative by the process disclosed herein is in the range of 10-95%. In another implementation, the yield of furan derivative by the process disclosed herein is in the range of 80-95%.
- the process is carried in a batch mode reactor. In one implementation, the process is carried out in a continuous reactor. In one implementation, the process is carried out in the fixed bed reactor.
- the process for preparation of a furan derivative from a sugar is carried out in presence of an acid catalyst.
- the acid catalyst is used in an amount in the range of 0.01 to 5 g/cc of the reaction mixture. In another implementation, the acid catalyst is used in an amount in the range of 0.1 to 1.0 g/cc of the reaction mixture.
- the reaction mixture is cooled and the catalyst is separated by filtration and reused for next reaction.
- recycling of catalyst is performed up to 20 times without addition of fresh catalyst and without regeneration. In another implementation, recycling of catalyst is performed more than 20 times without addition of fresh catalyst and without regeneration. In another implementation, recycling of catalyst is performed up to 5 times without addition of fresh catalyst and without regeneration.
- the acid catalyst is a homogenous acid catalyst.
- the homogenous acid catalyst is an aliphatic sulfonic acid.
- the homogenous acid catalyst is an aromatic sulfonic acid.
- the aromatic sulfonic acid is selected from the group consisting of naphthalene sulfonic acids, dimethyl aniline sulfonic acid, para-toluene sulfonic acid (p-TSA), ortho/meta-toluene sulfonic acid (o/m-TSA), and combinations thereof.
- the aromatic sulfonic acid is para-toluene sulfonic acid (p-TSA).
- the acid catalyst is a heterogenous solid acid catalyst.
- the heterogenous solid acid catalyst is a hydrophilic sulfonated solid porous matrix.
- the heterogenous solid acid catalyst is DIC A T acid catalyst.
- a process for preparing a heterogenous solid acid catalyst comprises the steps of: a) contacting a sulfonating agent with a polymer in presence of an organic solvent to obtain a reaction suspension; b) agitating the reaction suspension at a temperature in the range of 35° C. to 100° C. for a time period in the range of 30 min to 4 hrs to obtain a suspension of heterogeneous acid catalyst; and c) isolating the suspension of heterogeneous acid catalyst to obtain a heterogeneous solid acid catalyst.
- the sulfonating agent is selected from the group consisting of chlorosulfonic acid, sulphuric acid, sulfur trioxide, and combinations thereof. In one implementation, the sulfonating agent is chlorosulfonic acid.
- the heterogenous solid acid catalyst is composed of a hydrophilic functionalized polymer.
- the functionalized polymer has a surface area in the range of 5-200 m 2 /g.
- the functionalized polymer has a surface area in the range of 5-50 m 2 /g, pore size in the range of 2-50 nm, acidity in the range of 0.5-10 mmol/g, pore volume in the range of 0.022-2.0 cc/g.
- the molecular weight of the polymer is in the range of 3-23 kDa, particle size is in the range of 10-300 ⁇ m, and hydroxy value is in the range of 1 to 20 mg/g.
- the polymer is a homolinear polymer. In one implementation, the polymer is a crosslinked polymer. In one implementation, the polymer used is in crystalline form. In one implementation, the polymer used is in amorphous form. In one implementation, the polymer is in the form of spherical beads.
- the polymer comprises hydroxy functional group. In one implementation, the polymer comprises amine functional group. In one implementation, the polymer is selected from the group consisting of cellulose, polyvinyl alcohol, polyhydroxyethylmethacrylate, polyhydroxymethylmethacrylate polyethylene glycol, polypropylene glycol, silica, alumina, polyethylene amine, polyamide, and polyallylamine. In another implementation, the polymer is selected from the group consisting of cellulose, polyvinyl alcohol, polyhydroxyethylmcthacrylate, and polyhydroxymethylmcthacrylate.
- sulfonic acid derivatization of polymeric surfaces to obtain a heterogenous solid acid catalyst is done in presence of an organic solvent.
- the organic solvent is a non nucleophilic solvent.
- the organic solvent is selected from the group consisting of methylene dichloride, chloroform, carbon-tetrachloride, ethylene dichloride, propylene dichloride, and combinations thereof.
- the heterogonous solid acid catalyst as prepared by the process disclosed herein can also be used for various acid catalyzed organic transformation such as hydrolysis, elimination, addition, substitution, condensation, esterification, protection, deprotection, rearrangement, and ring opening.
- a process for preparing 5-HMF comprising the steps of: a) contacting fructose with isopropanol to obtain a reaction mixture; and b) subjecting the reaction mixture to a temperature of 120° C., in presence of an acid catalyst, for a time period of 2.0 min to obtain at least 70% conversion of fructose to 5-HMF, wherein the acid catalyst is PTSA.
- a process for preparing 5-HMF comprising the steps of: a) contacting fructose with isopropanol to obtain a reaction mixture; and b) subjecting the reaction mixture to a temperature of 130° C., in presence of an acid catalyst, for a time period in the range of 2.0 min to obtain at least 70% conversion of fructose to 5-HMF, wherein the acid catalyst is DIC A T.
- the experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz.
- 1 gm of crystalline fructose was added to 8 ml isopropyl alcohol in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature to obtain a reaction suspension.
- 0.1 gm/cc of acid catalyst (as provided in Table 1) was added to this reaction suspension under continuous stirring.
- the resulting reaction mixture was heated to 120° C. under stirring for 120 seconds by subjecting to microwave radiation. After 120 seconds, the reaction mass was cooled to room temperature.
- the HPLC analysis of the sample was obtained which demonstrates 84-94% molar yield of HMF with 97-98% of fructose conversion.
- the solvent was removed by the vacuum distillation to get dark brown viscous oil of crude HMF.
- the Table 1 given below provides the HMF yields and fructose conversions with different acid catalyst using the process described above.
- the experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz.
- 1 gm of crystalline fructose was added to 8 ml solvent (as provided in Table 2) in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature to obtain a reaction suspension.
- 0.1 gm/cc of acid catalyst (PTSA) was added to this reaction suspension under continuous stirring.
- the resulting reaction mass was heated under stirring for 120 seconds by subjecting to microwave radiation. After 120 seconds, the reaction mixture was cooled to room temperature.
- the HPLC analysis of the sample was obtained which demonstrates 76-88% molar yield of HMF with 80-99% of fructose conversion.
- the solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- the experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz.
- 1 gm of crystalline fructose was added to 8 ml isopropyl alcohol in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature.
- desired amount of PTSA (as provided in Table 3) was charged under stirring.
- the resulting reaction mass was heated for 90 seconds by subjecting to microwave radiation. After 90 seconds, reaction mass was cooled at room temperature.
- the HPLC analysis of the sample was obtained which demonstrates 74-88% molar yield of HMF with 94-98% of fructose conversion.
- the solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- the experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz.
- 1 gm of crystalline fructose was added to 8 ml isopropyl alcohol in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature.
- 0.10 gm/cc of PTSA was charged under stirring.
- the resulting reaction mass was heated to 120° C. by subjecting to microwave radiation for desired time period (as provided in Table 4). Thereafter the reaction mass was cooled to room temperature.
- the HPLC analysis of the sample was obtained which demonstrates the 32-91% molar yield of HMF and 50-100% of fructose conversion.
- the solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- the Table 4 given below provides the HMF yields and fructose conversions with varying reaction time by using process described above.
- the experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz.
- 1 gm of crystalline fructose was added to 8 ml of solvent (as provided in Table 5) in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature.
- desired amount of acid catalyst (DIC A T-1) was added under stirring.
- the resulting reaction mixture was heated for 120 seconds by subjecting to microwave radiation under stirring. After 120 seconds, the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration.
- the sample obtained demonstrated 50-94% molar yield of HMF with 80-99% of fructose conversion through HPLC analysis.
- the solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- the Table 5 given below provides the HMF yields and fructose conversions with varying reaction solvent by using process described above.
- the experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz.
- 1 gm of crystalline fructose was added to 8 ml of solvent (as provided in Table 6) in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature.
