WO2013155270A2 - Catalysts for the conversion of hydroxypropionic acid or its derivatives to acrylic acid or its derivatives - Google Patents

Catalysts for the conversion of hydroxypropionic acid or its derivatives to acrylic acid or its derivatives Download PDF

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Publication number
WO2013155270A2
WO2013155270A2 PCT/US2013/036127 US2013036127W WO2013155270A2 WO 2013155270 A2 WO2013155270 A2 WO 2013155270A2 US 2013036127 W US2013036127 W US 2013036127W WO 2013155270 A2 WO2013155270 A2 WO 2013155270A2
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WO
WIPO (PCT)
Prior art keywords
catalyst
mixtures
cations
phosphorus
acrylic acid
Prior art date
Application number
PCT/US2013/036127
Other languages
English (en)
French (fr)
Other versions
WO2013155270A9 (en
WO2013155270A3 (en
Inventor
Juan Esteban VELASQUEZ
Janette Villalobos LINGOES
Jane Ellen Godlewski
Dimitris Ioannis Collias
Fred C. WIREKO
Marc Andrew Mamak
Nancy Lee Redman-Furey
Original Assignee
The Procter & Gamble Company
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by The Procter & Gamble Company filed Critical The Procter & Gamble Company
Priority to CN201380002860.2A priority Critical patent/CN103764281A/zh
Priority to MX2014011396A priority patent/MX373258B/es
Priority to BR112014025359-5A priority patent/BR112014025359B1/pt
Priority to EP13719327.2A priority patent/EP2836300B1/en
Priority to IN8015DEN2014 priority patent/IN2014DN08015A/en
Priority to SG11201405711YA priority patent/SG11201405711YA/en
Priority to CA2869677A priority patent/CA2869677C/en
Priority to RU2014136558/04A priority patent/RU2591192C2/ru
Priority to ES13719327.2T priority patent/ES2611360T3/es
Priority to AU2013245925A priority patent/AU2013245925B2/en
Priority to JP2014530978A priority patent/JP5770942B2/ja
Publication of WO2013155270A2 publication Critical patent/WO2013155270A2/en
Publication of WO2013155270A3 publication Critical patent/WO2013155270A3/en
Publication of WO2013155270A9 publication Critical patent/WO2013155270A9/en

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
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    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/14—Phosphorus; Compounds thereof
    • B01J27/16—Phosphorus; Compounds thereof containing oxygen, i.e. acids, anhydrides and their derivates with N, S, B or halogens without carriers or on carriers based on C, Si, Al or Zr; also salts of Si, Al and Zr
    • B01J27/18—Phosphorus; Compounds thereof containing oxygen, i.e. acids, anhydrides and their derivates with N, S, B or halogens without carriers or on carriers based on C, Si, Al or Zr; also salts of Si, Al and Zr with metals other than Al or Zr
    • B01J27/1802—Salts or mixtures of anhydrides with compounds of other metals than V, Nb, Ta, Cr, Mo, W, Mn, Tc, Re, e.g. phosphates, thiophosphates
    • B01J27/1806—Salts or mixtures of anhydrides with compounds of other metals than V, Nb, Ta, Cr, Mo, W, Mn, Tc, Re, e.g. phosphates, thiophosphates with alkaline or alkaline earth metals
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61F—FILTERS IMPLANTABLE INTO BLOOD VESSELS; PROSTHESES; DEVICES PROVIDING PATENCY TO, OR PREVENTING COLLAPSING OF, TUBULAR STRUCTURES OF THE BODY, e.g. STENTS; ORTHOPAEDIC, NURSING OR CONTRACEPTIVE DEVICES; FOMENTATION; TREATMENT OR PROTECTION OF EYES OR EARS; BANDAGES, DRESSINGS OR ABSORBENT PADS; FIRST-AID KITS
    • A61F13/00—Bandages or dressings; Absorbent pads
    • A61F13/15—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators
    • A61F13/53—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators characterised by the absorbing medium
    • A61F13/534—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators characterised by the absorbing medium having an inhomogeneous composition through the thickness of the pad
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    • B01J27/18—Phosphorus; Compounds thereof containing oxygen, i.e. acids, anhydrides and their derivates with N, S, B or halogens without carriers or on carriers based on C, Si, Al or Zr; also salts of Si, Al and Zr with metals other than Al or Zr
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    • B01J27/1802—Salts or mixtures of anhydrides with compounds of other metals than V, Nb, Ta, Cr, Mo, W, Mn, Tc, Re, e.g. phosphates, thiophosphates
    • B01J27/1817—Salts or mixtures of anhydrides with compounds of other metals than V, Nb, Ta, Cr, Mo, W, Mn, Tc, Re, e.g. phosphates, thiophosphates with copper, silver or gold
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    • A61F13/53—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators characterised by the absorbing medium
