WO2012030619A1 - Succinic anhydride from ethylene oxide - Google Patents
Succinic anhydride from ethylene oxide Download PDFInfo
- Publication number
- WO2012030619A1 WO2012030619A1 PCT/US2011/049125 US2011049125W WO2012030619A1 WO 2012030619 A1 WO2012030619 A1 WO 2012030619A1 US 2011049125 W US2011049125 W US 2011049125W WO 2012030619 A1 WO2012030619 A1 WO 2012030619A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- catalyst
- reaction
- solvent
- carbonylation
- group
- Prior art date
Links
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
- C07D307/56—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 hetero atoms or with carbon atoms having three bonds to hetero atoms with at the most one bond to halogen, e.g. ester or nitrile radicals, directly attached to ring carbon atoms
- C07D307/60—Two oxygen atoms, e.g. succinic anhydride
-
- 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
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/2415—Tubular reactors
-
- 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
- B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J19/24—Stationary reactors without moving elements inside
- B01J19/245—Stationary reactors without moving elements inside placed in series
-
- 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
- B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
- B01J2219/24—Stationary reactors without moving elements inside
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/584—Recycling of catalysts
Definitions
- Acid anhydrides in particular succinic anhydride, are valuable reactive intermediates commonly used in a variety of applications.
- acid anhydrides are used in copolymers to produce biodegradable polyesters.
- acid anhydrides are useful intermediates in organic synthesis because they are easily ring opened to form diacids or other derivatives.
- Succinic anhydride is particularly useful as a precursor to 4 carbon commodity chemicals such as tetrahydrofuran, gamma butyrolactone and 1,4-butanediol.
- Additional production methods include catalyzed carbonylation of alkynes, alkenoic acids and lactones. Many of the methods suffered from low yield, production of many byproducts or lacked generality. Novel methods using more cost effective starting materials are sought.
- US Patent No. 6,852,865 discloses a class of well-defined bimetallic catalysts of the general type [Lewis acid] [M(CO) x ] ⁇ for the ring-expanding carbonylation of strained heterocycles.
- Related catalysts can carbonylate the resulting ⁇ -lactones to succinic anhydrides in high yields while preserving stereochemical purity.
- subsequent carbonylation of these ⁇ -lactones constitutes a versatile two-step method for the stereoselective synthesis of succinic anhydrides. (Scheme 1).
- the present invention includes a method of synthesizing succinic anhydride including the steps of: feeding a reaction stream including ethylene oxide, at least one catalyst, at least one solvent, and carbon monoxide to a reaction vessel under reaction conditions to promote a double carbonylation of ethylene oxide to form succinic anhydride in the reaction stream in a continuous flow process; b) treating the reaction stream containing succinic anhydride to conditions that cause the succinic anhydride to crystallize such that the reaction stream includes crystallized succinic anhydride and a liquid phase including catalyst and solvent; c) separating the crystallized succinic anhydride from the liquid phase; and d) recycling the catalyst and the solvent to the reaction stream including the ethylene oxide.
- the solvent includes dioxane.
- step b) occurs in an adiabatic evaporative cooling crystallizer.
- step c) occurs in a rotary drum filter.
- step d) includes the substep of feeding a solution including the catalyst and the solvent to a recovery flash drum to separate volatiles prior to returning the solution to the reaction stream.
- the method further includes treating the solution by performing at least one step selected from the group consisting of: drying the solution; heating or cooling the solution; removing spent catalyst; adding solvent; and any combination of two or more of these.
- the first carbonylation reaction is performed at a pressure from about 50 psi to about 5000 psi. In some embodiments, the first carbonylation reaction is performed at a pressure from about 50 psi to about 2000 psi. In some embodiments, the first carbonylation reaction is performed at a pressure from about 200 psi to about 1000 psi. In some embodiments, the first carbonylation reaction is performed at a pressure from about 200 psi to about 600 psi.
- the first carbonylation reaction is performed at a temperature from about 0 °C to about 125 °C. In some embodiments, the first carbonylation reaction is performed at a temperature from about 30 °C to about 100 °C. In some embodiments, the first carbonylation reaction is performed at a temperature from about 40 °C to about 80 °C.
- the at least one catalyst is a single catalyst.
- the single catalyst is [(ClTPP)Al(THF) 2 ] + [Co(CO) 4 ] ⁇ , where C1TPP is meso- tetra(4-chlorophenyl)porphyrinato and THF is tetrahydrofuran.
- the at least one catalyst includes a first catalyst selected to promote a first carbonylation of the double carbonylation and a second catalyst different from the first catalyst selected to promote a second carbonylation of the double carbonylation.
- the catalyst includes a metal carbonyl compound.
- the metal carbonyl compound has the formula [QM (CO) w ] x , where: Q is any ligand and need not be present; M is a metal atom; y is an integer from 1 to 6 inclusive; w is a number such as to provide the stable metal carbonyl; and x is an integer from -3 to +3 inclusive.
- M is selected from the group consisting of Ti, Cr, Mn, Fe, Ru, Co, Rh, Ni, Pd, Cu, Zn, Al, Ga, and In. In some embodiments, M is Co.
- the carbonylation catalyst further includes a Lewis acidic co- catalyst.
- the metal carbonyl compound is anionic, and the Lewis acidic co-catalyst is cationic.
- the metal carbonyl complex includes a carbonyl cobaltate and the Lewis acidic co-catalyst includes a metal-centered Lewis acid.
- the metal-centered Lewis acid is a metal complex of formula [M'(Z) 3 ⁇ 4 ] C+ , where: M' is a metal; each L is a ligand; b is an integer from 1 to 6 inclusive; c is 1, 2, or 3; and where, if more than one L is present, each L may be the same or different.
- M' is selected from the group consisting of: a transition metal, a group 13 or 14 metal, and a lanthanide.
- M' is a transition metal or a group 13 metal.
- M' is selected from the group consisting of aluminum, chromium, indium and gallium.
- M' is aluminum.
- M' is chromium.
- the Lewis acid includes a dianionic tetradentate ligand.
- the dianionic tetradentate ligand is selected from the group consisting of: porphyrin derivatives; salen derivatives; dibenzotetramethyltetraaza[14]annulene (tmtaa) derivatives; phthalocyaninate derivatives; and derivatives of the Trost ligand.
- step c) includes the substep of filtering the reaction stream.
- the present invention provides a succinic anhydride synthesis system including: a carbon monoxide source; an ethylene oxide source; a solvent source; a catalyst source; at least one reaction vessel fed with a reaction stream by the carbon monoxide source, the ethylene oxide source, the solvent source, and the catalyst source, the reaction stream including carbon monoxide, ethylene oxide, solvent, and catalyst; an adiabatic evaporative cooling crystallizer fed from the at least one reaction vessel; a rotary drum filter fed by the adiabatic evaporative cooling crystallizer; a solids dryer fed by the rotary drum filter; and a recovery flash drum fed by the adiabatic evaporative cooling crystallizer, the rotary drum filter, and the solids dryer, the recovery flash drum feeding recycled catalyst and solvent to the reaction stream.
- the reaction vessel includes a tubular reactor. In some embodiments, the reaction vessel includes a shell and tube adiabatic reactor. In some embodiments, the adiabatic evaporative cooling crystallizer includes a feed cooler and a crystallizer flash drum.
- the carbon monoxide source includes: a methane source; a steam reforming unit fed by the methane source; a hydrogen pressure swing adsorption unit fed by the steam reforming unit; a carbon monoxide pressure swing adsorption unit fed by the hydrogen pressure swing adsorption unit; a carbon monoxide compressor fed by the carbon monoxide pressure swing adsorption unit; and a carbon monoxide dryer fed by the carbon monoxide compressor.
- the solvent source includes: a solvent offloading pump; a solvent dryer fed by the solvent offloading pump; and a solvent storage tank fed by the solvent dryer; and a solvent charge pump fed by the solvent storage tank.
- the catalyst source includes a catalyst mix tank and a catalyst charge pump fed by the catalyst mix tank, wherein the solvent charge pump feeds solvent to the catalyst mix tank.
- Fig. 1 shows a process flow system for the production of succinic anhydride from ethylene oxide in one embodiment of the present invention.
- Certain compounds, as described herein may have one or more double bonds that can exist as either a Z or E isomer, unless otherwise indicated.
- the invention additionally encompasses the compounds as individual isomers substantially free of other isomers and alternatively, as mixtures of various isomers, e.g., racemic mixtures of enantiomers.
- this invention also encompasses compositions comprising one or more compounds.
- isomers includes any and all geometric isomers and stereoisomers.
- “isomers” include cis- and trans-isomers, E- and Z- isomers, R- and ⁇ -enantiomers, diastereomers, (D)-isomers, (L)-isomers, racemic mixtures thereof, and other mixtures thereof, as falling within the scope of the invention.
- a compound may, in some embodiments, be provided substantially free of one or more corresponding stereoisomers, and may also be referred to as "stereochemically enriched.”
- halo and “halogen” as used herein refer to an atom selected from fluorine
- halogenic refers to a compound substituted with one or more halogen atoms.
- aliphatic or "aliphatic group”, as used herein, denotes a hydrocarbon moiety that may be straight-chain (i.e., unbranched), branched, or cyclic (including fused, bridging, and spiro-fused polycyclic) and may be completely saturated or may contain one or more units of unsaturation, but which is not aromatic. Unless otherwise specified, aliphatic groups contain 1-30 carbon atoms. In certain embodiments, aliphatic groups contain 1-12 carbon atoms. In certain embodiments, aliphatic groups contain 1-8 carbon atoms. In certain embodiments, aliphatic groups contain 1-6 carbon atoms.
- aliphatic groups contain 1-5 carbon atoms, in some embodiments, aliphatic groups contain 1-4 carbon atoms, in yet other embodiments aliphatic groups contain 1-3 carbon atoms, and in yet other embodiments aliphatic groups contain 1-2 carbon atoms.