- desired amount of acid catalyst (DIC A T-3) was added under stirring.
- the resulting reaction mixture was heated for 120 seconds by subjecting to microwave radiation under stirring. After 120 seconds, the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration.
- the sample obtained demonstrated 50-94% molar yield of HMF with 80-99% of fructose conversion through HPLC analysis.
- the solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- the experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz.
- 1 gm of crystalline fructose was added to 8 ml of solvent (as provided in Table 6) in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature.
- desired amount of acid catalyst (DIC A T-3) was charged (as provided in Table 6).
- the resulting reaction mass was heated for 120 seconds by subjecting to microwave radiation under stirring. After 120 seconds, the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration. HPLC analysis of the sample demonstrated 61-93% molar yield of HMF with 97-100% fructose conversion. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- the Table 7 given below provides the HMF yields and fructose conversions with varying catalyst DIC A T-3 concentration by using process described above.
- the experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz.
- 1 gm of crystalline fructose was added to 8 ml of isopropyl alcohol in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature.
- 0.11 gm/cc of acid catalyst (DIC A T-3) was charged under stirring.
- the resulting reaction mass was heated under continuous stirring to 130° C. by subjecting to microwave radiation for desired time period (as provided in Table 8). After completion of the reaction, the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration.
- the sample obtained demonstrated 50-92% molar yield of HMF with 98-100% fructose conversion through HPLC analysis. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- the experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz.
- 1 gm of crystalline fructose was added to 8 ml of isopropyl alcohol in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature.
- 0.11 gm/cc of acid catalyst (DIC A T-3) was charged under stirring.
- the resulting reaction mass was heated under continuous stirring to desired temperature (as provided in Table 9) by subjecting to microwave radiation for 120 seconds.
- desired temperature as provided in Table 9
- the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration.
- the sample obtained demonstrated 21-93% molar yield of HMF with 73-100% of fructose conversion through HPLC analysis.
- the solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- the Table 9 given below provides the HMF yields and fructose conversions with varying reaction temperature by using process described above.
- the experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz.
- a desired amount of crystalline fructose (as shown in Table 10) was added to a requisite amount of the solvent in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature.
- 0.11 gm/cc of acid catalyst (DIC A T-3) was charged under stirring.
- the resulting reaction mass was heated under continuous stirring to a temperature of 130° C. by subjecting to microwave radiation for 120 seconds.
- the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration.
- the sample obtained demonstrated 26-92% molar yield HMF of with 99-100% fructose conversion through HPLC analysis.
- the solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- the Table 10 given below provides the HMF yields and fructose conversions with varying fructose concentration by using process described above.
- the experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz.
- 1 gm of desired substrate (as shown in Table 11) was added to a requisite amount of the solvent (16 ml) in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature.
- 0.11 gm/cc of acid catalyst (DIC A T-3) was charged under stirring.
- the resulting reaction mass was heated under continuous stirring to a temperature of 130° C. by subjecting to microwave radiation for 120 seconds. After completion of the reaction the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration.
- the sample obtained demonstrated 48-93% molar yield of HMF with 99-100% of fructose conversion through HPLC analysis.
- the solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- the Table 11 given below provides the HMF yields and fructose conversions with varying substrate by using process described above.
- the experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz.
- 1 gm of fructose was added to a requisite amount of the solvent (16 ml) in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature.
- 0.11 gm/cc of acid catalyst (DIC A T-1) was charged under stirring.
- the resulting reaction mass was heated under continuous stirring to a temperature of 130° C. by subjecting to microwave radiation for 120 seconds.
- the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration and the catalyst was recycled for subsequent runs (as provided in Table 12).
- the obtained filtrate sample was analyzed for HPLC which demonstrates 94-95% molar yield of HMF with 98-99% of fructose conversion.
- the solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- the Table 12 given below provides the HMF yields and fructose conversions with number of catalyst recycle by using process described above.
- the experiments was carried out in batch mode operation under conventional heating in a 300 ml Parr pressure reactor autoclave assembly having four peach bladed ampler and PID temperature controller with accuracy ⁇ 1° C.
- the autoclave was loaded with 2 gm of crystalline fructose in desired amount of solvent (32 ml) and a desired acid catalyst DIC A T (as provided in Table 13).
- the reaction mass in the autoclave was stirred for 5 minute at room temperature followed by nitrogen purging 2-3 times.
- the autoclave was pressurized to 15 kg/cm 3 using nitrogen and reaction mass was heated for 120 min under constant stirring. After 120 min of reaction, the reaction mass was cooled to room temperature and finally the nitrogen pressure was released. Heterogeneous catalyst in the reaction mass was removed by vacuum filtration.
- the sample from this filtrate was analyzed for HPLC and demonstrated 68-90% molar yield of HMF, with 96-98% fructose conversion.
- the solvent was removed by the vacuum distillation to obtain a dark brown viscous
- the Table 13 given below provides the HMF yields and fructose conversions with varying acid catalyst by using process described above.
- the Table 14 given below provides the HMF yields and fructose conversions with varying pressure by using process described above.
- the Table 15 given below provides the HMF yields and fructose conversions with varying time period by using process described above.
- DIC A T The heterogeneous solid acid catalyst DIC A T was prepared by sulfonic acid anchoring on aliphatic hydroxy groups of hydrophilic polymer through organic linkage.
- the typical experimental process for preparation of DIC A T is as follows:
- reaction was carried out in a four necked 250 ml dry round bottomed flask with heating oil bath, reflux condenser, thermometer pocket, addition funnel and over head stirrer.
- 1 gm of hydroxy polymer, (polyvinyl alcohol) was added under nitrogen blanketing.
- 10 ml of ethylene dichloride was charged in flask under slow stirring.
- the 9.5 ml of sulfonating agent, (chlorosulfonic acid) was added drop wise for 30 min through addition funnel under vigorous stirring. After the completion of addition reaction, reaction mass was stirred vigorously for 20-30 min at room temperature and then heated to reflux for 1 hr.
- reaction mass was allowed to cool at room temperature and subsequently to 0° C.; thereafter 10 ml of aqueous methanol was added slowly through addition funnel within 30 min and maintained at 0° C. under vigorous stirring for another 30 min.
- the resulting black solid was then filtered by suction pump and washed by cold water till removal of chlorine from filtrate which was tested by AgNO 3 precipitation test. Finally the solid cake was suck dried by suction pump and kept for drying at 70-80° C. under vacuum. Resulting black color dry powder of DIC A T obtained was used for reaction.
- the synthesis of HMF in packed bed reactor was performed in steel column of 2 ⁇ 20 cm height with heating jacket having inlet outlet temperature sensor and pressure control valve.
- the 5 cm catalyst bed was packed with sufficient amount of inert material.
- the column was pre equilibrated by passing 2-5 column volume (CV) of fresh water and IPA to obtain column temperature of 120° C. and 10-15 kg/cm 3 pressure.
- the pre heated 100 ml 6.25% solution of fructose in IPA was passed through catalyst bed maintained at 120° C. by conventional heating with desire flow rate in cyclic loop by means of binary piston pressure pump. Simultaneously, the samples from reaction mixture were removed at different time intervals for in process HPLC analysis.
- the synthesis of HMF in packed bed reactor was performed in steel column of 2 ⁇ 20 cm height with heating jacket having inlet outlet temperature sensor and pressure control valve.
- the 5 cm catalyst bed was packed with sufficient amount of inert material.
- the column was pre equilibrated by passing 2-5 column volume (CV) of fresh water and IPA to obtain column temperature of 120° C. and 10-15 kg/cm 3 pressure.
- the pre heated 100 ml 6.25% solution of fructose in IPA was passed through catalyst bed maintained at 120° C. by microwave heating with desired flow rate in cyclic loop by means of binary piston pressure pump. Simultaneously, the samples from reaction mixture were removed at different time intervals for in process HPLC analysis.
- the present disclosure relates to a process of preparing 5-hydroxymethyl furfural (5-HMF) from saccharides utilizing an acid catalyst.