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61F—FILTERS IMPLANTABLE INTO BLOOD VESSELS; PROSTHESES; DEVICES PROVIDING PATENCY TO, OR PREVENTING COLLAPSING OF, TUBULAR STRUCTURES OF THE BODY, e.g. STENTS; ORTHOPAEDIC, NURSING OR CONTRACEPTIVE DEVICES; FOMENTATION; TREATMENT OR PROTECTION OF EYES OR EARS; BANDAGES, DRESSINGS OR ABSORBENT PADS; FIRST-AID KITS
    • A61F13/00—Bandages or dressings; Absorbent pads
    • A61F13/15—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators
    • A61F13/53—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators characterised by the absorbing medium
    • A61F2013/530481—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators characterised by the absorbing medium having superabsorbent materials, i.e. highly absorbent polymer gel materials
    • A61F2013/530489—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators characterised by the absorbing medium having superabsorbent materials, i.e. highly absorbent polymer gel materials being randomly mixed in with other material
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61F—FILTERS IMPLANTABLE INTO BLOOD VESSELS; PROSTHESES; DEVICES PROVIDING PATENCY TO, OR PREVENTING COLLAPSING OF, TUBULAR STRUCTURES OF THE BODY, e.g. STENTS; ORTHOPAEDIC, NURSING OR CONTRACEPTIVE DEVICES; FOMENTATION; TREATMENT OR PROTECTION OF EYES OR EARS; BANDAGES, DRESSINGS OR ABSORBENT PADS; FIRST-AID KITS
    • A61F13/00—Bandages or dressings; Absorbent pads
    • A61F13/15—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators
    • A61F13/53—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators characterised by the absorbing medium
    • A61F2013/530481—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators characterised by the absorbing medium having superabsorbent materials, i.e. highly absorbent polymer gel materials
    • A61F2013/530489—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators characterised by the absorbing medium having superabsorbent materials, i.e. highly absorbent polymer gel materials being randomly mixed in with other material
    • A61F2013/530496—Absorbent pads, e.g. sanitary towels, swabs or tampons for external or internal application to the body; Supporting or fastening means therefor; Tampon applicators characterised by the absorbing medium having superabsorbent materials, i.e. highly absorbent polymer gel materials being randomly mixed in with other material being fixed to fibres
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
    • B01J2523/10—Constitutive chemical elements of heterogeneous catalysts of Group I (IA or IB) of the Periodic Table
    • B01J2523/12—Sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
    • B01J2523/10—Constitutive chemical elements of heterogeneous catalysts of Group I (IA or IB) of the Periodic Table
    • B01J2523/13—Potassium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
    • B01J2523/20—Constitutive chemical elements of heterogeneous catalysts of Group II (IIA or IIB) of the Periodic Table
    • B01J2523/23—Calcium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
    • B01J2523/20—Constitutive chemical elements of heterogeneous catalysts of Group II (IIA or IIB) of the Periodic Table
    • B01J2523/25—Barium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2523/00—Constitutive chemical elements of heterogeneous catalysts
    • B01J2523/50—Constitutive chemical elements of heterogeneous catalysts of Group V (VA or VB) of the Periodic Table
    • B01J2523/51—Phosphorus

Definitions

  • the present invention generally relates to catalysts useful for the conversion of hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof to acrylic acid, acrylic acid derivatives, or mixtures thereof. More specifically, the invention relates to catalysts useful for the dehydration of hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof to acrylic acid, acrylic acid derivatives, or mixtures thereof with high yield and selectivity to acrylic acid, acrylic acid derivatives, or mixtures thereof, short residence time, and without significant conversion of the hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof to undesired side products, such as, for example, acetaldehyde, propionic acid, acetic acid, 2,3-pentanedione, carbon dioxide, and carbon monoxide.
  • undesired side products such as, for example, acetaldehyde, propionic acid, acetic acid, 2,3-pentanedione, carbon dioxide, and carbon monoxide.
  • Acrylic acid, acrylic acid derivatives, or mixtures thereof have a variety of industrial uses, typically consumed in the form of polymers.
  • these polymers are commonly used in the manufacture of, among other things, adhesives, binders, coatings, paints, polishes, detergents, flocculants, dispersants, thixotropic agents, sequestrants, and superabsorbent polymers, which are used in disposable absorbent articles, including diapers and hygienic products, for example.