- Suitable aliphatic groups include, but are not limited to, linear or branched, alkyl, alkenyl, and alkynyl groups, and hybrids thereof such as (cycloalkyl)alkyl, (cycloalkenyl)alkyl or (cycloalkyl)alkenyl.
- heteroaliphatic refers to aliphatic groups wherein one or more carbon atoms are independently replaced by one or more atoms selected from the group consisting of oxygen, sulfur, nitrogen, phosphorus, or boron. In certain embodiments, one or two carbon atoms are independently replaced by one or more of oxygen, sulfur, nitrogen, or phosphorus. Heteroaliphatic groups may be substituted or unsubstituted, branched or unbranched, cyclic or acyclic, and include "heterocycle,” "heterocyclyl,”
- heterocycloaliphatic or “heterocyclic” groups.
- epoxide refers to a substituted or unsubstituted oxirane.
- Substituted oxiranes include monosubstituted oxiranes, disubstituted oxiranes, trisubstituted oxiranes, and tetrasubstituted oxiranes. Such epoxides may be further optionally substituted as defined herein. In certain embodiments, epoxides comprise a single oxirane moiety. In certain embodiments, epoxides comprise two or more oxirane moieties.
- the term "acrylate” or "acrylates” as used herein refer to any acyl group having a vinyl group adjacent to the acyl carbonyl. The terms encompass mono-, di- and tri-substituted vinyl groups.
- acrylates include, but are not limited to: acrylate, methacrylate, ethacrylate, cinnamate (3-phenylacrylate), crotonate, tiglate, and senecioate. Because it is known that cylcopropane groups can in certain instances behave very much like double bonds, cyclopropane esters are specifically included within the definition of acrylate herein.
- polymer refers to a molecule of high relative molecular mass, the structure of which comprises the multiple repetition of units derived, actually or conceptually, from molecules of low relative molecular mass.
- a polymer is comprised of only one monomer species (e.g., polyethylene oxide).
- a polymer of the present invention is a copolymer, terpolymer, heteropolymer, block copolymer, or tapered heteropolymer of one or more epoxides.
- unsaturated as used herein, means that a moiety has one or more double or triple bonds.
- alkyl refers to saturated, straight- or branched-chain hydrocarbon radicals derived from an aliphatic moiety containing between one and six carbon atoms by removal of a single hydrogen atom. Unless otherwise specified, alkyl groups contain 1-12 carbon atoms. In certain embodiments, alkyl groups contain 1-8 carbon atoms. In certain embodiments, alkyl groups contain 1-6 carbon atoms. In some embodiments, alkyl groups contain 1-5 carbon atoms, in some embodiments, alkyl groups contain 1-4 carbon atoms, in yet other embodiments alkyl groups contain 1-3 carbon atoms, and in yet other embodiments alkyl groups contain 1-2 carbon atoms.
- alkyl radicals include, but are not limited to, methyl, ethyl, n-propyl, isopropyl, n-butyl, iso-butyl, sec-butyl, sec- pentyl, iso-pentyl, tert-butyl, n-pentyl, neopentyl, n-hexyl, sec-hexyl, n-heptyl, n-octyl, n- decyl, n-undecyl, dodecyl, and the like.
- carbocycle and “carbocyclic ring” as used herein, refers to monocyclic and polycyclic moieties wherein the rings contain only carbon atoms. Unless otherwise specified, carbocycles may be saturated, partially unsaturated or aromatic, and contain 3 to 20 carbon atoms.
- the terms “carbocycle” or “carbocyclic” also include aliphatic rings that are fused to one or more aromatic or nonaromatic rings, such as decahydronaphthyl or tetrahydronaphthyl, where the radical or point of attachment is on the aliphatic ring. In some embodiments, a carbocyclic groups is bicyclic.
- a carbocyclic group is tricyclic. In some embodiments, a carbocyclic group is polycyclic. In certain embodiments, the terms "3- to 14-membered carbocycle" and “C3_i 4 carbocycle” refer to a 3- to 8-membered saturated or partially unsaturated monocyclic carbocyclic ring, or a 7- to 14-membered saturated or partially unsaturated polycyclic carbocyclic ring.
- carbocyles include cyclopropane, cyclobutane, cyclopentane, cyclohexane, bicyclo[2,2,l]heptane, norbornene, phenyl, cyclohexene, naphthalene, spiro[4.5]decane,
- aryl used alone or as part of a larger moiety as in “aralkyl”, “aralkoxy”, or “aryloxyalkyl” refers to monocyclic and polycyclic ring systems having a total of five to 20 ring members, wherein at least one ring in the system is aromatic and wherein each ring in the system contains three to twelve ring members.
- aryl may be used interchangeably with the term “aryl ring”.
- aryl refers to an aromatic ring system which includes, but is not limited to, phenyl, biphenyl, naphthyl, anthracyl and the like, which may bear one or more substituents.
- aryl is a group in which an aromatic ring is fused to one or more additional rings, such as benzofuranyl, indanyl, phthalimidyl, naphthimidyl, phenantriidinyl, or tetrahydronaphthyl, and the like.
- the terms “6- to 10-membered aryl” and “C 6 -io aryl” refer to a phenyl or an 8- to 10-membered polycyclic aryl ring.
- heteroaryl and “heteroar-”, used alone or as part of a larger moiety refer to groups having 5 to 14 ring atoms, preferably 5, 6, or 9 ring atoms; having 6, 10, or 14 electrons shared in a cyclic array; and having, in addition to carbon atoms, from one to five heteroatoms.
- heteroatom refers to nitrogen, oxygen, or sulfur, and includes any oxidized form of nitrogen or sulfur, and any quatemized form of a basic nitrogen.
- Heteroaryl groups include, without limitation, thienyl, furanyl, pyrrolyl, imidazolyl, pyrazolyl, triazolyl, tetrazolyl, oxazolyl, isoxazolyl, oxadiazolyl, thiazolyl, isothiazolyl, thiadiazolyl, pyridyl, pyridazinyl, pyrimidinyl, pyrazinyl, indolizinyl, purinyl, naphthyridinyl, benzofuranyl and pteridinyl.
- heteroaryl and “heteroar-”, as used herein, also include groups in which a heteroaromatic ring is fused to one or more aryl, cycloaliphatic, or heterocyclyl rings, where the radical or point of attachment is on the heteroaromatic ring.
- Nonlimiting examples include indolyl, isoindolyl, benzothienyl, benzofuranyl, dibenzofuranyl, indazolyl, benzimidazolyl, benzthiazolyl, quinolyl, isoquinolyl, cinnolinyl, phthalazinyl, quinazolinyl, quinoxalinyl, 4H-quinolizinyl, carbazolyl, acridinyl, phenazinyl, phenothiazinyl, phenoxazinyl, tetrahydroquinolinyl, tetrahydroisoquinolinyl, and pyrido[2,3-b]-l,4-oxazin-3(4H)-one.
- heteroaryl group may be mono- or bicyclic.
- heteroaryl may be used interchangeably with the terms “heteroaryl ring”, “heteroaryl group”, or “heteroaromatic”, any of which terms include rings that are optionally substituted.
- heteroarylkyl refers to an alkyl group substituted by a heteroaryl, wherein the alkyl and heteroaryl portions independently are optionally substituted.
- the term "5- to 14-membered heteroaryl” refers to a 5- to 6-membered heteroaryl ring having 1 to 3 heteroatoms independently selected from nitrogen, oxygen, or sulfur, or an 8- to 14-membered polycyclic heteroaryl ring having 1 to 4 heteroatoms independently selected from nitrogen, oxygen, or sulfur.
- heterocycle As used herein, the terms “heterocycle”, “heterocyclyl”, “heterocyclic radical”, and “heterocyclic ring” are used interchangeably and refer to a stable 5- to 7-membered monocyclic or 7- 14-membered bicyclic heterocyclic moiety that is either saturated, partially unsaturated, or aromatic and having, in addition to carbon atoms, one or more, preferably one to four, heteroatoms, as defined above.
- heterocycle When used in reference to a ring atom of a
- nitrogen includes a substituted nitrogen.
- the nitrogen in a saturated or partially unsaturated ring having 0-3 heteroatoms selected from oxygen, sulfur or nitrogen, the nitrogen may be N (as in 3,4-dihydro-2H-pyrrolyl), NH (as in pyrrolidinyl), or (as in N-substituted pyrrolidinyl).
- the term "3- to 14-membered heterocycle” refers to a 3- to 8-membered saturated or partially unsaturated monocyclic heterocyclic ring having 1 to 2 heteroatoms independently selected from nitrogen, oxygen, or sulfur, or a 7- to 14-membered saturated or partially unsaturated polycyclic heterocyclic ring having 1-3 heteroatoms independently selected from nitrogen, oxygen, or sulfur.
- a heterocyclic ring can be attached to its pendant group at any heteroatom or carbon atom that results in a stable structure and any of the ring atoms can be optionally substituted.
- saturated or partially unsaturated heterocyclic radicals include, without limitation, tetrahydrofuranyl, tetrahydrothienyl, pyrrolidinyl, pyrrolidonyl, piperidinyl, pyrrolinyl, tetrahydroquinolinyl, tetrahydroisoquinolinyl, decahydroquinolinyl, oxazolidinyl, piperazinyl, dioxanyl, dioxolanyl, diazepinyl, oxazepinyl, thiazepinyl, morpholinyl, and quinuclidinyl.
- heterocycle refers to an alkyl group substituted by a heterocyclyl, wherein the alkyl and heterocyclyl portions
- partially unsaturated refers to a ring moiety that includes at least one double or triple bond.
- the term “partially unsaturated” is intended to encompass rings having multiple sites of unsaturation, but is not intended to include aryl or heteroaryl moieties, as herein defined.
- compounds of the invention may contain "optionally substituted” moieties.
- substituted whether preceded by the term “optionally” or not, means that one or more hydrogens of the designated moiety are replaced with a suitable substituent.
- an "optionally substituted” group may have a suitable substituent at each substitutable position of the group, and when more than one position in any given structure may be substituted with more than one substituent selected from a specified group, the substituent may be either the same or different at every position.