- the acid catalyzed cyclodehydration process for synthesis of 5-HMF provides a simple and cost effective route for the production of 5-HMF in monophasic organic solvent.
- the heterogenous solid acid catalyst, DIC A T used in the process disclosed herein has excellent catalytic activity, stability, and selectivity towards desired product. Due to higher selectivity of catalyst, formation of side products such as polymers, humins, levulinic acid, and condensation products is significantly reduced.
- the overall process employs use of monophasic organic solvents (low boiling, or high boiling) which are easy to separate with minimum energy utilization for solvent distillation. The process is carried out in significantly decreased reaction time through conventional or microwave assisted heating resulting in increased productivity.
- The comprises microwave assisted short time reaction that is carried out in a monophasic organic solvent at temperature ranges of 100-180° C., thus providing process feasibility at an economical cost and with low energy consumption.
- the short reaction time of 30-120 seconds enhance the bulk production and economics of 5-HMF production in the given time period.
- the present process for synthesis of 5-HMF synthesis involves lower energy utilization with production of minimum waste and effluents.
- the disclosed process is therefore a green and efficient process which results in higher selectivity and yield; has a higher conversion rate with enhanced catalytic stability, has ease of separation and most importantly has the advantage of recycling the catalyst with 100% recovery.
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Abstract
Description
- The subject matter herein in general relates to a process for synthesis of furan derivative using an acid catalyst in monophasic organic solvent. The subject matter further relates to acid catalysts and preparation thereof.
- Furan derivatives such as 5-methyl furfural and 5-methyl furfural alcohol as well as hydroxymethyl furfural and furfural are products of saccharide dehydration with high industrial value. The 5-hydroxy methyl furfural (5-HMF) is a multipurpose and multi functional organic molecule having wide range of application in various sectors of synthetic organic chemistry e.g. bulk chemicals, fine chemicals, pharmaceuticals, agrochemicals, polymer, and chemical intermediates etc. The structure of 5-HMF is shown below:
- The process for 5-HMF synthesis is of great interest in chemical industries due to its potential for production of industrially important bio-based chemicals such as furan 2, 5-dicarboxylic acid (FDCA) which is required for production of bio-based polymer, chemicals and pharmaceuticals etc. Furans 2, 5-dicarboxylic acid derived polymers have potential replacements for the petro-based terephthalic acid polymer. Thus, the huge replacement of petro based polymer by bio-based polymer provide great platform of green chemistry in the sector of polymer industry. But the key role for these replacement is synthesis of 5-HMF and therefore 5-HMF synthesis occupy nutshell position for synthesis of bio-based products.
- The synthetic chemistry of 5-HMF begins with hexose sugars, glucose and fructose, more specifically from fructose via acid catalyzed cyclodehydration reaction. Since the synthetic chemistry applications for 5-HMF production is directed towards the development of acid catalysis. A number of acid catalysts like mineral acids, inorganic acids, and solid acids have been employed for this purpose. But the synthetic process for production of 5-HMF by acid catalysis suffers from many technical problems in terms of yield, selectivity, process feasibility and process economics. Due to complex chemical properties between reaction substrate, catalyst used for dehydration and reaction products separation, number of issues are raised during synthesis of 5-HMF.
- Another important factor that affects 5-HMF synthesis is the type of catalyst used for dehydration reaction. Various types of organic, inorganic and mineral acids have been employed as in situ catalysts for 5-HMF synthesis. But most of these processes suffer from handling problems due to corrosive nature of mineral acids as well as difficult catalyst separation protocols from reaction mixture with subsequent recycling of the catalyst.
- Therefore heterogeneous acid catalysis as well as various solid acid catalysts such as zeolites, silica, and amberlyst resins have been explored and investigated as a possible alternative. Ken-ichi Shimizu and co-workers reported use of heteropoly acid, zeolites, and acidic resin (Catalysis Communications, 2009, 10, 1849-1853) with DMSO as solvent. Though the use of heterogeneous catalysis resulted in higher yield, high boiling point of solvent rendered separation of the product difficult.
- Yugen zhang report (ChemSusChem, 2011, 12, 1745-1748) disclosed the synthesis of 5-HMF in isopropyl alcohol with aqueous HCl as a catalyst. However, the use of halogenated corrosive HCl as a catalyst in aqueous condition resulted in product separation problem as well as recovery of catalyst with difficulty in handling during large scale production.
- US2007757461 discloses use of mineral acid, zeolites, silica-, silica-alumina, and titania-based supports functionalized by acid groups, cation exchange resin, Lewis acid, heteropolyacid, in biphasic reactor, having aqueous and organic phase of 1-butanol, DCM, MIBK, 2-butanol, and mixtures thereof. However, the invention also employs modifier such as DMSO, DMF, N-methyl pyrrolidinone (NMP), which are difficult to separate and non eco-friendly.
- Similarly patent documents WO2009/076627, US2009/0156841, U.S. Pat. No. 7,579,489, EP2233476, and Lye et. al (ChemSusChem, 2012, 5, 1737-1742) disclose the use of a heterogeneous catalyst, amberlyst-35 resin, in high boiling solvents like DMF, N-methylpyrrolidinone (NMP) with yield figure less than 80%. The solvents used are non green and require high energy to separate them from reaction mass.
- Typically aqueous biphasic solvents and ionic liquids are used for the synthesis of 5-HMF in presence of acid catalyst. However, due to higher solubility of 5-HMF in water, procedures become complicated and require large amounts of organic solvents for extraction. This leads to substantial increase in the process cost and unit operation for the bulk production of 5-HMF. This necessitates the optimization of solvent and catalytic systems that would be cost effective as well as provide ease of process operation.
- WO2011124639 recites claims to the use of mineral and Lewis acid catalyst such as aqueous HCl, AlCl3 respectively by using salt, NaCl, LiCl, LiBr, LiNO3, KCl, KBr, KNO3, FeCl3, etc. in biphasic organic solvent, wherein the biphasic organic solvent consisted of mixture of water and methyl isobutyl ketone (MIBK). However, the disclosed process of the invention resulted in low yield (52%) and selectivity (less than 65%). The process also employs halogenated catalyst and salts which cause corrosion problems as well as environmental hazards.
- Microwave assisted reaction for synthesis of 5-HMF has gained significance as it leads to reduction in reaction time, increases selectivity and also results in reduction of energy consumptions. Thomas S. Hansen and co-workers (Carbohydrate Research, 2009, 344, 2568-2572) reported microwave assisted synthesis of 5-HMF by using Aq. HCl catalyst at 200° C. temp with only 52% HMF yield. Xinhua Qi, and co-workers (Ind. Eng. Chem. Res. 2008, 47, 9234-9239) reported HMF synthesis by employing strong acidic cation-exchange resin catalyst and a mixed organic solvent system comprising acetone and DMSO in ratio of 70:30 w/w under microwave heating condition. The reaction resulted in 80% yield with a reaction time period of 10-30 min.
- Sudipta De and co-workers (Green Chem., 2011, 13, 2859) report microwave assisted synthesis of 5-HMF by using Lewis acid catalyst AlCl3 with 21.4-60.6% yields in solvent DMSO and biphasic system, water—MIBK. Xinhua Qi and co-workers (Green Chem., 2008, 10, 799-805) employed microwave assisted heating for HMF synthesis in acetone-water mixtures in the presence of a cation exchange resin catalyst with yields of 5-HMF as high as 73.4%, with 94% conversion rate at 150° C. Sakita Dutta and co-workers (Applied Catalysis A vol. 409-410, 133-139), carried out microwave assisted 5-HMF synthesis by using mesoporous TiO2 nanoparticles in solvents DMSO and NMP.
- WO2012/015616 A1 claims for microwave assisted synthesis of 5-HMF by using catalyst amberlyst and H2SO4 in 5-30 min reaction time with 0-69.47% yield by using DMSO solvent. These methods of the microwave assisted synthesis for 5-HMF also reflect earlier predicaments of lower yield, selectivity, use of non-green solvent systems and higher cost economics that affect scaling up of the processes adversely.