  • Acrylic acid is commonly made from petroleum sources. For example, acrylic acid has long been prepared by catalytic oxidation of propylene. These and other methods of making acrylic acid from petroleum sources are described in the Kirk-Othmer Encyclopedia of Chemical Technology, Vol. 1, pgs.
  • Petroleum-based acrylic acid contributes to greenhouse emissions due to its high petroleum derived carbon content. Furthermore, petroleum is a non-renewable material, as it takes hundreds of thousands of years to form naturally and only a short time to consume. As petrochemical resources become increasingly scarce, more expensive, and subject to regulations for C0 2 emissions, there exists a growing need for bio-based acrylic acid, acrylic acid derivatives, or mixtures thereof that can serve as an alternative to petroleum-based acrylic acid, acrylic acid derivatives, or mixtures thereof.
  • lactic acid or lactate presents a real opportunity of serving as a feedstock for bio-based acrylic acid, acrylic acid derivatives, or mixtures thereof.
  • 3-hydroxypropionic acid is expected to be produced at commercial scale in a few years, and as such, 3-hydropropionic acid will present another real opportunity of serving as feedstock for bio-based acrylic acid, acrylic acid derivatives, or mixtures thereof.
  • Sulfate salts; phosphate salts; mixtures of sulfate and phosphate salts; bases; zeolites or modified zeolites; metal oxides or modified metal oxides; and supercritical water are the main catalysts which have been used to dehydrate lactic acid or lactate to acrylic acid, acrylic acid derivatives, or mixtures thereof in the past with varying success.
  • U.S. Patent No. 4,786,756 (issued in 1988), describes the vapor phase dehydration of lactic acid or ammonium lactate to acrylic acid using aluminum phosphate (AIPO 4 ) treated with an aqueous inorganic base as a catalyst.
  • AIPO 4 aluminum phosphate
  • the '756 patent discloses a maximum yield of acrylic acid of 43.3% when lactic acid was fed into the reactor at approximately atmospheric pressure, and a respective yield of 61.1% when ammonium lactate was fed into the reactor.
  • acetaldehyde was produced at yields of 34.7% and 11.9%, respectively, and other side products were also present in large quantities, such as, propionic acid, CO, and C0 2 .
  • Examples of other catalysts tested by the group were Na 2 S0 4 , NaCl, Na 3 P0 4 , NaNC>3, Na 2 Si0 3 , Na 4 P 2 0 7 , NaH 2 P0 4 , Na 2 HP0 4 , Na 2 HAs0 4 , NaC 3 H 5 0 3 , NaOH, CsCl, Cs 2 S0 4 , KOH, CsOH, and LiOH.
  • the above referenced catalysts were tested as individual components, not in mixtures.
  • the group suggested that the yield to acrylic acid is improved and the yield to the side products is suppressed when the surface area of the silica support is low, reaction temperature is high, reaction pressure is low, and residence time of the reactants in the catalyst bed is short.
  • the Chinese patent application 200910054519.7 discloses the use of ZSM-5 molecular sieves modified with aqueous alkali (such as, NH 3 , NaOH, and Na 2 C0 3 ) or a phosphoric acid salt (such as, NaH 2 P0 4 , Na 2 HP0 4 , LiH 2 P0 4 , LaP0 4 , etc.).
  • aqueous alkali such as, NH 3 , NaOH, and Na 2 C0 3
  • a phosphoric acid salt such as, NaH 2 P0 4 , Na 2 HP0 4 , LiH 2 P0 4 , LaP0 4 , etc.
  • these side products can catalyze other undesired reactions, such as polymerization reactions. Aside from depositing on the catalysts, these side products, even when present in only small amounts, impose additional costs in processing acrylic acid (when present in the reaction product effluent) in the manufacture of superabsorbent polymers (SAP), for example.
  • SAP superabsorbent polymers
  • a catalyst for dehydrating hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof to acrylic acid, acrylic acid derivatives, or mixtures thereof is provided.
  • the catalyst includes: (a) at least one condensed phosphate anion selected from the group consisting of formulae (I), (II), and (III),
  • n is at least 2 and m is at least 1, and (b) at least two different cations, wherein the catalyst is essentially neutrally charged, and further, wherein the molar ratio of phosphorus to the at least two different cations is between about 0.7 and about 1.7.
  • the anions defined by formulae (I), (II), and (III) are also referred to as polyphosphates (or oligophosphates), cyclophosphates, and ultraphosphates, respectively.