- Combinations of substituents envisioned by this invention are preferably those that result in the formation of stable or chemically feasible compounds.
- stable refers to compounds that are not substantially altered when subjected to conditions to allow for their production, detection, and, in certain embodiments, their recovery, purification, and use for one or more of the purposes disclosed herein.
- Suitable monovalent substituents on a substitutable carbon atom of an "optionally substituted" group are independently halogen; -(CH 2 )o- 4 R°; -(CH 2 ) 0 ⁇ OR°;
- Suitable monovalent substituents on R° are independently halogen, -(CH 2 ) 0 2 R*, -(haloR*), -(CH 2 )o 2 OH, -(CH 2 ) 0 2 OR*, -(CH 2 ) 0 2 CH(OR*) 2 ; -O(haloR'), -CN, -N 3 , - (CH 2 )o 2 C(0)R*, -(CH 2 )o 2 C(0)OH, -(CH 2 ) 0 2 C(0)OR*, -(CH 2 ) 0 _ 4 C(O)N(R°) 2 ; -(CH 2 ) 0 2 SR*, -(CH 2 )o 2 SH, -(CH 2 )o 2 NH 2 , -(CH 2 ) 0 2 NHR*, -(CH 2 ) 0 _ 2
- Suitable divalent substituents that are bound to vicinal substitutable carbons of an "optionally substituted” group include: -0(CR 2 ) 2 3O-, wherein each independent occurrence of R is selected from hydrogen, Ci_ 6 aliphatic which may be substituted as defined below, or an unsubstituted 5-6-membered saturated, partially unsaturated, or aryl ring having 0-4 heteroatoms independently selected from nitrogen, oxygen, or sulfur.
- Suitable substituents on the aliphatic group of R * include halogen, -R*, -(haloR*), - OH, -OR*, -O(haloR'), -CN, -C(0)OH, -C(0)OR*, -NH 2 , -NHR*, -NR* 2 , or -N0 2 , wherein each R* is unsubstituted or where preceded by "halo" is substituted only with one or more halogens, and is independently Ci_ 4 aliphatic, -CH 2 Ph, -O(CH 2 ) 0 -iPh, or a 5-6- membered saturated, partially unsaturated, or aryl ring having 0-4 heteroatoms independently selected from nitrogen, oxygen, or sulfur.
- Suitable substituents on a substitutable nitrogen of an "optionally substituted" group include -R ⁇ , -NR ⁇ 2 , -C(0)R ⁇ , -C(0)OR ⁇ , -C(0)C(0)R ⁇ , -C(0)CH 2 C(0)R ⁇ , -S(0) 2 R ⁇ , -S(0) 2 NR ⁇ 2 , -C(S)NR ⁇ 2 , -C(NH)NR ⁇ 2 , or -N(R ⁇ )S(0) 2 R ⁇ ; wherein each R ⁇ is independently hydrogen, Ci_ 6 aliphatic which may be substituted as defined below, unsubstituted -OPh, or an unsubstituted 5-6-membered saturated, partially unsaturated, or aryl ring having 0-4 heteroatoms independently selected from nitrogen, oxygen, or sulfur, or, notwithstanding the definition above, two independent occurrences of R ⁇ , taken together with their intervening atom(s) form an
- Suitable substituents on the aliphatic group of R ⁇ are independently halogen, -R*, - (haloR*), -OH, -OR*, -O(haloR'), -CN, -C(0)OH, -C(0)OR*, -NH 2 , -NHR*, -NR* 2 , or -N0 2 , wherein each R* is unsubstituted or where preceded by "halo" is substituted only with one or more halogens, and is independently Ci_ 4 aliphatic, -CH 2 Ph, -0(CH 2 )o-iPh, or a 5-6-membered saturated, partially unsaturated, or aryl ring having 0-4 heteroatoms independently selected from nitrogen, oxygen, or sulfur.
- catalyst refers to a substance the presence of which increases the rate of a chemical reaction, while not being consumed or undergoing a permanent chemical change itself.
- Methods of the present invention achieve the double carbonylation of epoxides, whereby each epoxide molecule reacts with two molecules of carbon monoxide to produce an acid anhydride (e.g., a cyclic anhydride).
- the double carbonylation is facilitated by the catalysts and conditions of the present invention.
- the double carbonylation is preferably achieved in a single process using reaction conditions under which both carbonylation reactions occur without the necessity of isolating or purifying the product of the first carbonylation.
- One embodiment of the present invention encompasses catalyst/solvent combinations that enable this process to succeed in a single pot reaction format.
- the present invention provides catalysts and methods that enable the double carbonylation of epoxides to provide acid anhydride products.
- the process is a continuous process.
- the acid anhydride product is crystallizable in order to separate it from the catalyst or catalysts.
- the epoxide is ethylene oxide and the product is succinic anhydride, although the epoxide may be any epoxide that forms an acid anhydride derivative that is crystallizable.
- the epoxide may be propylene oxide, where the product is methylsuccinic anhydride.
- the catalysts described herein may be used to successfully transform epoxides into acid anhydrides in a continuous flow process.
- the transformation occurs in a single reaction (i.e. in a single reaction vessel under one set of reaction conditions).
- the reaction vessel is can be a continuous flow reaction vessel.
- the transformation occurs under continuous flow using more than one reaction vessel but without isolation of the intermediate lactone product.
- the double carbonylation occurs using a single catalyst.
- the double carbonylation uses a single catalyst for both carbonylation steps.
- two catalysts are used in which one catalyst is selected for improved performance in the first carbonylation step and the other is selected for improved performance in the second carbonylation step.
- a first catalyst is used to promote the first carbonylation
- a second catalyst different from the first catalyst is used to promote the second carbonylation.
- the catalysts and solvents are preferably chosen to optimize the reaction rate of the particular carbonylation step.
- the transformation occurs in a single continuous flow reaction vessel with controlled reaction conditions in the reaction vessel or along the length of the reaction vessel.
- the reaction conditions as the reaction stream enters the reaction vessel are different from the reaction conditions as the product stream leaves the reaction vessel such that the reaction conditions as the reaction stream enters the reaction vessel promote the first carbonylation, and the reaction conditions as the product stream leaves the reaction vessel promote the second carbonylation.
- Several aspects of the reaction conditions have been found to affect the outcome of these processes including, but not limited to, the presence of a reaction solvent, the concentration of the substrate, the amount of catalyst present, and the pressure and temperature at which the reaction is performed.
- Fig. 1 shows a process flow system for the production of succinic anhydride from ethylene oxide in a preferred embodiment of the present invention.
- the epoxide is transferred from an epoxide source, (e.g., railcars), by an offloading pump to a storage tank, where it is stored until needed.
- the epoxide is preferably ethylene oxide (EO) in this embodiment.
- the solvent (e.g., dioxane), is transferred from a solvent source (e.g., trucks), by an offloading pump to a dryer before being stored in a storage tank.
- the catalyst is stored in a mix tank.
- Carbon monoxide (CO) from a carbon monoxide source is compressed in a compressor and dried in a dryer.
- CO Carbon monoxide
- the carbon monoxide, along with hydrogen, is produced by steam reforming methane from a methane source (e.g., a pipeline).
- the hydrogen is separated, for example by pressure swing adsorption (PSA) and may be used for other purposes, for example butanediol production.
- PSA pressure swing adsorption
- the CO is purified by a further PSA prior to compression, with carbon dioxide and methane being recycled for further steam reforming.
- the solvent is supplied by a charge pump, which sends a portion of the solvent to the catalyst mix tank to form a slurry or solution. Where a slurry is produced, it may be supplied by a charge pump to combine with additional solvent to form a catalyst- solvent solution.
- the EO is supplied by a charge pump, and the CO is applied to the EO prior to mixing with the catalyst-solvent solution to form the reaction stream.
- the reaction stream is fed to a tubular or shell and tube adiabatic reactor with temperature control.
- the product stream exiting the reactor can then be sent to a separation process to isolate the acid anhydride product from the solvent, catalyst, by-products and un-reacted reactants.
- the separation can be one step or a combination of steps. Further, the separation can be a solid-liquid, liquid-liquid or liquid-gas separation.
- the product stream exiting the reactor is fed to an adiabatic evaporative cooling anhydride crystallizer including a crystallizer feed cooler followed by a crystallizer flash drum. This produces a volatiles stream and a slurry of solid succinic anhydride along with the catalyst in solvent.
- the catalyst is preferably highly soluble in the solvent such that it remains dissolved in the slurry.
- the slurry is fed to a solvent/catalyst recovery rotary drum filter, where the liquid solution is separated from the solid succinic anhydride.
- the solid succinic anhydride stream is sent to a succinic anhydride solids dryer, which is preferably a rotary kiln, from which it exits as the product.
- the volatiles stream from the crystallizer flash drum is cooled and the remaining gaseous phase is sent to a solids dryer gas heater, where it is dried and heated prior to being sent to the succinic anhydride solids dryer for drying the succinic anhydride.
- the gas stream exiting the succinic anhydride solids dryer is sent to a gas cooler prior to being fed to a solvent/catalyst recovery flash drum along with the liquid component of the cooled volatiles stream and the liquid solution exiting the dioxane/catalyst recovery rotary drum filter.
- the solvent/catalyst liquid exiting the recovery flash drum is sent by a recovery pump to the reaction stream before entering the reactor.
- the gas stream exiting the recovery flash drum is vented in part and compressed in part in a compressor and recycled back into the CO feed stream.
- the methods are generally applicable and a wide range of epoxide starting materials can be used.
- the epoxide substrates (and by extension the lactone intermediates and anhydride products) may be unsubstituted (i.e., ethylene oxide) or may be monosubstituted, vicinally disubstituted (either cis or trans).
- the methods can also be applied to geminally disubstituted, trisubstituted or tetrasubstituted epoxides though these substrates react more slowly and tend to give lower yields of anhydride.
- the substituent(s) on the epoxide can be any that is compatible with the reaction conditions described herein.
- the epoxide has the formula I: O
- R group and any other chemical variable appearing in the Schemes and structures described herein encompass those chemical moieties and functional groups that would be recognized by one having skill in the art of organic chemistry as being compatible with the structure and function of the molecules bearing those chemical variables.