- WO2014180979 discloses a process for the synthesis of 5-hydroxymethyl furfural (HMF) from saccharides. In particular it discloses a process for the dehydration of monosaccharides having 6 carbon atoms (hexoses), disaccharides, oligosaccharides and polysaccharides deriving therefrom to yield highly pure 5-hydroxymethyl furfural (HMF) in high yield.
- The methods of prior art disclose the use of various catalyst and solvent systems for synthesis of 5-HMF through microwave assisted as well as conventional means. Evidently, these methods are associated with issues pertaining to higher cost economics, reaction feasibility, longer reaction time, catalysts and product separation, low catalyst activity, low selectivity & yield, and use of non-green solvents that pose environmental hazards.
- Accordingly, there has been a need in the prior art for a process for synthesis of 5-HMF, wherein the process results in higher selectivity and yield; has a higher conversion rate with enhanced catalytic stability, has ease of product separation and most importantly has the advantage of recycling the catalyst with 100% recovery.
- The present disclosure relates to a process for preparing a furan derivative, the process comprising the steps of: a) contacting a sugar with a monophasic organic solvent to obtain a reaction mixture; and b) subjecting the reaction mixture to a temperature in the range from 100° C. to 180° C., in presence of an acid catalyst, for a time period in the range of 0.5 min to 4.0 h to obtain at least 70% conversion of the sugar to a single furan derivative, wherein the acid catalyst is selected from the group consisting of homogenous acid catalyst, heterogeneous solid acid catalyst, and combinations thereof.
- The present disclosure also relates to a process for preparing a heterogeneous solid acid catalyst, the process comprising the steps of: contacting a sulfonating agent with a polymer in presence of an organic solvent to obtain a reaction suspension; agitating the reaction suspension at a temperature in the range of 35° C. to 100° C. for a time period in the range of 30 min to 4 hrs to obtain a suspension of heterogeneous acid catalyst; and isolating the suspension of heterogeneous acid catalyst to obtain a heterogeneous solid acid catalyst.
- These and other features, aspects, and advantages of the present subject matter will be better understood with reference to the following description and appended claims. This summary is provided to introduce a selection of concepts in a simplified form. This summary is not intended to identify key features or essential features of the claimed subject matter, nor is it intended to be used to limit the scope of the claimed subject matter.
- Those skilled in the art will be aware that the present disclosure is subject to variations and modifications other than those specifically described. It is to be understood that the present disclosure includes all such variations and modifications. The disclosure also includes all such steps, features, compositions and compounds referred to or indicated in this specification, individually or collectively, and any and all combinations of any or more of such steps or features.
- For convenience, before further description of the present disclosure, certain terms employed in the specification, and examples are collected here. These definitions should be read in the light of the remainder of the disclosure and understood as by a person of skill in the art. The terms used herein have the meanings recognized and known to those of skill in the art, however, for convenience and completeness, particular terms and their meanings are set forth below.
- The articles “a”, “an” and “the” are used to refer to one or to more than one (i.e., to at least one) of the grammatical object of the article.
- The terms “comprise” and “comprising” are used in the inclusive, open sense, meaning that additional elements may be included. Throughout this specification, unless the context requires otherwise the word “comprise”, and variations, such as “comprises” and “comprising”, will be understood to imply the inclusion of a stated element or step or group of element or steps but not the exclusion of any other element or step or group of element or steps.
- The term “including” is used to mean “including but not limited to”. “Including” and “including but not limited to” are used interchangeably.
- The term “DICAT” used herein refers to the solid acid catalyst disclosed in the present invention and developed at DBT-ICT Centre for Energy Biosciences, Institute of Chemical Technology. Various solid acid catalysts prepared by using different polymeric support and disclosed in the present invention, and further disclosed in the present invention are:
- DICAT-1:—DBT-ICT-CEB Catalyst prepared by using polyvinyl alcohol
DICAT-2:—DBT-ICT-CEB Catalyst prepared by using cellulose
DICAT-3:—DBT-ICT-CEB Catalyst prepared by using hydroxy acrylate polymer - The term “saccharides” used herein refers to sugars having composition according to formula (CH2O)n consisting of monosaccharide, disaccharides and/or polysaccharides. The word “sugars” has been interchangeably used in this disclosure with the word “saccharides”.
- Ratios, concentrations, amounts, and other numerical data may be presented herein in a range format. It is to be understood that such range format is used merely for convenience and brevity and should be interpreted flexibly to include not only the numerical values explicitly recited as the limits of the range, but also to include all the individual numerical values or sub-ranges encompassed within that range as if each numerical value and sub-range is explicitly recited. For example, a temperature range of about 70° C. to about 180° C. should be interpreted to include not only the explicitly recited limits of about 70° C. to about 180° C., but also to include sub-ranges, such as 90° C. to 110° C., 120° C. to 160° C., and so forth, as well as individual amounts, including fractional amounts, within the specified ranges, such as 82° C., 121.6° C., and 168.3° C., for example.
- As discussed above, methods of synthesis of 5-hydroxy methyl furfural (5-HMF) using various catalyst and solvents through microwave assisted method and conventional methods as disclosed in the prior arts have several drawbacks such as longer reaction time, higher cost, catalyst and product separation, low catalyst activity, and low yield. The present disclosure is directed to a process for synthesis of a furan derivative, more particularly 5-hydroxy methyl furfural (5-HMF), from sugars with a short time microwave assisted or conventional heating reaction, by using homogeneous or heterogeneous-solid acid catalyst. The use of the acid catalyst in monophasic organic solvent system for the synthesis of 5-HMF provides excellent catalytic activity, selectivity, conversion, rate of production and yield of product. Also, the use of a heterogeneous-solid acid catalyst, DICAT, in the present invention provides the convenience of a simple process for separating the catalyst from the reaction mixture. The reaction products and catalyst are easily separated from reaction mixture by conventional methods such as simple solvent distillation and filtration procedures.
- The process for preparing a furan derivative as disclosed herein, comprises the steps of a) contacting a sugar with a monophasic organic solvent to obtain a reaction mixture; and b) subjecting the reaction mixture to a temperature in the range from 100° C. to 180° C., in presence of an acid catalyst, for a time period in the range of 0.5 min to 4.0 h to obtain at least 70% conversion of the sugar to a single furan derivative, wherein the acid catalyst is selected from the group consisting of homogenous acid catalyst, heterogeneous solid acid catalyst, and combinations thereof.
- The present disclosure further relates to a process for preparing a heterogeneous solid acid catalyst, the process comprising the steps of: a) contacting a sulfonating agent with a polymer in presence of an organic solvent to obtain a reaction suspension; b) agitating the reaction suspension at a temperature in the range of 35° C. to 100° C. for a time period in the range of 30 min to 4 hrs to obtain a suspension of heterogeneous acid catalyst; and c) isolating the suspension of heterogeneous acid catalyst to obtain a heterogeneous solid acid catalyst.
- In one implementation, the furan derivative prepared by the disclosed process is 5-hydroxy methyl furfural (5-HMF).
- Saccharides are used as substrates for synthesis of furan derivatives. In one implementation, saccharide sources used for the disclosed process include, but are not limited to hexose and pentose sugars, polysaccharides comprising at least one hexose, corn syrup, high fructose corn syrup, cane sugar molasses, fructose, fructose syrup, crystalline fructose, crude fructose; purified fructose, high fructose concentration, fructose syrup or combinations thereof. In one implementation, the substrate is a hexose sugar. In one implementation, the sugar is selected from the group consisting of glucose, fructose, sucrose, and combinations thereof. In another implementation, the sugar is fructose. In one application, the form of fructose is anhydrous. In one implementation, the sugar is in amorphous form. In one implementation, the sugar is in crystalline form.