  • a method of preparing the catalyst includes mixing and heating at least two different phosphorus containing compounds, wherein each said compound is described by one of the formulae (IV) to (XXV), or any of the hydrated forms of said formulae:
  • a method of preparing the catalyst includes mixing and heating: (a) at least one phosphorus containing compound, wherein each said compound is described by one of the formulae (IV) to (XXV), or any of the hydrated forms of said formulae:
  • a method of preparing a catalyst including the following steps: (a) combining a phosphorus containing compound, a nitrate salt, phosphoric acid, and water to form a wet mixture, wherein the molar ratio between phosphorus and the cations in both the phosphorus containing compound and nitrate salt is about 1, (b) calcining said wet mixture stepwise at about 50°C, about 80°C, about 120°C, and about 450°C to about 550°C to produce a dried solid, and (c) grinding and sieving said dried solid to about 100 ⁇ to about 200 ⁇ , to produce said catalyst.
  • a method of preparing a catalyst including: (a) combining Ca 2 P 2 C>7 and KH 2 P0 4 in a molar ratio of about 3: 1 to form a solid mixture, and (b) calcining said solid mixture stepwise at about 50°C, about 80°C, about 120°C, and about 450°C to about 550°C, to produce said catalyst.
  • the term "monophosphate” or “orthophosphate” refers to any salt whose anionic entity, [P0 4 ] 3" , is composed of four oxygen atoms arranged in an almost regular tetrahedral array about a central phosphorus atom.
  • condensed phosphate refers to any salts containing one or several P-O-P bonds generated by corner sharing of P0 4 tetrahedra.
  • polyphosphate refers to any condensed phosphates containing linear P-O-P linkages by corner sharing of P0 4 tetrahedra leading to the formation of finite chains.
  • oligophosphate refers to any polyphosphates that contain five or less P0 4 units.
  • cyclophosphate refers to any cyclic condensed phosphate constituted of two or more corner-sharing P0 4 tetrahedra.
  • ultraphosphate refers to any condensed phosphate where at least two PO 4 tetrahedra of the anionic entity share three of their corners with the adjacent ones.
  • cation refers to any atom or group of covalently-bonded atoms having a positive charge.
  • anion refers to any atom or group of covalently-bonded atoms having a negative charge.
  • the term "monovalent cation" refers to any cation with a positive charge of
  • polyvalent cation refers to any cation with a positive charge equal or greater than +2.
  • heteropolyanion refers to any anion with covalently bonded XOp and YO r polyhedra, and thus includes X-O-Y, and possibly X-O-X and Y-O-Y bonds, wherein X and Y represent any atoms, and wherein p and r are any positive integers.
  • heteropolyphosphate refers to any heteropolyanion, wherein X represents phosphorus (P) and Y represents any other atom.
  • phosphate adduct refers to any compound with one or more phosphate anions and one or more non-phosphate anions that are not covalently linked.
  • LA refers to lactic acid
  • AA refers to acrylic acid
  • AcH refers to acetaldehyde
  • PA refers to propionic acid
  • particle span refers to a statistical representation of a given particle sample and is equal to ⁇ D Vt o,go - ⁇ > ⁇ ⁇ . ⁇ V-Dv,o. o-
  • median particle size or D v ,o.5o refers to the diameter of a particle below which 50% of the total volume of particles lies.
  • Dyfl.io refers to the particle size that separates the particle sample at the 10% by volume fraction
  • D Vt o,9o is the particle size that separates the particle sample at the 90% by volume fraction.
  • conversion in % is defined as [hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof flow rate in (mol/min) - hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof flow rate out (mol/min)] / [hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof flow rate in (mol/min)] * 100.
  • conversion means molar conversion, unless otherwise noted.
  • yield in % is defined as [product flow rate out (mol/min) / hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof flow rate in (mol/min)]*100.
  • yield means molar yield, unless otherwise noted.
  • the term “selectivity” in % is defined as [Yield / Conversion]* 100.
  • the term “selectivity” means molar selectivity, unless otherwise noted.
  • total flow rate out in mol/min and for hydroxypropionic acid is defined as: (2/3)* [C2 flow rate out (mol/min)] + [C3 flow rate out (mol/min)] + (2/3)*[acetaldehyde flow rate out (mol/min)] + (4/3)*[C4 flow rate out (mol/min)] + [hydroxypropionic acid flow rate out (mol/min)] + [pyruvic acid flow rate out (mol/min)] + (2/3)* [acetic acid flow rate out (mol/min)] + [1,2-propanediol flow rate out (mol/min)] + [propionic acid flow rate out (mol/min)] + [acrylic acid flow rate out (mol/min)] + (5/3)*[2,3- pentanedione flow rate out (mol/min)] + (l/3)*[carbon monoxide flow rate out (mol/min)] + (l/3)*[carbon dioxide flow rate out (mol)
  • C2 means ethane and ethylene.