- exemplary functional groups include substituted and unsubstituted cyclic and acyclic hydrocarbon moieties, substituted and unsubstituted cyclic and acyclic heteroatom-containing moieties, as well as common functional groups comprising heteroatoms, halogens, and metalloid elements. To further define the range of suitable groups certain definitions are provided below.
- a chemical variable is shown attached to a bond that crosses a bond of ring (for example as shown for R above, R d in certain ligands below, etc.), this means that one or more such variables are optionally attached to the ring having the crossed bond.
- Each R group on such a ring can be attached at any suitable position, this is generally understood to mean that the group is attached in place of a hydrogen atom on the parent ring. This includes the possibility that two R groups can be attached to the same ring atom.
- each may be the same or different than other R groups attached thereto, and each group is defined independently of other groups that may be attached elsewhere on the same molecule, even though they may be represented by the same identifier.
- each R group can be independently selected from the group consisting of: (a) Ci to C 20 alkyl; (b) C 2 to C 2 o alkenyl; (c) C 2 to C 2 o alkynyl; (d) up to a C 12 carbocycle; (e) up to a C 12 heterocycle; (f) -C(R 13 ) Z H (3 _ Z) ; and (g) a polymer chain.
- Two or more R groups may be taken together with the carbon atoms to which they are attached to form one or more rings, and any of (a) through (e) may optionally be further substituted with one or more F groups.
- F at each occurrence can be independently selected from the group consisting of: halogen; -OR 10 ; -OC(0)R 13 ; -OC(0)OR 13 ; -OC(0)NR u R 12 ; -CN; -CNO;
- R 10 at each occurrence can be independently selected from the group consisting of: - C(R 13 ) Z H(3_ Z ); Ci to C 12 alkyl; C 2 to C 12 alkenyl; C 2 to C 12 alkynyl; up to a C 12 carbocycle; up to a C 12 heterocycle; -S(0) 2 R 13 ; -Si(R 15 ) 3 ; -H; and a hydroxyl protecting group.
- R 11 and R 12 at each occurrence can be independently selected from the group consisting of: -H; Ci to C 12 alkyl; C 2 to C 12 alkenyl; C 2 to C 12 alkynyl; and -C(R 13 ) Z H (3 _ Z) .
- R 11 and R 12 when both present, can optionally be taken together with the atom to which they are attached to form a 3- to 10-membered ring.
- R 13 at each occurrence can be independently selected from the group consisting of: - H; Ci to C 12 alkyl; C 2 to C 12 alkenyl; C 2 to C 12 alkynyl; up to a C 12 carbocycle; and up to a C 12 heterocycle.
- R 14 at each occurrence can be independently selected from the group consisting of: halogen; -OR 10 ; -OC(0)R 13 ; -OC(0)OR 13 ; -OC(0)NR u R 12 ; -CN; -CNO;
- R 15 at each occurrence can be independently selected from the group consisting of: Ci to C 6 alkyl; C 2 to C 6 alkenyl; C 2 to C 6 alkynyl; and up to C 12 substituted or unsubstituted carbocycle.
- R at each occurrence can be independently selected from the group consisting of: Ci to Ci2 alkyl; C 2 to C 12 alkenyl; C 2 to C 12 alkynyl; up to a C 12 heterocycle; up to a C 12
- Z is a divalent linker and can be selected from the group consisting of:
- a can be 1, 2, 3, or 4.
- k can be an integer from 1 to 8 inclusive.
- m can be an integer from 1 to 8 inclusive.
- x can be 0, 1, or 2.
- z can be 1, 2, or 3.
- epoxides which comprise any combination of these variable definitions.
- Additional reactants can include carbon monoxide, or a mixture of carbon monoxide and another gas.
- carbon monoxide is provided in a mixture with hydrogen (e.g., Syngas).
- the ratio of carbon monoxide and hydrogen can be any ratio, including by not limited to 1 : 1, 1 :2, 1 :4, 1 : 10, 10:1, 4:1, or 2: 1.
- the carbon monoxide is provided in a mixture containing other gases.
- the carbon monoxide sources include but are not limited to: wood gas, producer gas, coal gas, town gas, manufactured gas, hygas, Dowson gas or water gas, among others.
- the carbon monoxide is provided by steam reforming from another hydrocarbon (e.g., methane) as described above.
- the carbon monoxide can be purified by pressure swing absorption to reduce the quantity of other gases in the steam reforming effluent.
- the carbon monoxide is provided at super-atmospheric pressure. The quantity of carbon monoxide should be supplied to effect efficient conversion of the epoxide starting material to an acid anhydride.
- the present invention encompasses the use of carbonylation catalysts comprising a Lewis acid in combination with a transition metal carbonyl complex.
- Lewis acid refers to any electrophilic species that is capable of accepting an electron pair and that is not a Bronsted-Lowry acid.
- the catalyst comprises a complex of formula [Lewis acid] u+ ⁇ [QT(CO)v] s" ⁇ t where Q is any ligand and need not be present; T is a transition metal; u is an integer from 1 to 6 inclusive; s is an integer from 1 to 4 inclusive; t is a number such that t multiplied by s equals u; and v is an integer from 1 to 9 inclusive.
- u and s are both 1.
- u and s are both 2.
- v is an integer from 1 to 4 inclusive.
- v is 4.
- the Lewis acid portion of the catalyst includes an element from groups 3 through 14 of the periodic table or contains a lanthanide metal.
- Useful Lewis acids may either be neutral (e.g., compounds such as A1C1 3 , CrCl 2 , CrCl 3 , ZnCl 2 , BF 3 , BC1 3 , Yb(OTf) 3 , FeCl 2 , FeCl 3 , CoCl 2 , etc.) or cationic (for instance, metal complexes of the formula [M(Z)b] c+ where M is a metal, each L is a ligand, b is an integer from 1 to 6 inclusive, and c is 1, 2, or 3, and where, if more than one L is present, each L may be the same or different).
- M is a transition metal, a group 13 or 14 metal, or a lanthanide.
- M is aluminum, chromium, indium or gallium. In some embodiments, M is aluminum or chromium.
- ligands (L) can be present in the metallo Lewis acid component of the catalyst.
- the ligand can be a dianionic tetradentate ligand.
- Suitable ligands include, but are not limited to: porphyrin derivatives 1, salen derivatives 2, dibenzotetramethyltetraaza[14]annulene (tmtaa) derivatives 3, phthalocyaninate derivatives 4, and derivatives of the Trost ligand 5.
- porphyrin, salen and tmtaa derivatives are of particular utility.
- a mixture of more than one Lewis acid component can be present in the catalyst. Exemplary definitions for the R groups appearing in structures 1 through 5 are more fully described below.
- the metal complex includes a metal M and a ligand L of formula 1 : where R d at each occurrence is independently selected from the group consisting of: H; C 1 -C 12 alkyl; C 2 -Ci 2 alkenyl; C 2 -Ci 2 alkynyl; halogen; -OR 10 ; -OC(0)R 13 ;
- -OC(0)OR 13 -OC(0)NR u R 12 ; -CN; -CNO; -C(0)R 13 ; -C(R 13 ) z H( 3 - z) ; -C(0)OR 13 ;
- R 10 , R 11 , R 12 , R 13 , R 14 , R 16 , Z, k, m, x, and z are as defined above.
- the metal complex includes a metal M and a ligand L of formula 2:
- R 1 and R 1 are independently selected from the group consisting of: -H; Ci to C 12 alkyl; C 2 to C i2 alkenyl; C 2 to C i2 alkynyl; -C(R 13 ) z H (3 _ z) ; -(CH ⁇ R 14 ; and
- R 2 , R 2' , R 3 , and R 3' are independently selected from the group consisting of: (i) C 1 -C 12 alkyl; (ii) C 2 -C 12 alkenyl; (iii) C 2 -C 12 alkynyl; (iv) up to a C 12 carbocycle; (v) up to a C12 heterocycle; (vi) -(CH 2 ) t R 14 ; (vii) R 20 ; and (viii) -C(R 13 ) Z H (3 - Z ), where each of (i) through (v) may optionally be further substituted with one or more
- R groups and where R and R , and R and R may optionally be taken together with the carbon atoms to which they are attached to form one or more rings which may in turn be substituted with one or more R 20 groups; and where R 4 is selected from the group consisting of:
- X is a divalent linker selected from the group consisting of:
- R d is as defined above, where R c at each occurrence is independently selected from the group consisting of: (a) C 1 -C 12 alkyl; (b) C 2 -Ci 2 alkenyl, (c) C 2 -Ci 2 alkynyl; (e) up to a C 12 carbocycle, (f) up to a C 12 heterocycle; (g) R 20 ; (h) -C(R 13 ) Z H (3 _ Z) ; and (i) -H, where two or more R c groups may be taken together with
- R 20 at each occurrence is independently selected from the group consisting of: -H; halogen; -OR 10 ; -OC(0)R 13 ; -OC(0)OR 13 ; -OC(0)NR n R 12 ; -CN; -CNO;
- R 1 at each occurrence is independently selected from the group consisting of: H; Ci to Ci2 alkyl; C 2 to C i2 alkenyl; C 2 to C i2 alkynyl; -C(R 13 ) z H (3 _ z) ; -(CH 2 R 14 ; and - (CH 2 ) Z-R 14 , and where R 13 , R 14 , Z, k, and z are as defined above.
- the metal complex includes a metal M and a ligand L of formula 4:
- R d is as defined above.
- the metal complex includes a metal M and a ligand L of formula 5:
- R c and R d are as defined above.
- the transition metal carbonyl complex included in the catalyst may be neutral or anionic.
- the metal carbonyl complex is anionic, e.g., monoanionic carbonyl complexes of metals from groups 5, 7 or 9 of the periodic table or dianionic carbonyl complexes of metals from groups 4 or 8 of the periodic table.
- the metal carbonyl complex contains a metal from groups 7 or 9 of the periodic table, e.g., cobalt, manganese or rhodium.