- The solvent as used in the process disclosed herein is a monophasic organic solvent. In one implementation, the solvent is selected from the group consisting of alcohols with the formula R—OH, N, N-Dimethyl formamide, Dimethyl sulfoxide, esters, and 1, 4-dioxane. In one implementation, the solvent is an alcohol with the formula R—OH, wherein R ranges from C1 to C15, more preferably C1 to C4. In one implementation, the C1 to C4 alcohol is selected from the group consisting of methanol, ethanol, n-propanol, iso-propanol, sec-butanol, tert-butanol, and combinations thereof. In another implementation, the C1 to C4 alcohol is isopropanol. In one implementation, the monophasic organic solvent has a boiling point less than 100° C.
- The reaction mixture for preparing a furan derivative comprises a sugar and a low boiling point organic solvent. In one implementation, the concentration of sugar in the reaction mixture is in the range of 1-50% (w/v), preferably 1-10% (w/v). In one implementation, the water content in the reaction mixture is in the range of 0 to 20%, preferably 0 to 6% w/w.
- In one implementation, the reaction is carried out at a temperature in the range of 100-180° C. In one implementation, contacting the reaction mixture with microwave radiation to bring it to a temperature in the range of 100° C. to 180° C. for a desired time is sufficient to convert at least 70% of the reactant into the desired product. In another implementation, contacting the reaction mixture with microwave radiation to bring it to a temperature in the range of 100° C. to 180° C. for a desired time is sufficient to convert at least 90% of the reactant into the desired product.
- In one implementation, the reaction is carried out at a temperature in the range of 100-180° C. In one implementation, contacting the reaction mixture with a conventional heater bringing it to a temperature in the range of 100° C. to 180° C. for a desired time is sufficient to convert at least 70% of the reactant into the desired product. In another implementation, contacting the reaction mixture a conventional heater bringing it to a temperature in the range of 100° C. to 180° C. for a desired time is sufficient to convert at least 90% of the reactant into the desired product.
- In an implementation, process for synthesis of 5-HMF is carried out in a microwave reactor, wherein the temperature is in the range of 100-180° C. In another implementation, the preferred temperature is in the range of 110-150° C. under microwave heating condition. In one implementation, the process provides the use of microwave reactor with frequency of 2.45 GHz, and power ranging between 10-400 watts. In one implementation, the reaction mixture is stirred at the rotational speed ranging between 200-800 rpm. In another implementation, the reaction mixture is stirred at the rotational speed ranging between 400-650 rpm. In one implementation, the reaction is carried under microwave heating conditions for 30-300 seconds. In another implementation, the reaction is carried under microwave heating conditions for 30-120 seconds.
- In one implementation, the process for synthesis of 5-HMF is carried out by means of conventional heating under pressure in the range of 5-50 bar. In another implementation, conventional heating is done under pressure in the range of 5-30 bar. In one implementation, the reaction mixture is heated to a temperature in the range of 100-180° C. In another implementation, the reaction mixture is heated to a temperature in the range of 100-150° C. The temperature was maintained by proportional-integral-derivative (PID) heating temperature controller. In one implementation, reaction time under conventional heating is in the range of 0.5-5 hrs. In one implementation, reaction time under conventional heating is in the range of 0.5-4 hrs. In one implementation, reaction time under conventional heating is in the range of 0.5-3 hrs. In one implementation, the agitation of reaction mixture is carried out by four pitch bladed impeller at a rotational speed in the range of 100-800 rpm.
- In one implementation, conversion of the sugar by the process disclosed herein is in the range of 45-100%. In another implementation, conversion of the sugar by the process disclosed herein is in the range of 95-100%.
- In one implementation, the yield of furan derivative by the process disclosed herein is in the range of 10-95%. In another implementation, the yield of furan derivative by the process disclosed herein is in the range of 80-95%.
- In one implementation, the process is carried in a batch mode reactor. In one implementation, the process is carried out in a continuous reactor. In one implementation, the process is carried out in the fixed bed reactor.
- The process for preparation of a furan derivative from a sugar is carried out in presence of an acid catalyst. In one implementation, the acid catalyst is used in an amount in the range of 0.01 to 5 g/cc of the reaction mixture. In another implementation, the acid catalyst is used in an amount in the range of 0.1 to 1.0 g/cc of the reaction mixture.
- Following conversion of sugar to a furan derivative, the reaction mixture is cooled and the catalyst is separated by filtration and reused for next reaction. In one implementation, recycling of catalyst is performed up to 20 times without addition of fresh catalyst and without regeneration. In another implementation, recycling of catalyst is performed more than 20 times without addition of fresh catalyst and without regeneration. In another implementation, recycling of catalyst is performed up to 5 times without addition of fresh catalyst and without regeneration.
- In one implementation, the acid catalyst is a homogenous acid catalyst. In one implementation, the homogenous acid catalyst is an aliphatic sulfonic acid. In one implementation, the homogenous acid catalyst is an aromatic sulfonic acid. In one implementation, the aromatic sulfonic acid is selected from the group consisting of naphthalene sulfonic acids, dimethyl aniline sulfonic acid, para-toluene sulfonic acid (p-TSA), ortho/meta-toluene sulfonic acid (o/m-TSA), and combinations thereof. In another implementation, the aromatic sulfonic acid is para-toluene sulfonic acid (p-TSA).
- In one implementation, the acid catalyst is a heterogenous solid acid catalyst. In one implementation, the heterogenous solid acid catalyst is a hydrophilic sulfonated solid porous matrix. In one implementation, the heterogenous solid acid catalyst is DICAT acid catalyst.
- In one implementation, there is provided a process for preparing a heterogenous solid acid catalyst. The process for preparing a heterogenous solid acid catalyst comprises the steps of: a) contacting a sulfonating agent with a polymer in presence of an organic solvent to obtain a reaction suspension; b) agitating the reaction suspension at a temperature in the range of 35° C. to 100° C. for a time period in the range of 30 min to 4 hrs to obtain a suspension of heterogeneous acid catalyst; and c) isolating the suspension of heterogeneous acid catalyst to obtain a heterogeneous solid acid catalyst.
- In one implementation, the sulfonating agent is selected from the group consisting of chlorosulfonic acid, sulphuric acid, sulfur trioxide, and combinations thereof. In one implementation, the sulfonating agent is chlorosulfonic acid.
- In one implementation, the heterogenous solid acid catalyst is composed of a hydrophilic functionalized polymer. In one implementation, the functionalized polymer has a surface area in the range of 5-200 m2/g. In another implementation, the functionalized polymer has a surface area in the range of 5-50 m2/g, pore size in the range of 2-50 nm, acidity in the range of 0.5-10 mmol/g, pore volume in the range of 0.022-2.0 cc/g. In one implementation, the molecular weight of the polymer is in the range of 3-23 kDa, particle size is in the range of 10-300 μm, and hydroxy value is in the range of 1 to 20 mg/g. In one implementation, the polymer is a homolinear polymer. In one implementation, the polymer is a crosslinked polymer. In one implementation, the polymer used is in crystalline form. In one implementation, the polymer used is in amorphous form. In one implementation, the polymer is in the form of spherical beads.
- In one implementation, the polymer comprises hydroxy functional group. In one implementation, the polymer comprises amine functional group. In one implementation, the polymer is selected from the group consisting of cellulose, polyvinyl alcohol, polyhydroxyethylmethacrylate, polyhydroxymethylmethacrylate polyethylene glycol, polypropylene glycol, silica, alumina, polyethylene amine, polyamide, and polyallylamine. In another implementation, the polymer is selected from the group consisting of cellulose, polyvinyl alcohol, polyhydroxyethylmcthacrylate, and polyhydroxymethylmcthacrylate.
- In one implementation, sulfonic acid derivatization of polymeric surfaces to obtain a heterogenous solid acid catalyst is done in presence of an organic solvent. In one implementation, the organic solvent is a non nucleophilic solvent. In one implementation, the organic solvent is selected from the group consisting of methylene dichloride, chloroform, carbon-tetrachloride, ethylene dichloride, propylene dichloride, and combinations thereof.
- In one implementation, the heterogonous solid acid catalyst as prepared by the process disclosed herein can also be used for various acid catalyzed organic transformation such as hydrolysis, elimination, addition, substitution, condensation, esterification, protection, deprotection, rearrangement, and ring opening.