  • C3 means propane and propylene.
  • C4 means butane and butenes.
  • total molar balance or “TMB” in % is defined as [total flow rate out (mol/min) / hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof flow rate in (mol/min)]* 100.
  • the term "the acrylic acid yield was corrected for TMB” is defined as [acrylic acid yield / total molar balance]* 100, to account for slightly higher flows in the reactor.
  • GHSV Gas Hourly Space Velocity
  • STP Standard Temperature and Pressure conditions
  • LHSV Liquid Hourly Space Velocity
  • mixed condensed phosphate catalysts dehydrate hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof to acrylic acid, acrylic acid derivatives, or mixtures thereof with high: 1) yield and selectivity for acrylic acid, acrylic acid derivatives, or mixtures thereof, i.e., low amount and few side products; 2) efficiency, i.e., performance in short residence time; and 3) longevity.
  • the catalyst which includes at least one condensed phosphate anion and two different cations, works as follows: the carboxylate group of the hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof, associates with one or several cations, which in one embodiment is polyvalent, through one or both oxygen atoms, holding the molecule onto the surface of the catalyst, deactivating it from decarbonylation, and activating the C-OH bond for elimination.
  • the resulting protonated condensed phosphate anion dehydrates the hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof by concerted protonation of the hydroxyl group, removal of a proton from the methyl group, and elimination of the protonated hydroxyl group as a molecule of water, generating acrylic acid, acrylic acid derivatives, or mixtures thereof and reactivating the catalyst.
  • hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof are diluted with water, some condensed phosphate salts in the catalyst can be hydrolyzed to uncondensed monophosphates or shorter condensed phosphates, which can be transformed into a liquid state under the proper temperature and pressure conditions, facilitating the dehydration of hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof.
  • the catalyst comprises: (a) at least one condensed phosphate anion selected from the group consisting of formulae (I), (II), and (III),
  • n is at least 2 and m is at least 1, and (b) at least two different cations, wherein the catalyst is essentially neutrally charged, and further, wherein the molar ratio of phosphorus to the at least two different cations is between about 0.7 and about 1.7.
  • the anions defined by formulae (I), (II), and (III) are also referred to as polyphosphates (or oligophosphates), cyclophosphates, and ultraphosphates, respectively.
  • the catalyst comprises: (a) at least one condensed phosphate anion selected from the group consisting of formulae (I) and (II),
  • the cations can be monovalent or polyvalent. In one embodiment, one cation is monovalent and the other cation is polyvalent. In another embodiment, the polyvalent cation is selected from the group consisting of divalent cations, trivalent cations, tetravalent cations, pentavalent cations, and mixtures thereof.
  • Non-limiting examples of monovalent cations are H + , Li + , Na + , K + , Rb + , Cs + , Ag + , Rb + , Tl + , and mixtures thereof.
  • the monovalent cation is selected from the group consisting of Li + , Na + , K + , Rb + , Cs + , and mixtures thereof; in another embodiment, the monovalent cation is Na + or K + ; and in yet another embodiment, the monovalent cation is K + .
  • Non-limiting examples of polyvalent cations are cations of the alkaline earth metals (i.e., Be, Mg, Ca, Sr, Ba, and Ra), transition metals (e.g. Y, Ti, Zr, V, Nb, Cr, Mo, Mn, Re, Fe, Ru, Co, Rh, Ni, Pd, Pt, Cu, Ag, and Au), poor metals (e.g.
  • the polyvalent cation is selected from the group consisting of Be 2+ , Mg 2+ , Ca 2+ , Sr 2+ , Ba 2+ , Mn 2+ , Fe 2+ , Co 2+ , Ni 2+ , Cu 2+ , Zn 2+ , Cd 2+ , Sn 2+ , Pb 2+ , Ti 3+ , Cr 3+ , Mn 3+ , Fe 3+ , Al 3+ , Ga 3+ , Y 3+ , In 3+ , Sb 3+ , Bi 3+ , Si 4+ , Ti 4+ , V 4+ , Ge 4+ , Mo 4+ , Pt 4+ , V 5+ , Nb 5+ , Sb 5+ , and mixtures thereof.
  • the polyvalent cation is selected from the group consisting of Ca 2+ , Ba 2+ , Cu 2+ , Mn 2+ , Mn 3+ , and mixtures thereof; in another embodiment, the polyvalent cation is selected from the group consisting of Ca 2+ , Ba 2+ , Mn 3+ , and mixtures thereof; and in yet another embodiment, the polyvalent cation is Ba 2+ .