- suitable anionic metal carbonyl complexes include, but are not limited to: [Co(CO)4] ⁇ and [Mn(CO) 5 ] " . In certain embodiments [Co(CO)4] ⁇ may be used. In some cases, a mixture of two or more transition metal carbonyl complexes can be present in the catalyst.
- metal carbonyl complexes disclosed herein are generally binary metal carbonyl complexes (i.e., they have the formula M(CO) v and consist only of a metal and carbonyl ligands) this is not a limiting requirement of the present invention, and the use of mixed ligand metal carbonyl complexes is also contemplated.
- a bidentate phosphine ligand may be present along with the carbonyl ligands.
- mixed ligand carbonyl complexes may be formed in situ from the binary complexes during the reaction. Whether added or formed in situ, catalysts containing mixed ligand carbonyl complexes are encompassed by the present invention.
- the stoichiometry of the Lewis acid and the metal carbonyl complex components of the catalyst encompassed by the present invention can be varied. Typically, the two components are present in a ratio that balances the charges of the two species. For example, if the Lewis acid is a monocation and the metal carbonyl complex is a dianion, then they can be present in a charge-balancing ratio of 2: 1 (i.e., 2 [Lewis acid] + + [M(CO) x ] 2" ).
- the excess negative charge of the carbonyl complex can be balanced by the presence of a group 1 or 2 metal cation, or by a non-metallic cation such as an ammonium, phosphonium, or arsonium cation.
- the metal atom of the metallo Lewis acid can be coordinated to one or more additional neutral coordinating ligands (for instance to satisfy the metal atom's coordination valence) one such ligand that is particularly preferred is tetrahydrofuran (THF), it will be understood however that many other solvents and other ligands such as are well known in the art may also fulfill this role without departing from the present invention. It will also be realized that under reaction conditions, the coordinating ligands can be replaced by reagents, products, intermediates or solvents that may be present. Such in sz ' tw-generated species are also encompassed by the present invention. As with many catalytic processes, the structure of the specific catalyst added to the reaction will not always be the active species.
- catalysts suitable for the processes of the present invention can be formed in situ from individual components.
- the Lewis acid and the metal carbonyl complex can be added separately to the reaction vessel in which the reaction is performed.
- the catalyst instead of adding aluminum tetrakis-(4- chlorophenyl)-porphine 3zs-tetrahydrofuran tetracarbonylcobaltate (lc) as the catalyst, one can separately add aluminum tetrakis-(4-chlorophenyl)-porphine chloride and sodium tetracarbonyl cobaltate.
- catalysts combining a Lewis acid component that is cationic and a metal carbonyl complex that is anionic are particularly suitable for carbonylation processes of the present invention. It is further believed that Lewis acid/metal carbonyl combinations that have a propensity to form non-ionic associations may be less effective (for instance if a covalent or coordinate covalent bond is prone to form between the metals of the two components). In such cases it can be advantageous to add additional components that prevent this association.
- the carbonylation reaction is improved by addition of triphenylphosphine.
- the phosphine is believed to coordinate with the indium and thereby disrupt its propensity to bind to the cobaltate component of the catalyst.
- the metal carbonyl complex can be present in an excess ranging from about 2-fold to about 10- fold. If there is an excess of an anionic metal carbonyl complex relative to the Lewis acid, then the negative charge can be balanced as described above, the excess negative charge is balanced by the presence of an alkali or alkaline earth metal.
- solvents i.e., reaction solvents
- methods of the invention have been found to be improved by the presence of a solvent.
- solvents are of a low to moderate polarity.
- the solvent fully dissolves the epoxide substrate to provide a reaction mixture in which the catalyst employed is at least partially soluble. Additionally, in some aspect, the solvents lack reactive functional groups.
- the solvent includes a Lewis base.
- Lewis base refers to any nucleophilic species that is capable of donating an electron pair.
- the presence of suitable solvents can suppress the formation of polymeric side products and, in some cases, increase the rate and/or yield of the reaction.
- the Lewis base is distinct from the epoxide.
- the Lewis base is the epoxide (i.e., the reaction is performed in neat epoxide). Indeed, while the use of non-epoxide solvents may lead to higher yields, we have found that certain catalysts allow double carbonylation to be achieved in neat epoxide.
- the solvent used will fully dissolve the epoxide and provide a reaction mixture in which the catalyst employed is at least partially soluble.
- Suitable solvents may include ethers, ketones, aromatic hydrocarbons, halocarbons, esters, nitriles, and some alcohols.
- a suitable solvent may include: 1,4-dioxane; 1,3- dioxane; tetrahydrofuran; tetrahydropyran; dimethoxyethane; glyme; diethyl ether; t-butyl methyl ether; 2,5-dimethyl tetrahydrofuran; ethyl acetate; propyl acetate; butyl acetate;
- the solvent includes 1,4-dioxane, toluene, and/or dimethoxyethane.
- solvent includes 1,4-dioxane. Mixtures of two or more of the above solvents are also useful, and in some cases may be preferred to a single solvent. For example, mixtures of toluene and 1,4-dioxane are useful.
- the solvent may include a Lewis base with lower electron donicity than tetrahydrofuran.
- the solvent may include a Lewis base with lower electron donicity than 2-methyltetrahydrofuran.
- the solvent may include a Lewis base with lower electron donicity than 2,5-dimethyltetrahydrofuran.
- the solvent may include a Lewis base with higher electron donicity than difluorobenzene.
- the solvent may include a Lewis base with higher electron donicity than toluene.
- the solvent may include a Lewis base with substantially the same electron donicity as 1,4-dioxane.
- Inferior solvents include ionic liquids, chlorinated hydrocarbons, sulfolane, dimethylsulfoxide, formamide, pyridine, and the like.
- the solvent is preferably added in an amount sufficient to achieve an epoxide concentration of from about O.IM to about 20M, for example from about O.IM to about 5M or about from 0.5M to about 2M.
- the conditions for the carbonylation reaction are selected based on a number of factors to effect conversion of the epoxide to an acid anhydride. Temperature, pressure, and reaction time influence reaction speed and efficiency. Additionally, the ratio of reactants to each other and to the catalyst effect reaction speed and efficiency.
- the reaction temperature can range from between about -20 °C, to about 600 °C. In some embodiments, the reaction temperature is about -20 °C, about 0 °C, about 20 °C, about 40 °C, about 60 °C, about 80 °C, about 100 °C, about 200 °C, about 300 °C, about 400 °C, about 500 °C or about 600 °C.
- the reactants, catalyst and solvent are supplied to the reactor at standard temperature, and then heated in the reactor. In some embodiments, the reactants are pre-heated before entering the reactor. In some embodiments, the reactants are cooled before entering the reactor.
- reaction temperature was found to affect the rate and outcome of processes of the invention. At higher temperatures the reaction proceeds more quickly than at lower temperatures, but the propensity to form reaction by-products may increase.
- the reaction pressure can range from between about 50 psig to about 5000 psig. In some embodiments, the reaction pressure is about 100 psig, about 200 psig, about 300 psig, about 400 psig, about 500 psig, about 600 psig, about 700 psig, about 800 psig, about 900 psig, or about 1000 psig. In some embodiments, the pressure ranges from about 50 psig to about 2000 psig. In some embodiments, the pressure ranges from about 100 psig to 1000 psig. In some embodiments, the pressure ranges from about 200 psig to about 800 psig. In some embodiments, the reaction pressure is supplied entirely by the carbon monoxide.
- the reactants, catalyst and solvent are charged to the reactor at atmospheric pressure, or under a vacuum, and carbon monoxide is added to the reactor to increase pressure to the reaction pressure.
- carbon monoxide is added to the reactor to increase pressure to the reaction pressure.
- all reactants, solvent and catalyst are supplied to the reactor at reaction pressure.
- the atmosphere under which the reaction is conducted can include other gasses.
- Such other gasses can include, for example, hydrogen, methane, nitrogen, carbon dioxide, air, and trace amounts of steam.
- the present invention also specifically encompasses processes in which other carbon monoxide-containing gas streams provide the atmosphere under which the reaction is conducted, as described above.
- Undesirable side-product can be minimized at higher reaction temperatures by performing the reaction at relatively high carbon monoxide pressures. In some cases therefore, the optimal temperature will be dependent upon the pressure at which the reaction is conducted. At high carbon monoxide pressures, e.g., greater than about 400 psi, elevated temperatures were found to be
- the reaction may be conducted at a temperature ranging from about 40 °C to about 80 °C.
- the reaction mixture may be pressurized with CO while at a low temperature (e.g., ⁇ 0 °C) and heating is introduced only after CO has been allowed to contact the reaction mixture.
- the CO pressure may be applied for a period of time prior to heating the mixture (e.g., at least 5 minutes prior to heating).
- the ratio of catalyst to epoxide is selected, based on other reaction conditions, so that the reaction proceeds in an economical and time-feasible manner.
- the ratio of catalyst to epoxide is about 1 : 10000 on a molar basis. In some embodiments, the molar ratio of catalyst to epoxide is about 1 :5000, is about 1 :2500, is about 1 :2000, is about 1 : 1500, is about 1 : 1000, is about 1 :750, is about 1 :500, is about 1 :250, is about 1 : 200, is about 1 : 150, or is about 1 : 100. In some embodiments, the concentration of the epoxide is in the range between about 0.1 M and about 5.0 M. In some embodiments, the concentration of the epoxide is in the range between about 0.5 M and about 3.0 M.
- the catalysts may be present at a constant ratio and a constant concentration in the reaction vessel or vessels or the concentrations or ratio of the catalysts may be varied during the double carbonylation.
- the reaction stream may include predominantly only the first catalyst when it enters the reaction vessel, with the second catalyst being introduced at a later point in the process.
- the first catalyst may be predominantly separated from the intermediate lactone prior to introduction of the second catalyst to the lactone, or, alternatively, the second catalyst may be introduced to the reaction stream without separation of the first catalyst from the lactone.
- both the first catalyst and the second catalyst may be present in the reaction stream throughout the process.