- In one implementation, there is disclosed a process for preparing 5-HMF, the process comprising the steps of: a) contacting fructose with isopropanol to obtain a reaction mixture; and b) subjecting the reaction mixture to a temperature of 120° C., in presence of an acid catalyst, for a time period of 2.0 min to obtain at least 70% conversion of fructose to 5-HMF, wherein the acid catalyst is PTSA.
- In one implementation, there is disclosed a process for preparing 5-HMF, the process comprising the steps of: a) contacting fructose with isopropanol to obtain a reaction mixture; and b) subjecting the reaction mixture to a temperature of 130° C., in presence of an acid catalyst, for a time period in the range of 2.0 min to obtain at least 70% conversion of fructose to 5-HMF, wherein the acid catalyst is DICAT.
- The disclosure is further illustrated with the following schemes:
- The disclosure will now be illustrated with working examples, which is intended to illustrate the working of disclosure and not intended to take restrictively to imply any limitations on the scope of the present disclosure. Other examples are also possible which are within the scope of the present disclosure.
- The experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz. 1 gm of crystalline fructose was added to 8 ml isopropyl alcohol in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature to obtain a reaction suspension. 0.1 gm/cc of acid catalyst (as provided in Table 1) was added to this reaction suspension under continuous stirring. The resulting reaction mixture was heated to 120° C. under stirring for 120 seconds by subjecting to microwave radiation. After 120 seconds, the reaction mass was cooled to room temperature. The HPLC analysis of the sample was obtained which demonstrates 84-94% molar yield of HMF with 97-98% of fructose conversion. The solvent was removed by the vacuum distillation to get dark brown viscous oil of crude HMF.
- The Table 1 given below provides the HMF yields and fructose conversions with different acid catalyst using the process described above.
-
TABLE 1 Time Temperature % Fructose % HMF Example-1 Catalyst (Sec.) (° C.) Conversion Yield A PTSA 120 120 98.78 92.12 B DICAT-1 120 120 98.52 85.76 C DICAT-2 120 120 97.45 84.00 D DICAT-3 120 120 97.60 93.85 - The experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz. 1 gm of crystalline fructose was added to 8 ml solvent (as provided in Table 2) in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature to obtain a reaction suspension. 0.1 gm/cc of acid catalyst (PTSA) was added to this reaction suspension under continuous stirring. The resulting reaction mass was heated under stirring for 120 seconds by subjecting to microwave radiation. After 120 seconds, the reaction mixture was cooled to room temperature. The HPLC analysis of the sample was obtained which demonstrates 76-88% molar yield of HMF with 80-99% of fructose conversion. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- The Table 2 given below provides the HMF yields and fructose conversions with different solvent using the process described above.
-
TABLE 2 % Temperature Time % Fructose HMF Example-2 Solvent (° C.) (seconds) Conversion Yield A IPA 120 120 97.60 76.34 (iso-propyl alcohol) B TBA 120 120 97.80 38.28 (tert-butyl alcohol) C NBA 120 120 80.22 46.81 (n-butyl alcohol) D IAA 120 120 94.66 16.90 (iso-amyl alcohol) E DMSO 120 120 98.94 88.14 (dimethyl sulfoxide) F DMF (N,N- 120 120 99.18 88.70 dimethyl formamide) - The experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz. 1 gm of crystalline fructose was added to 8 ml isopropyl alcohol in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature. To this reaction suspension desired amount of PTSA (as provided in Table 3) was charged under stirring. The resulting reaction mass was heated for 90 seconds by subjecting to microwave radiation. After 90 seconds, reaction mass was cooled at room temperature. The HPLC analysis of the sample was obtained which demonstrates 74-88% molar yield of HMF with 94-98% of fructose conversion. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- The Table 3 given below provides the HMF yields and fructose conversions with varying acid catalyst concentrations using the process described above.
-
TABLE 3 Catalyst concentration Time Temperature % Fructose % HMF Example-3 (g/cc) (Sec.) (° C.) Conversion Yield A 0.03 90 120 94.97 74.83 B 0.07 90 120 97.85 83.21 C 0.10 90 120 98.78 88.22 D 0.13 90 120 98.46 75.76 - The experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz. 1 gm of crystalline fructose was added to 8 ml isopropyl alcohol in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature. To this reaction suspension 0.10 gm/cc of PTSA was charged under stirring. The resulting reaction mass was heated to 120° C. by subjecting to microwave radiation for desired time period (as provided in Table 4). Thereafter the reaction mass was cooled to room temperature. The HPLC analysis of the sample was obtained which demonstrates the 32-91% molar yield of HMF and 50-100% of fructose conversion. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- The Table 4 given below provides the HMF yields and fructose conversions with varying reaction time by using process described above.
-
TABLE 4 Catalyst concentration Time Temperature % Fructose % HMF Example-4 (g/cc) (Sec.) (° C.) Conversion Yield A 0.10 30 120 50.00 32.58 B 0.10 90 120 98.32 90.89 C 0.10 150 120 100.00 84.12 D 0.10 180 120 100.00 74.32 - The experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz. 1 gm of crystalline fructose was added to 8 ml of solvent (as provided in Table 5) in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature. To this reaction suspension desired amount of acid catalyst (DICAT-1) was added under stirring. The resulting reaction mixture was heated for 120 seconds by subjecting to microwave radiation under stirring. After 120 seconds, the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration. The sample obtained demonstrated 50-94% molar yield of HMF with 80-99% of fructose conversion through HPLC analysis. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- The Table 5 given below provides the HMF yields and fructose conversions with varying reaction solvent by using process described above.
-
TABLE 5 Temperature Time % Fructose % HMF Example-5 Solvent (° C.) (seconds) Conversion Yield A IPA 130 120 97.60 93.85 B TBA 130 120 97.80 50.23 C NBA 130 120 80.22 59.30 D IAA 130 120 94.66 52.34 E DMSO 130 120 98.94 90.08 F DMF 130 120 99.18 86.70 - The experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz. 1 gm of crystalline fructose was added to 8 ml of solvent (as provided in Table 6) in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature. To this reaction suspension desired amount of acid catalyst (DICAT-3) was added under stirring. The resulting reaction mixture was heated for 120 seconds by subjecting to microwave radiation under stirring. After 120 seconds, the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration. The sample obtained demonstrated 50-94% molar yield of HMF with 80-99% of fructose conversion through HPLC analysis. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- The Table 6 given below provides the HMF yields and fructose conversions with varying reaction solvent by using process described above.
-
TABLE 6 Temperature Time % Fructose % HMF Example-5 Solvent (° C.) (seconds) Conversion Yield A IPA 130 120 97.60 93.85 B TBA 130 120 97.80 50.23 C NBA 130 120 80.22 59.30 D IAA 130 120 94.66 52.34 E DMSO 130 120 98.94 90.08 F DMF 130 120 99.18 86.70 - The experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz. 1 gm of crystalline fructose was added to 8 ml of solvent (as provided in Table 6) in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature. To this reaction suspension desired amount of acid catalyst (DICAT-3) was charged (as provided in Table 6). The resulting reaction mass was heated for 120 seconds by subjecting to microwave radiation under stirring. After 120 seconds, the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration. HPLC analysis of the sample demonstrated 61-93% molar yield of HMF with 97-100% fructose conversion. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- The Table 7 given below provides the HMF yields and fructose conversions with varying catalyst DICAT-3 concentration by using process described above.
-
TABLE 7 Catalyst Conc. Temperature Time % Fructose % HMF Example-6 (gm/cc) (° C.) (seconds) Conversion Yield A 0.04 130 120 96.92 61.18 B 0.08 130 120 98.60 85.03 C 0.11 130 120 97.60 93.85 D 0.15 130 120 100.00 85.65 - The experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz. 1 gm of crystalline fructose was added to 8 ml of isopropyl alcohol in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature. To this reaction suspension 0.11 gm/cc of acid catalyst (DICAT-3) was charged under stirring. The resulting reaction mass was heated under continuous stirring to 130° C. by subjecting to microwave radiation for desired time period (as provided in Table 8). After completion of the reaction, the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration. The sample obtained demonstrated 50-92% molar yield of HMF with 98-100% fructose conversion through HPLC analysis. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- The Table 8 given below provides the HMF yields and fructose conversions with varying reaction time.