  • the catalyst can include cations: (a) H + , Li + , Na + , K + , Rb + , Cs + , or mixtures thereof; and (b) Be 2+ , Mg 2+ , Ca 2+ , Sr 2+ , Ba 2+ , Mn 2+ , Fe 2+ , Co 2+ , Ni 2+ , Cu 2+ , Zn 2+ , Cd 2+ , Sn 2+ , Pb 2+ , Ti 3+ , Cr 3+ , Mn 3+ , Fe 3+ , Al 3+ , Ga 3+ , Y 3+ , In 3+ , Sb 3+ , Bi 3+ , Si 4+ , Ti 4+ , V 4+ , Ge 4+ , Mo 4+ , Pt 4+ , V 5+ , Nb 5+ , Sb 5+ , or mixtures thereof.
  • the catalyst comprises Li + , Na + , or K + as monovalent cation, and Ca 2+ , Ba 2+ , or Mn 3+ as polyvalent cation; in another embodiment, the catalyst comprises Na + or K + as monovalent cation, and Ca 2+ or Ba 2+ as polyvalent cation; and in yet another embodiment, the catalyst comprises K + as the monovalent cation and Ba 2+ as the polyvalent cation.
  • the catalyst comprises Ba2-x- s K2xH2 S P 2 0 7 and (KP0 3 ) n , wherein x and s are greater or equal to 0 and less than about 0.5 and n is a positive integer.
  • the catalyst comprises Ca2_ x - s K2 X H 2s P 2 0 7 and (KPC>3) n , wherein x and s are greater or equal to 0 and less than about 0.5 and n is a positive integer.
  • the catalyst comprises Mni_ x _ s Ki+3 X H3 S P 2 C>7 or Mni_ x _ s K2+2xH2 S P 2 0 7 and (KP03) n wherein x and s are greater or equal to 0 and less than about 0.5 and n is a positive integer.
  • the catalyst comprises any blend of Ba 2 _ x _ s K2 X H2 S P20 7 , Ca 2 _ x _ s K2 X H2 S P20 7 , Mn 1 _ x _ s K 1 +3x H3 S P 2 0 7 or Mni_ x _ s K2+2 X H2sP2C>7; and (KP03) n , wherein x and s are greater or equal to 0 and less than about 0.5 and n is a positive integer.
  • the molar ratio of phosphorus to the cations in the catalyst is between about 0.7 and about 1.7; in another embodiment, the molar ratio of phosphorus to the cations in the catalyst is between about 0.8 and about 1.3; and in yet another embodiment, the molar ratio of phosphorus to the cations in the catalyst is about 1.
  • the catalyst comprises: (a) at least two different condensed phosphate anions selected from the group consisting of formulae (I), (II), and (III),
  • n is at least 2 and m is at least 1, and (b) one cation, wherein the catalyst is essentially neutrally charged, and further, wherein the molar ratio of phosphorus to the cation is between about 0.5 and about 4.0. In another embodiment, the molar ratio of phosphorus to the cation is between about t/2 and about t, wherein t is the charge of the cation.
  • the catalyst can include an inert support that is constructed of a material comprising silicates, aluminates, carbons, metal oxides, and mixtures thereof.
  • the carrier is inert relative to the reaction mixture expected to contact the catalyst.
  • the carrier is a low surface area silica or zirconia.
  • the carrier represents an amount of about 5 wt to about 98 wt , based on the total weight of the catalyst.
  • a catalyst that includes an inert support can be made by one of two exemplary methods: impregnation or co-precipitation.
  • the method of preparing the catalyst includes mixing and heating at least two different phosphorus containing compounds, wherein each said compound is described by one of the formulae (IV) to (XXV), or any of the hydrated forms of said formulae:
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds of formula (IV), wherein y is equal to 1, and one or more phosphorus containing compounds of formula (V), wherein y is equal to 2.
  • the catalyst is prepared by mixing and heating ⁇ : ⁇ 2 ⁇ 4 and M n HP0 4 .
  • M 1 is K + and M n is Ca 2+ , i.e., the catalyst is prepared by mixing and heating KH 2 P0 4 and CaHP0 4 ; or M 1 is K and M n is Ba 2+ , i.e., the catalyst is prepared by mixing and heating KH 2 P0 4 and BaHP0 4 .
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compound of formula (IV), wherein y is equal to 1, one or more phosphorus containing compounds of formula (XV), wherein v is equal to 2.
  • the catalyst is prepared by mixing and heating M : H 2 P0 4 and M n 2 P 2 C>7.