- the catalyst is preferably present in an amount sufficient to allow the reaction process to be completed in a convenient time interval (e.g. less than about 24 hours, for example less than about 3 hours). In real terms this can require catalyst loadings ranging from about 0.0001 mole percent to about 20 mole percent based on the epoxide substrate. In certain embodiments, the catalyst loading can range from about 0.0001 mole percent to about 1 mole percent, e.g., from about 0.0001 mole percent to about 0.1 mole percent or from about 0.0001 mole percent to about 0.01 mole percent. In certain
- the catalyst loading can range from about 0.001 mole percent to about 20 mole percent, e.g., from about 0.1 mole percent to about 1 mole percent or from about 0.067 mole percent to about 5 mole percent. In some embodiments, the catalyst loading is less than about 0.154 mole percent based on the epoxide substrate. In one such embodiment, the epoxide is ethylene oxide.
- the carbonylation reaction is maintained for a period of time sufficient to allow complete, near complete reaction of the epoxide to acid anhydride or as complete as possible based on the reaction kinetics and or reaction conditions. In some embodiments, the reaction time is maintained for about 24 hours, about 12 hours, about 8 hours, about 6 hours, about 3 hours, about 2 hours or about 1 hour. In some embodiments, the reaction time is established as a residence time within the reactor. The reaction can be halted by reducing the reactor temperature or pressure, withdrawing a particular reactant or introducing a quenching compound. The reaction may be halted at any point or any percentage conversion of epoxide to acid anhydride.
- the catalyst or catalysts are preferably recycled from the product stream and returned to the reaction stream after being substantially separated from the acid anhydride product. In some embodiments, the catalyst remains substantially dissolved in the solvent throughout the separation and recycling. In some embodiments, the reaction product is separated by crystallization and filtration. In some embodiments, the catalyst recycling stream is further processed after separation of the product. When two or more catalysts are present, in some embodiments the catalyst recycling stream is further processed to separate the different catalysts into two or more catalyst recycling streams. The separation of the different catalysts may only produce catalyst recycling streams with different ratios of catalyst, or the separation may substantially completely separate the different catalysts. Further processing steps include, but are not limited to, feeding the recycling stream to a flash drum to separate volatiles, drying the recycling stream, heating or cooling the recycling stream, removing spent catalyst, and adding solvent.
- the separation may be accomplished by a variety of separation means, including but not limited to so lid- liquid, gas-liquid, and liquid- liquid separation techniques.
- the portion of acid anhydride product stream separated is between about 0 % and about 100% of the reaction products.
- the separation can result in a recycle stream comprising solvent and catalyst and an acid anhydride stream.
- the separation results in all or nearly all of the reaction catalyst being retained in the recycle stream.
- the temperature reduction of the second reaction product stream 300 is decrease in temperature of between 1% and about 99% from the reaction temperature (on an absolute scale). In some embodiments, the temperature of the second reaction product stream 300 is decreased by between about 1 °C and about 600 °C in the separation step 3. In some embodiments, the pressure or the partial pressure of carbon monoxide of the second reaction product stream 300 is lowered by between about 1 psig and about 5000 psig in the separation step 3.
- the separation includes adding a component to the reaction product stream. This component causes a reduction in the solubility of the acid anhydride in the stream, and results in precipitation of the acid anhydride.
- the reaction product stream is near or above the saturation point of acid anhydride at particular reaction and reactor exit conditions.
- the separation method is crystallization, filtration or sedimentation. Separation may be accomplished with a variety of techniques including but not limited to evaporative cooling crystallization, cooling crystallization, flash drums, drying, filtering and combinations of these techniques.
- the separation includes separating acid anhydride in the vapor phase (e.g., distillation, flashing, etc.,).
- separation of the acid anhydride is accomplished through liquid-liquid extraction.
- the extraction process involves partitioning the reaction product stream into two immiscible solvents. In the extraction, a portion of the acid anhydride will be partitioned into one solvent and the other solvent will contain at least the reaction catalyst. In some embodiments, after the extraction, the solvent containing acid anhydride product will be the acid anhydride product, and the stream containing the catalyst will be recycled.
- un-reacted epoxide may prevent the formation of an acid anhydride.
- the second carbonylation reaction converting the beta-lactone to acid anhydride does not proceed, unless all of the epoxide is consumed.
- the reaction product of the double carbonylation reaction is an acid anhydride.
- the product is a cyclic anhydride.
- the product is succinic anhydride, methylsuccinic anhydride,
- chloromethylsuccinic anhydride ethylsuccinic anhydride, or C 5 _ 30 acid anhydrides.
- reaction may produce by-products, and the outlet of the reactor may contain un-reacted reactants, as well as catalyst and solvent.
- un-reacted reactants include beta-lactone, epoxide or carbon monoxide.
- the reaction may not proceed to completion and may be considered a partial reaction. Examples
- the process parameters of the processes described in Fig. 1 may be modified to optimize the efficiency of the anhydride production.
- the embodiment of Fig. 1 describes illustrative and non-limiting process parameters suitable for one embodiment of the present invention.
- the solvent used is dioxane and the selected parameters are based on the efficient conversion of epoxide, separation of anhydride, and recycling of catalyst using this solvent.
- the product stream is about 99.9 wt% succinic anhydride.
- the gas stream exiting the second PSA unit is about 98.5 wt% CO, about 0.7 wt% methane, and about 0.5 wt% carbon dioxide.
- the EO, dioxane, and dioxane-catalyst slurry are fed and combined at a pressure of about 225 psia and a temperature of about 30 °C.
- the CO is applied at a pressure of about 210 psia and a temperature of about 100 °C.
- the reaction stream enters the reactor at a pressure of about 215 psia and a temperature of about 50 °C, and the product stream exits the reactor at a pressure of about 200 psia and a temperature of about 90 °C.
- the lights vented from the gas stream of the recovery flash drum contain about 3 wt% dioxane, about 21 wt% CO, about 34 wt% methane, and about 42 wt% carbon dioxide.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Materials Engineering (AREA)
- Low-Molecular Organic Synthesis Reactions Using Catalysts (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Catalysts (AREA)
- Furan Compounds (AREA)
Abstract
Description
Claims
Priority Applications (10)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US13/819,969 US9156803B2 (en) | 2010-08-28 | 2011-08-25 | Succinic anhydride from ethylene oxide |
CN201180047249.2A CN103140482B (en) | 2010-08-28 | 2011-08-25 | The succinic anhydride prepared by oxirane |
CA2809661A CA2809661A1 (en) | 2010-08-28 | 2011-08-25 | Succinic anhydride from ethylene oxide |
EP11822380.9A EP2609090A4 (en) | 2010-08-28 | 2011-08-25 | Succinic anhydride from ethylene oxide |
SG2013014824A SG188323A1 (en) | 2010-08-28 | 2011-08-25 | Succinic anhydride from ethylene oxide |
JP2013526148A JP2013536801A (en) | 2010-08-28 | 2011-08-25 | Succinic anhydride from ethylene oxide |
BR112013004870A BR112013004870A2 (en) | 2010-08-28 | 2011-08-25 | succinic ethylene oxide |
KR1020137007846A KR20130138762A (en) | 2010-08-28 | 2011-08-25 | Succinic anhydride from ethylene oxide |
ZA2013/01568A ZA201301568B (en) | 2010-08-28 | 2013-02-28 | Succinic anhydride from ethylene oxide |
US14/857,315 US20160102068A1 (en) | 2010-08-28 | 2015-09-17 | Succinic anhydride from ethylene oxide |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US37791710P | 2010-08-28 | 2010-08-28 | |
US61/377,917 | 2010-08-28 |
Related Child Applications (2)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US13/819,969 A-371-Of-International US9156803B2 (en) | 2010-08-28 | 2011-08-25 | Succinic anhydride from ethylene oxide |
US14/857,315 Division US20160102068A1 (en) | 2010-08-28 | 2015-09-17 | Succinic anhydride from ethylene oxide |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2012030619A1 true WO2012030619A1 (en) | 2012-03-08 |
Family
ID=45773209
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US2011/049125 WO2012030619A1 (en) | 2010-08-28 | 2011-08-25 | Succinic anhydride from ethylene oxide |