-
TABLE 8 Catalyst concentration Time Temperature % Fructose % HMF Example-7 (g/cc) (Sec.) (° C.) Conversion Yield A 0.10 30 130 97.61 50.01 B 0.10 90 130 98.52 73.16 C 0.10 120 130 99.12 92.22 D 0.10 180 130 100.00 74.32 - The experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz. 1 gm of crystalline fructose was added to 8 ml of isopropyl alcohol in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature. To this reaction suspension 0.11 gm/cc of acid catalyst (DICAT-3) was charged under stirring. The resulting reaction mass was heated under continuous stirring to desired temperature (as provided in Table 9) by subjecting to microwave radiation for 120 seconds. After completion of the reaction, the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration. The sample obtained demonstrated 21-93% molar yield of HMF with 73-100% of fructose conversion through HPLC analysis. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- The Table 9 given below provides the HMF yields and fructose conversions with varying reaction temperature by using process described above.
-
TABLE 9 Catalyst concentration Time Temperature % Fructose % HMF Example-8 (g/cc) (Sec.) (° C.) Conversion Yield A 0.11 120 100 73.14 21.98 B 0.11 120 120 98.16 74.60 C 0.11 120 130 98.27 93.22 D 0.11 120 150 100.00 80.27 E 0.11 120 180 100.00 72.76 - The experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz. A desired amount of crystalline fructose (as shown in Table 10) was added to a requisite amount of the solvent in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature. To this reaction suspension 0.11 gm/cc of acid catalyst (DICAT-3) was charged under stirring. The resulting reaction mass was heated under continuous stirring to a temperature of 130° C. by subjecting to microwave radiation for 120 seconds. After completion of the reaction, the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration. The sample obtained demonstrated 26-92% molar yield HMF of with 99-100% fructose conversion through HPLC analysis. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- The Table 10 given below provides the HMF yields and fructose conversions with varying fructose concentration by using process described above.
-
TABLE 10 Fructose Conc. Temperature Time % Fructose % HMF Example-9 (gm/cc) (° C.) (seconds) Conversion Yield A 0.125 130 120 99.340 52.34 B 0.063 130 120 98.520 92.83 C 0.031 130 120 100.000 54.23 D 0.016 130 120 100.000 26.23 - The experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz. 1 gm of desired substrate (as shown in Table 11) was added to a requisite amount of the solvent (16 ml) in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature. To this reaction suspension 0.11 gm/cc of acid catalyst (DICAT-3) was charged under stirring. The resulting reaction mass was heated under continuous stirring to a temperature of 130° C. by subjecting to microwave radiation for 120 seconds. After completion of the reaction the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration. The sample obtained demonstrated 48-93% molar yield of HMF with 99-100% of fructose conversion through HPLC analysis. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- The Table 11 given below provides the HMF yields and fructose conversions with varying substrate by using process described above.
-
TABLE 11 Example- Temperature % 10 Substrate (° C.) % Conversion Yield A Fructose 130 97.60 93.85 B Glucose 130 96.93 48.04 C Glucose/Fructose (1:1) 130 97.65 60.78 D Sucrose 130 100.00 86.84 - The experiment is carried out in batch mode operation under microwave heating at a frequency of 2.45 GHz. 1 gm of fructose was added to a requisite amount of the solvent (16 ml) in a 20 ml sealed glass tube with magnetic stirrer; and stirred for 5 minute at room temperature. To this reaction suspension 0.11 gm/cc of acid catalyst (DICAT-1) was charged under stirring. The resulting reaction mass was heated under continuous stirring to a temperature of 130° C. by subjecting to microwave radiation for 120 seconds. After completion of the reaction, the reaction mass was cooled at room temperature and catalyst was removed by vacuum filtration and the catalyst was recycled for subsequent runs (as provided in Table 12). The obtained filtrate sample was analyzed for HPLC which demonstrates 94-95% molar yield of HMF with 98-99% of fructose conversion. The solvent was removed by the vacuum distilled to get dark brown viscous oil of crude HMF.
- The Table 12 given below provides the HMF yields and fructose conversions with number of catalyst recycle by using process described above.
-
TABLE 12 Example- Fructose Temperature % % 11 Catalyst Run Conc. (° C.) Conversion Yield A 1 0.063 130 99.14 95.90 B 2 0.063 130 98.47 95.05 C 3 0.063 130 99.08 94.00 D 4 0.063 130 99.26 94.95 E 5 0.063 130 99.20 95.57 - The experiments was carried out in batch mode operation under conventional heating in a 300 ml Parr pressure reactor autoclave assembly having four peach bladed ampler and PID temperature controller with accuracy ±1° C. The autoclave was loaded with 2 gm of crystalline fructose in desired amount of solvent (32 ml) and a desired acid catalyst DICAT (as provided in Table 13). The reaction mass in the autoclave was stirred for 5 minute at room temperature followed by nitrogen purging 2-3 times. The autoclave was pressurized to 15 kg/cm3 using nitrogen and reaction mass was heated for 120 min under constant stirring. After 120 min of reaction, the reaction mass was cooled to room temperature and finally the nitrogen pressure was released. Heterogeneous catalyst in the reaction mass was removed by vacuum filtration. The sample from this filtrate was analyzed for HPLC and demonstrated 68-90% molar yield of HMF, with 96-98% fructose conversion. The solvent was removed by the vacuum distillation to obtain a dark brown viscous oil of crude HMF.
- The Table 13 given below provides the HMF yields and fructose conversions with varying acid catalyst by using process described above.
-
TABLE 13 Example- Time Temperature % Fructose % HMF 12 Catalyst (min) (° C.) Conversion Yield A PTSA 120 120 96.51 68.54 B DICAT-1 120 120 98.52 70.97 C DICAT-2 120 120 98.12 70.36 D DICAT-3 120 130 98.32 90.76 - All the experiments were carried out in batch mode operation under conventional heating in a 300 ml Parr pressure reactor autoclave assembly having four peach bleded ampler and PID temperature controller with accuracy ±1° C. The autoclave was loaded with 2 gm of crystalline fructose in desired amount of solvent (32 ml) and a desired acid catalyst DICAT-3. The reaction mass in the autoclave was stirred for 5 minute at room temperature followed by 2-3 time nitrogen purging. The desired pressure (as provided in Table 14) was obtained by employing nitrogen gas and reaction mass was heated for 120 min under stirring followed by sample removal at desired time intervals. After 120 min reaction mass was cooled at room temperature, and nitrogen pressure was released. The heterogeneous catalyst was removed by vacuum filtration. The sample from this filtrate was analyzed through HPLC and depicted 40-90% molar yield of HMF, with 60-100% fructose conversion. Then the solvent was removed by the vacuum distilled to dark brown viscous oil of crude HMF.
- The Table 14 given below provides the HMF yields and fructose conversions with varying pressure by using process described above.
-
TABLE 14 Example- Pressure Time Temperature % Fructose % HMF 13 (Kg/cm3) (min) (° C.) Conversion Yield A 5 120 120 60.51 40.54 B 10 120 120 78.52 52.97 C 15 120 120 98.32 90.76 D 20 120 120 99.32 84.76 E 25 120 120 100.00 60.40 - All the experiments were carried out in batch mode operation under conventional heating in a 300 ml Parr pressure reactor autoclave assembly having four peach bleded ampler and PID temperature controller with accuracy ±1° C. The autoclave was loaded with 2 gm of crystalline fructose in desired amount of IPA (32 ml) and a desired acid catalyst DICAT-3. The reaction mass in the autoclave was stirred for 5 minute at room temperature followed by 2-3 time nitrogen purging. The desired nitrogen pressure of 15 kg/cm3 was employed and reaction mass was heated for desire time (as provided in Table 15) under constant stirring. After completion of reaction, reaction mass was cooled at room temperature and the nitrogen pressure was released. The heterogeneous catalyst was removed from the reaction mass by vacuum filtration. The sample from this filtrate was analyzed for HPLC and showed 30-90% molar yield of HMF, with 60-100% fructose conversion. The solvent was removed by the vacuum distillation to obtain dark brown viscous oil of crude HMF.