  • M 1 is K + and M n is Ca 2+ , i.e., the catalyst is prepared by mixing and heating KH 2 P0 4 and Ca 2 P 2 C>7; or M 1 is K + and M n is Ba 2+ , i.e., the catalyst is prepared by mixing and heating KH 2 P0 4 and Ba 2 P 2 C>7.
  • the molar ratio of phosphorus to the cations in the catalyst is between about 0.7 and about 1.7; in yet another embodiment, the molar ratio of phosphorus to the cations in the catalyst is between about 0.8 and about 1.3; and in another embodiment, the molar ratio of phosphorus to the cations in the catalyst is about 1.
  • the method of preparing the catalyst includes mixing and heating (a) at least one phosphorus containing compound, wherein each said compound is described by one of the formulae (IV) to (XXV), or any of the hydrated forms of said formulae:
  • the non-phosphorus containing compounds can be selected from the group consisting of carboxylic acid-derived salts, halide salts, metal acetylacetonates, and metal alkoxides.
  • the molar ratio of phosphorus to the cations in the catalyst is between about 0.7 and about 1.7; in another embodiment, the molar ratio of phosphorus to the cations in the catalyst is between about 0.8 and about 1.3; and in yet another embodiment, the molar ratio of phosphorus to the cations in the catalyst is about 1.
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds of formulae (IV) to (XXV) or their hydrated forms, and one or more nitrate salts of formulae (XXVI) to (XXVIII) or their hydrated forms.
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds of formula (IV) and one or more nitrate salts of formula (XXVII).
  • the catalyst is prepared by mixing and heating a phosphorus containing compound of formula (IV) wherein y is equal to 2, a phosphorus containing compound of formula (IV) wherein y is equal to 0 (i.e., phosphoric acid), and a nitrate salt of formula (XXVII).
  • the catalyst is prepared by mixing and heating K 2 HP0 4 , H 3 P0 4 , and Ba(NC>3) 2 .
  • the catalyst is prepared by mixing and heating K 2 HP0 4 , ]3 ⁇ 4 ⁇ 0 4 , and Ca(N0 3 ) 2 .
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds of formula (IV) and one or more nitrate salts of formula (XXVIII).
  • the catalyst is prepared by mixing and heating a phosphorus containing compound of formula (IV) wherein y is equal to 2, a phosphorus containing compound of formula (IV) wherein y is equal to 0 (i.e., phosphoric acid), and a nitrate salt of formula (XXVIII).
  • the catalyst is prepared by mixing and heating ⁇ 2 ⁇ 0 4 , ]3 ⁇ 4 ⁇ 0 4 , and ⁇ ( ⁇ 3 ) 2 ⁇ 4 ⁇ 2 0.
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds of formula (V) and one or more nitrate salts of formula (XXVI).
  • the catalyst is prepared by mixing and heating a phosphorus containing compound of formula (V) wherein y is equal to 2, a phosphorus containing compound of formula (V) wherein y is equal to 0 (i.e., phosphoric acid), and a nitrate salt of formula (XXVI).
  • the catalyst is prepared by mixing and heating BaHP0 4 , H 3 PC , and KNO 3 .
  • the catalyst is prepared by mixing and heating CaHP0 4 , ]3 ⁇ 4 ⁇ 0 4 , and KNO 3 .
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds of formula (V), one or more phosphorus containing compounds of formula (XV), and one or more nitrate salts of formula (XXVI).
  • the catalyst is prepared by mixing and heating a phosphorus containing compound of formula (V), wherein y is equal to 0 (i.e., phosphoric acid); a phosphorus containing compound of formula (XV), wherein v is equal to 2; and a nitrate salt of formula (XXVI).
  • the catalyst is prepared by mixing and heating H 3 P0 4> Ca 2 P 2 C>7, and KNO 3 .
  • the catalyst is prepared by mixing and heating H 3 P0 4> Ba 2 P 2 0 7 , and KNO 3 .
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds of formula (VI) and one or more nitrate salts of formula (XXVI).
  • the catalyst is prepared by mixing and heating a phosphorus containing compound of formula (VI), wherein y is equal to 3; a phosphorus containing compound of formula (VI), wherein y is equal to 0 (i.e., phosphoric acid); and a nitrate salt of formula (XXVI).
  • the catalyst is prepared by mixing and heating MnP0 4 qH 2 0, H 3 P0 4 , and KNO 3 .
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds of formula (IV), one or more phosphorus containing compounds of formula (IX), and one or more nitrate salts of formula (XXVII).