Country Status (11)
Country | Link |
---|---|
US (2) | US9156803B2 (en) |
EP (1) | EP2609090A4 (en) |
JP (1) | JP2013536801A (en) |
KR (1) | KR20130138762A (en) |
CN (1) | CN103140482B (en) |
BR (1) | BR112013004870A2 (en) |
CA (1) | CA2809661A1 (en) |
MY (1) | MY163064A (en) |
SG (1) | SG188323A1 (en) |
WO (1) | WO2012030619A1 (en) |
ZA (1) | ZA201301568B (en) |
Cited By (33)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2013122905A1 (en) * | 2012-02-13 | 2013-08-22 | Novomer, Inc. | Process for the production of acid anhydrides from epoxides |
WO2015138975A1 (en) | 2014-03-14 | 2015-09-17 | Novomer, Inc. | Catalysts for epoxide carbonylation |
US9156803B2 (en) | 2010-08-28 | 2015-10-13 | Novomer, Inc. | Succinic anhydride from ethylene oxide |
WO2015171372A1 (en) | 2014-05-05 | 2015-11-12 | Novomer, Inc. | Catalyst recycle methods |
WO2015184289A1 (en) | 2014-05-30 | 2015-12-03 | Novomer Inc. | Integrated methods for chemical synthesis |
WO2016130988A1 (en) | 2015-02-13 | 2016-08-18 | Novomer, Inc. | Flexible chemical production platform |
US9493391B2 (en) | 2009-04-08 | 2016-11-15 | Novomer, Inc. | Process for beta-lactone production |
US9593203B2 (en) | 2011-07-18 | 2017-03-14 | Novomer, Inc. | Metal complexes |
US9719037B2 (en) | 2015-07-01 | 2017-08-01 | Novomer, Inc. | Methods for production of terephthalic acid from ethylene oxide |
US9718755B2 (en) | 2015-07-01 | 2017-08-01 | Novomer, Inc. | Methods for coproduction of terephthalic acid and styrene from ethylene oxide |
US9771388B2 (en) | 2012-08-24 | 2017-09-26 | Saudi Aramco Technologies Company | Metal complexes |
US9914689B2 (en) | 2011-10-26 | 2018-03-13 | Novomer, Inc. | Process for production of acrylates from epoxides |
US10099989B2 (en) | 2015-02-13 | 2018-10-16 | Novomer, Inc. | Distillation process for production of acrylic acid |
US10099988B2 (en) | 2015-02-13 | 2018-10-16 | Novomer, Inc. | Process for production of acrylic acid |
US10221150B2 (en) | 2015-02-13 | 2019-03-05 | Novomer, Inc. | Continuous carbonylation processes |
US10221278B2 (en) | 2011-05-13 | 2019-03-05 | Novomer, Inc. | Catalytic carbonylation catalysts and methods |
US10428165B2 (en) | 2015-02-13 | 2019-10-01 | Novomer, Inc. | Systems and processes for polyacrylic acid production |
US10457624B2 (en) | 2017-04-24 | 2019-10-29 | Novomer, Inc. | Systems and processes for thermolysis of polylactones to produce organic acids |
US10500104B2 (en) | 2016-12-06 | 2019-12-10 | Novomer, Inc. | Biodegradable sanitary articles with higher biobased content |
US10590099B1 (en) | 2017-08-10 | 2020-03-17 | Novomer, Inc. | Processes for producing beta-lactone with heterogenous catalysts |
US10662139B2 (en) | 2016-03-21 | 2020-05-26 | Novomer, Inc. | Acrylic acid production process |
US10662283B2 (en) | 2015-02-13 | 2020-05-26 | Novomer, Inc. | Process and system for production of polypropiolactone |
US10669373B2 (en) | 2016-12-05 | 2020-06-02 | Novomer, Inc. | Beta-propiolactone based copolymers containing biogenic carbon, methods for their production and uses thereof |
US10676426B2 (en) | 2017-06-30 | 2020-06-09 | Novomer, Inc. | Acrylonitrile derivatives from epoxide and carbon monoxide reagents |
US10683390B2 (en) | 2015-02-13 | 2020-06-16 | Novomer, Inc. | Systems and processes for polymer production |
US10703702B2 (en) | 2015-07-31 | 2020-07-07 | Novomer, Inc. | Production system/production process for acrylic acid and precursors thereof |
US10711095B2 (en) | 2016-03-21 | 2020-07-14 | Novomer, Inc. | Systems and methods for producing superabsorbent polymers |
US10974234B2 (en) | 2014-07-25 | 2021-04-13 | Novomer, Inc. | Synthesis of metal complexes and uses thereof |
US11027242B2 (en) | 2013-12-07 | 2021-06-08 | Novomer, Inc. | Nanofiltration membranes and methods of use |
US11078172B2 (en) | 2015-02-13 | 2021-08-03 | Novomer, Inc. | Integrated methods for chemical synthesis |
US11351519B2 (en) | 2016-11-02 | 2022-06-07 | Novomer, Inc. | Absorbent polymers, and methods and systems of producing thereof and uses thereof |
US11498894B2 (en) | 2019-03-08 | 2022-11-15 | Novomer, Inc. | Integrated methods and systems for producing amide and nitrile compounds |
US11814498B2 (en) | 2018-07-13 | 2023-11-14 | Novomer, Inc. | Polylactone foams and methods of making the same |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9403861B2 (en) * | 2011-12-11 | 2016-08-02 | Novomer, Inc. | Salen complexes with dianionic counterions |
EP3114103A4 (en) | 2014-03-04 | 2018-01-17 | White Dog Labs, Inc. | Energy efficient batch recycle method for the production of biomolecules |
AR110833A1 (en) * | 2017-01-19 | 2019-05-08 | Novomer Inc | METHODS AND SYSTEMS FOR THE TREATMENT OF ETHYLENE OXIDE |
EP3691785A4 (en) | 2017-10-05 | 2021-08-04 | Novomer, Inc. | Isocyanates, derivatives, and processes for producing the same |
CN109896996A (en) * | 2019-02-28 | 2019-06-18 | 凯莱英生命科学技术(天津)有限公司 | Organic carboxyl acid is continuously synthesizing to method |
KR20210134914A (en) | 2019-03-18 | 2021-11-11 | 노보머, 인코포레이티드 | Membrane separation systems and uses thereof |
JP2024507694A (en) * | 2021-01-29 | 2024-02-21 | ノボマー, インコーポレイテッド | Improved reactor and method for reacting gaseous and liquid reactants |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2245404A (en) * | 1939-02-03 | 1941-06-10 | Solvay Process Co | Manufacture of succinic anhydride |
US5096470A (en) * | 1990-12-05 | 1992-03-17 | The Boc Group, Inc. | Hydrogen and carbon monoxide production by hydrocarbon steam reforming and pressure swing adsorption purification |
US6773578B1 (en) * | 2000-12-05 | 2004-08-10 | Chevron U.S.A. Inc. | Process for preparing lubes with high viscosity index values |
Family Cites Families (17)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
BE559038A (en) * | 1956-07-09 | |||
US3813428A (en) * | 1968-08-15 | 1974-05-28 | Monsanto Co | Production of monocarboxylic acids |
US4079116A (en) * | 1976-12-27 | 1978-03-14 | Amax Inc. | Process for producing ammonium heptamolybdate and/or ammonium dimolybdate |
DE3612213A1 (en) * | 1986-04-11 | 1987-10-15 | Basf Ag | TUBE BUNCH REACTOR, THEIR USE IN EXOTHERMAL ORGANIC REACTIONS AND METHOD FOR THE PRODUCTION OF KETONES AND ALDEHYDES WITH THE AID OF THE TUBE BUNCH REACTOR |
US5110984A (en) * | 1990-11-06 | 1992-05-05 | Amoco Corporation | Process for increasing the yield of purified isophthalic acid and reducing waste-water treatment a |
US6054610A (en) * | 1995-06-07 | 2000-04-25 | Hfm International, Inc. | Method and apparatus for preparing purified terephthalic acid and isophthalic acid from mixed xylenes |
US5980857A (en) * | 1998-03-18 | 1999-11-09 | The Boc Group, Inc. | Production of carbon monoxide from syngas |
US6191321B1 (en) * | 1998-09-30 | 2001-02-20 | Shell Oil Company | Process for preparing 1,3-propanediol from methyl 3-hydroxypropionate |
ES2225112T3 (en) * | 1999-03-22 | 2005-03-16 | Purac Biochem Bv | PROCESSING PURIFICATION OF LACTIC ACID AT INDUSTRIAL SCALE. |
US6747171B2 (en) * | 2000-02-03 | 2004-06-08 | Bp Corporation North America Inc. | Low temperature purification of naphthalene dicarboxylic acids |
WO2003050154A2 (en) * | 2001-12-06 | 2003-06-19 | Cornell Research Foundation, Inc. | Catalytic carbonylation of three and four membered heterocycles |
EP1615901A1 (en) | 2003-04-09 | 2006-01-18 | Shell Internationale Researchmaatschappij B.V. | Carbonylation of epoxides |
IN2015DN00761A (en) * | 2004-09-02 | 2015-07-10 | Grupo Petrotemex Sa De Cv | |
US7569709B2 (en) | 2006-03-10 | 2009-08-04 | Cornell Research Foundation, Inc. | Low pressure carbonylation of heterocycles |
US8481756B1 (en) * | 2007-09-04 | 2013-07-09 | Cornell Research Foundation, Inc. | Succinic anhydrides from epoxides |
SG175132A1 (en) | 2009-04-08 | 2011-11-28 | Novomer Inc | Process for beta-lactone production |
SG188323A1 (en) | 2010-08-28 | 2013-04-30 | Novomer Inc | Succinic anhydride from ethylene oxide |
-
2011
- 2011-08-25 SG SG2013014824A patent/SG188323A1/en unknown
- 2011-08-25 US US13/819,969 patent/US9156803B2/en active Active
- 2011-08-25 CN CN201180047249.2A patent/CN103140482B/en active Active
- 2011-08-25 JP JP2013526148A patent/JP2013536801A/en active Pending
- 2011-08-25 WO PCT/US2011/049125 patent/WO2012030619A1/en active Application Filing
- 2011-08-25 EP EP11822380.9A patent/EP2609090A4/en not_active Ceased
- 2011-08-25 BR BR112013004870A patent/BR112013004870A2/en not_active Application Discontinuation
- 2011-08-25 CA CA2809661A patent/CA2809661A1/en not_active Abandoned
- 2011-08-25 KR KR1020137007846A patent/KR20130138762A/en not_active Application Discontinuation
- 2011-08-25 MY MYPI2013000688A patent/MY163064A/en unknown
-
2013
- 2013-02-28 ZA ZA2013/01568A patent/ZA201301568B/en unknown
-
2015
- 2015-09-17 US US14/857,315 patent/US20160102068A1/en not_active Abandoned
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US2245404A (en) * | 1939-02-03 | 1941-06-10 | Solvay Process Co | Manufacture of succinic anhydride |
US5096470A (en) * | 1990-12-05 | 1992-03-17 | The Boc Group, Inc. | Hydrogen and carbon monoxide production by hydrocarbon steam reforming and pressure swing adsorption purification |