- The Table 15 given below provides the HMF yields and fructose conversions with varying time period by using process described above.
-
TABLE 15 Example- Pressure Time Temperature % Fructose % HMF 14 (Kg/cm3) (min) (° C.) Conversion Yield A 15 30 120 60.51 30.54 B 15 90 120 78.52 52.97 C 15 120 120 98.32 90.76 D 15 180 120 99.32 70.72 E 15 240 120 100.00 62.42 - The heterogeneous solid acid catalyst DICAT was prepared by sulfonic acid anchoring on aliphatic hydroxy groups of hydrophilic polymer through organic linkage. The typical experimental process for preparation of DICAT is as follows:
- The reaction was carried out in a four necked 250 ml dry round bottomed flask with heating oil bath, reflux condenser, thermometer pocket, addition funnel and over head stirrer. 1 gm of hydroxy polymer, (polyvinyl alcohol) was added under nitrogen blanketing. 10 ml of ethylene dichloride was charged in flask under slow stirring. The 9.5 ml of sulfonating agent, (chlorosulfonic acid) was added drop wise for 30 min through addition funnel under vigorous stirring. After the completion of addition reaction, reaction mass was stirred vigorously for 20-30 min at room temperature and then heated to reflux for 1 hr. On completion of 1 hr reflux, reaction mass was allowed to cool at room temperature and subsequently to 0° C.; thereafter 10 ml of aqueous methanol was added slowly through addition funnel within 30 min and maintained at 0° C. under vigorous stirring for another 30 min. The resulting black solid was then filtered by suction pump and washed by cold water till removal of chlorine from filtrate which was tested by AgNO3 precipitation test. Finally the solid cake was suck dried by suction pump and kept for drying at 70-80° C. under vacuum. Resulting black color dry powder of DICAT obtained was used for reaction.
- The synthesis of HMF in packed bed reactor was performed in steel column of 2×20 cm height with heating jacket having inlet outlet temperature sensor and pressure control valve. The 5 cm catalyst bed was packed with sufficient amount of inert material. Before passing the substrate through packed bed column, the column was pre equilibrated by passing 2-5 column volume (CV) of fresh water and IPA to obtain column temperature of 120° C. and 10-15 kg/cm3 pressure. The pre heated 100 ml 6.25% solution of fructose in IPA was passed through catalyst bed maintained at 120° C. by conventional heating with desire flow rate in cyclic loop by means of binary piston pressure pump. Simultaneously, the samples from reaction mixture were removed at different time intervals for in process HPLC analysis. Once the requisite HMF yield and fructose conversion were obtained, the substrate flow was stopped and catalyst bed was washed by 2 CV of fresh IPA to remove the line and the catalyst bed hold up. The resulting composite fraction was analyzed through HPLC and depicted results in the range of 88-94% HMF yield with 95-100% of fructose conversion.
- The synthesis of HMF in packed bed reactor was performed in steel column of 2×20 cm height with heating jacket having inlet outlet temperature sensor and pressure control valve. The 5 cm catalyst bed was packed with sufficient amount of inert material. Before passing the substrate through packed bed column, the column was pre equilibrated by passing 2-5 column volume (CV) of fresh water and IPA to obtain column temperature of 120° C. and 10-15 kg/cm3 pressure. The pre heated 100 ml 6.25% solution of fructose in IPA was passed through catalyst bed maintained at 120° C. by microwave heating with desired flow rate in cyclic loop by means of binary piston pressure pump. Simultaneously, the samples from reaction mixture were removed at different time intervals for in process HPLC analysis. Once the requisite HMF yield and fructose conversion were obtained, the substrate flow was stopped and catalyst bed was washed by 2 CV of fresh IPA to remove the line and the catalyst bed hold up. The resulting composite fraction was analyzed through HPLC and depicted results in the range of 88-94% HMF yield with 95-100% of fructose conversion.
- The present disclosure relates to a process of preparing 5-hydroxymethyl furfural (5-HMF) from saccharides utilizing an acid catalyst. The acid catalyzed cyclodehydration process for synthesis of 5-HMF provides a simple and cost effective route for the production of 5-HMF in monophasic organic solvent. The heterogenous solid acid catalyst, DICAT used in the process disclosed herein has excellent catalytic activity, stability, and selectivity towards desired product. Due to higher selectivity of catalyst, formation of side products such as polymers, humins, levulinic acid, and condensation products is significantly reduced. The overall process employs use of monophasic organic solvents (low boiling, or high boiling) which are easy to separate with minimum energy utilization for solvent distillation. The process is carried out in significantly decreased reaction time through conventional or microwave assisted heating resulting in increased productivity.
- The comprises microwave assisted short time reaction that is carried out in a monophasic organic solvent at temperature ranges of 100-180° C., thus providing process feasibility at an economical cost and with low energy consumption. The short reaction time of 30-120 seconds enhance the bulk production and economics of 5-HMF production in the given time period.
- The present process for synthesis of 5-HMF synthesis involves lower energy utilization with production of minimum waste and effluents.
- The disclosed process is therefore a green and efficient process which results in higher selectivity and yield; has a higher conversion rate with enhanced catalytic stability, has ease of separation and most importantly has the advantage of recycling the catalyst with 100% recovery.
- Although the subject matter has been described in considerable detail with reference to certain examples and implementations thereof, other implementations are possible. As such, the spirit and scope of the appended claims should not be limited to the description of the preferred examples and implementations contained therein.
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CN105418550A (en) | 2010-07-30 | 2016-03-23 | 阿彻丹尼尔斯米德兰德公司 | Microwave assisted synthesis of dehydrated sugar derivatives hydroxymethylfurfural, levulinic acid, anhydrosugar alcohols, and ethers thereof |
SG11201400867PA (en) * | 2011-09-23 | 2014-04-28 | Agency Science Tech & Res | Method of producing 5-hydroxymethylfurfural from carbohydrates |
US8772515B2 (en) * | 2012-10-11 | 2014-07-08 | Wisconsin Alumni Research Foundation | Method to convert biomass to 5-(hydroxymethyl)-furfural (HMF) and furfural using lactones, furans, and pyrans as solvents |
ITNO20130003A1 (en) | 2013-05-09 | 2014-11-10 | Novamont Spa | 5-HYDROXYMETHYLPHURFURAL SYNTHESIS PROCESS FROM SACCHARIDES |
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2014
- 2014-11-21 WO PCT/IB2014/002537 patent/WO2015075540A1/en active Application Filing
- 2014-11-21 BR BR112016011539A patent/BR112016011539A2/en not_active Application Discontinuation
- 2014-11-21 CA CA2931330A patent/CA2931330A1/en not_active Abandoned
- 2014-11-21 EP EP14819069.7A patent/EP3071556A1/en not_active Withdrawn
- 2014-11-21 JP JP2016533608A patent/JP6410822B2/en not_active Expired - Fee Related
- 2014-11-21 US US15/038,416 patent/US9975866B2/en not_active Expired - Fee Related
- 2014-11-21 CN CN201480073605.1A patent/CN106061955A/en active Pending
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2018
- 2018-05-16 US US15/981,264 patent/US20180258060A1/en not_active Abandoned
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CA2931330A1 (en) | 2015-05-28 |
JP2016539941A (en) | 2016-12-22 |
CN106061955A (en) | 2016-10-26 |
BR112016011539A2 (en) | 2017-08-08 |
US9975866B2 (en) | 2018-05-22 |
JP6410822B2 (en) | 2018-10-24 |
US20160289203A1 (en) | 2016-10-06 |
EP3071556A1 (en) | 2016-09-28 |
WO2015075540A1 (en) | 2015-05-28 |
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