US6773578B1 (en) * | 2000-12-05 | 2004-08-10 | Chevron U.S.A. Inc. | Process for preparing lubes with high viscosity index values |
Non-Patent Citations (2)
Title |
---|
ROWLEY ET AL.: "Catalytic Double Carbonylation of Epoxides to Succinic Anhydrides: Catalyst Discovery, Reaction Scope, and Mechanism", JOURNAL OF AMERICAN CHEMICAL SOC OCIETY, vol. 129, 31 March 2007 (2007-03-31), pages 4948 - 4960, XP055076024 * |
See also references of EP2609090A4 * |
Cited By (53)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9493391B2 (en) | 2009-04-08 | 2016-11-15 | Novomer, Inc. | Process for beta-lactone production |
US9156803B2 (en) | 2010-08-28 | 2015-10-13 | Novomer, Inc. | Succinic anhydride from ethylene oxide |
US10221278B2 (en) | 2011-05-13 | 2019-03-05 | Novomer, Inc. | Catalytic carbonylation catalysts and methods |
US10479861B2 (en) | 2011-05-13 | 2019-11-19 | Novomer, Inc. | Catalytic carbonylation catalysts and methods |
US9593203B2 (en) | 2011-07-18 | 2017-03-14 | Novomer, Inc. | Metal complexes |
US9914689B2 (en) | 2011-10-26 | 2018-03-13 | Novomer, Inc. | Process for production of acrylates from epoxides |
US9403788B2 (en) | 2012-02-13 | 2016-08-02 | Novomer, Inc. | Process for the production of acid anhydrides from epoxides |
WO2013122905A1 (en) * | 2012-02-13 | 2013-08-22 | Novomer, Inc. | Process for the production of acid anhydrides from epoxides |
US9771388B2 (en) | 2012-08-24 | 2017-09-26 | Saudi Aramco Technologies Company | Metal complexes |
US11027242B2 (en) | 2013-12-07 | 2021-06-08 | Novomer, Inc. | Nanofiltration membranes and methods of use |
WO2015138975A1 (en) | 2014-03-14 | 2015-09-17 | Novomer, Inc. | Catalysts for epoxide carbonylation |
US11667617B2 (en) | 2014-05-05 | 2023-06-06 | Novomer, Inc. | Catalyst recycle methods |
WO2015171372A1 (en) | 2014-05-05 | 2015-11-12 | Novomer, Inc. | Catalyst recycle methods |
US10858329B2 (en) | 2014-05-05 | 2020-12-08 | Novomer, Inc. | Catalyst recycle methods |
WO2015184289A1 (en) | 2014-05-30 | 2015-12-03 | Novomer Inc. | Integrated methods for chemical synthesis |
US10829372B2 (en) | 2014-05-30 | 2020-11-10 | Novomer, Inc. | Integrated methods for chemical synthesis |
US10597294B2 (en) | 2014-05-30 | 2020-03-24 | Novomer, Inc. | Integrated methods for chemical synthesis |
US10974234B2 (en) | 2014-07-25 | 2021-04-13 | Novomer, Inc. | Synthesis of metal complexes and uses thereof |
US10099989B2 (en) | 2015-02-13 | 2018-10-16 | Novomer, Inc. | Distillation process for production of acrylic acid |
US11401358B2 (en) | 2015-02-13 | 2022-08-02 | Novomer, Inc. | Method of converting ethylene to polyacrylic acid (PAA) and superabsorbent polymer (SAP) within an integrated system |
US12037447B2 (en) | 2015-02-13 | 2024-07-16 | Novomer, Inc. | Systems and processes for polymer production |
US11807613B2 (en) | 2015-02-13 | 2023-11-07 | Novomer, Inc. | Integrated methods for chemical synthesis |
US10428165B2 (en) | 2015-02-13 | 2019-10-01 | Novomer, Inc. | Systems and processes for polyacrylic acid production |
US10626073B2 (en) | 2015-02-13 | 2020-04-21 | Novomer, Inc. | Process for production of acrylic acid |
WO2016130988A1 (en) | 2015-02-13 | 2016-08-18 | Novomer, Inc. | Flexible chemical production platform |
US10662283B2 (en) | 2015-02-13 | 2020-05-26 | Novomer, Inc. | Process and system for production of polypropiolactone |
US11492443B2 (en) | 2015-02-13 | 2022-11-08 | Novomer, Inc. | Process and system for production of polypropiolactone |
US11420177B2 (en) | 2015-02-13 | 2022-08-23 | Novomer, Inc. | Flexible chemical production method |
US10683390B2 (en) | 2015-02-13 | 2020-06-16 | Novomer, Inc. | Systems and processes for polymer production |
US11155511B2 (en) | 2015-02-13 | 2021-10-26 | Novomer, Inc. | Distillation process for production of acrylic acid |
US11078172B2 (en) | 2015-02-13 | 2021-08-03 | Novomer, Inc. | Integrated methods for chemical synthesis |
US10717695B2 (en) | 2015-02-13 | 2020-07-21 | Novomer, Inc. | Distillation process for production of acrylic acid |
US10738022B2 (en) | 2015-02-13 | 2020-08-11 | Novomer, Inc. | Continuous carbonylation processes |
US10822436B2 (en) | 2015-02-13 | 2020-11-03 | Novomer, Inc. | Systems and processes for polyacrylic acid production |
US10221150B2 (en) | 2015-02-13 | 2019-03-05 | Novomer, Inc. | Continuous carbonylation processes |
US10099988B2 (en) | 2015-02-13 | 2018-10-16 | Novomer, Inc. | Process for production of acrylic acid |
EP3757088A1 (en) | 2015-02-13 | 2020-12-30 | Novomer, Inc. | Flexible chemical production platform |
US10927091B2 (en) | 2015-02-13 | 2021-02-23 | Novomer, Inc. | Continuous carbonylation processes |
US9718755B2 (en) | 2015-07-01 | 2017-08-01 | Novomer, Inc. | Methods for coproduction of terephthalic acid and styrene from ethylene oxide |
US9719037B2 (en) | 2015-07-01 | 2017-08-01 | Novomer, Inc. | Methods for production of terephthalic acid from ethylene oxide |
US10703702B2 (en) | 2015-07-31 | 2020-07-07 | Novomer, Inc. | Production system/production process for acrylic acid and precursors thereof |
US10711095B2 (en) | 2016-03-21 | 2020-07-14 | Novomer, Inc. | Systems and methods for producing superabsorbent polymers |
US11827590B2 (en) | 2016-03-21 | 2023-11-28 | Novomer, Inc. | Acrylic acid, and methods of producing thereof |
US10662139B2 (en) | 2016-03-21 | 2020-05-26 | Novomer, Inc. | Acrylic acid production process |
US11351519B2 (en) | 2016-11-02 | 2022-06-07 | Novomer, Inc. | Absorbent polymers, and methods and systems of producing thereof and uses thereof |
US11655333B2 (en) | 2016-12-05 | 2023-05-23 | Novomer, Inc. | Beta-propiolactone based copolymers containing biogenic carbon, methods for their production and uses thereof |
US10669373B2 (en) | 2016-12-05 | 2020-06-02 | Novomer, Inc. | Beta-propiolactone based copolymers containing biogenic carbon, methods for their production and uses thereof |
US10500104B2 (en) | 2016-12-06 | 2019-12-10 | Novomer, Inc. | Biodegradable sanitary articles with higher biobased content |
US10457624B2 (en) | 2017-04-24 | 2019-10-29 | Novomer, Inc. | Systems and processes for thermolysis of polylactones to produce organic acids |
US10676426B2 (en) | 2017-06-30 | 2020-06-09 | Novomer, Inc. | Acrylonitrile derivatives from epoxide and carbon monoxide reagents |
US10590099B1 (en) | 2017-08-10 | 2020-03-17 | Novomer, Inc. | Processes for producing beta-lactone with heterogenous catalysts |
US11814498B2 (en) | 2018-07-13 | 2023-11-14 | Novomer, Inc. | Polylactone foams and methods of making the same |
US11498894B2 (en) | 2019-03-08 | 2022-11-15 | Novomer, Inc. | Integrated methods and systems for producing amide and nitrile compounds |
Also Published As
Publication number | Publication date |
---|---|
US20130165670A1 (en) | 2013-06-27 |
ZA201301568B (en) | 2016-02-24 |
JP2013536801A (en) | 2013-09-26 |
EP2609090A1 (en) | 2013-07-03 |
US9156803B2 (en) | 2015-10-13 |
CN103140482A (en) | 2013-06-05 |
MY163064A (en) | 2017-08-15 |
EP2609090A4 (en) | 2013-12-25 |
BR112013004870A2 (en) | 2016-05-03 |
US20160102068A1 (en) | 2016-04-14 |
CA2809661A1 (en) | 2012-03-08 |
CN103140482B (en) | 2017-03-29 |
KR20130138762A (en) | 2013-12-19 |
SG188323A1 (en) | 2013-04-30 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US9156803B2 (en) | Succinic anhydride from ethylene oxide | |
US9403788B2 (en) | Process for the production of acid anhydrides from epoxides | |
US11492443B2 (en) | Process and system for production of polypropiolactone | |
US9493391B2 (en) | Process for beta-lactone production | |
EP2707353B1 (en) | Carbonylation catalysts and method | |
WO2018200471A1 (en) | Systems and processes for thermolysis of polylactones to produce organic acids | |
EP2867189A2 (en) | Process for acrylate production | |
WO2013138243A1 (en) | Bifunctional compounds | |
WO2013033209A1 (en) | Poly (hydroxy alkanoate) co-polymers |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 201180047249.2 Country of ref document: CN |
|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 11822380 Country of ref document: EP Kind code of ref document: A1 |
|
DPE1 | Request for preliminary examination filed after expiration of 19th month from priority date (pct application filed from 20040101) | ||
ENP | Entry into the national phase |
Ref document number: 2013526148 Country of ref document: JP Kind code of ref document: A Ref document number: 2809661 Country of ref document: CA |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
WWE | Wipo information: entry into national phase |
Ref document number: 13819969 Country of ref document: US |
|
REEP | Request for entry into the european phase |
Ref document number: 2011822380 Country of ref document: EP |
|
WWE | Wipo information: entry into national phase |
Ref document number: 2011822380 Country of ref document: EP |
|
ENP | Entry into the national phase |
Ref document number: 20137007846 Country of ref document: KR Kind code of ref document: A |
|
REG | Reference to national code |
Ref country code: BR Ref legal event code: B01A Ref document number: 112013004870 Country of ref document: BR |
|
ENP | Entry into the national phase |
Ref document number: 112013004870 Country of ref document: BR Kind code of ref document: A2 Effective date: 20130228 |