  • the catalyst is prepared by mixing and heating a phosphorus containing compound of formula (IV), wherein y is equal to 2; a phosphorus containing compound of formula (IV), wherein y is equal to 0 (i.e., phosphoric acid); a phosphorus containing compound of formula (IX), wherein a is equal to 2, b is equal to 1, and c is equal to 1; and a nitrate salt of formula (XXVII).
  • the catalyst is prepared by mixing and heating K 2 HP0 4 , H 3 P0 4 , Cu 2 (OH)P0 4 , and Ba(N0 3 ) 2 .
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds of formula (V), one or more phosphorus containing compounds of formula (IX), and one or more nitrate salts of formula (XXVI).
  • the catalyst is prepared by mixing and heating a phosphorus containing compound of formula (V), wherein y is equal to 3; a phosphorus containing compound of formula (V), wherein y is equal to 0 (i.e., phosphoric acid); a phosphorus containing compound of formula (IX), wherein a is equal to 2, b is equal to 1, and c is equal to 1; and a nitrate salt of formula (XXVI).
  • the catalyst is prepared by mixing and heating Ba 3 (P0 4 ) 2 , H 3 P0 4 , Cu 2 (OH)P0 4 , and KN0 3 .
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds described by one of the formulae (IV) to (XXV) or any of the hydrated forms, and one or more carbonate salts described by one of the formulae (XXIX) to (XXXI) or any of the hydrated forms.
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds described by one of the formulae (IV) to (XXV) or any of the hydrated forms, and one or more acetate salts described by one of the formulae (XXXII) to (XXXV), any other organic acid-derived salts, or any of the hydrated forms.
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds described by one of the formulae (IV) to (XXV) or any of the hydrated forms, and one or more metal oxides described by one of the formulae (XXXVI) to (XXXIX) or any of the hydrated forms.
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds described by one of the formulae (IV) to (XXV) or any of the hydrated forms, and one or more chloride salts described by one of the formulae (XXXX) to (XXXXIII), any other halide salts, or any of the hydrated forms.
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds described by one of the formulae (IV) to (XXV) or any of the hydrated forms, and one or more sulfate salts described by one of the formulae (XXXXIV) to (XXXX VII) or any of the hydrated forms.
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds described by one of the formulae (IV) to (XXV) or any of the hydrated forms, and one or more hydroxides described by one of the formulae (XXXXVIII) to (XL) or any of the hydrated forms.
  • the catalyst is prepared by mixing and heating one or more phosphorus containing compounds of formulae (IV) to (XXV), and two or more non-phosphorus containing compounds of formulae (XXVI) to (XL) or their hydrated forms.
  • the molar ratio of phosphorus to the cations is between about 0.7 and about 1.7; in another embodiment, the molar ratio of phosphorus to the cations (i.e., M M ⁇ M 111 ⁇ ...) is between about 0.8 and about 1.3, and in yet another embodiment, the molar ratio of phosphorus to the cations (i.e., M M ⁇ M 111 ⁇ %) is about 1.
  • the molar ratio between phosphorus and the metals (K + Ba) is between about 0.7 and about 1.7; and in another embodiment, the molar ratio between phosphorus and the metals (K + Ba) is about 1.
  • the molar ratio between cations is, in one embodiment, between about 1 :50 and about 50: 1; and in another embodiment, the molar ratio between cations is between about 1 :4 and about 4: 1.
  • the molar ratio between cations is between about 1 :4 and about 4: 1.
  • the catalyst is prepared by mixing and heating K2HPO4, Ba(NC>3)2, and H 3 PO4, the potassium and barium are present, in another embodiment, in a molar ratio, K:Ba, between about 2:3 to about 1: 1.
  • the catalyst can include an inert support that is constructed of a material comprising silicates, aluminates, carbons, metal oxides, and mixtures thereof.
  • the carrier is inert relative to the reaction mixture expected to contact the catalyst.
  • the method of preparing the catalyst can further include mixing an inert support with the catalyst before, during, or after the mixing and heating of the phosphorus containing compounds, wherein the inert support includes silicates, aluminates, carbons, metal oxides, and mixtures thereof.
  • the method of preparing the catalyst can further include mixing an inert support with the catalyst before, during, or after the mixing and heating of the phosphorus containing compounds and the non-phosphorus containing compounds, wherein the inert support includes silicates, aluminates, carbons, metal oxides, and mixtures thereof.
  • Mixing of the phosphorus containing compounds or the phosphorus containing and non- phosphorus containing compounds of the catalyst can be performed by any method known to those skilled in the art, such as, by way of example and not limitation: solid mixing and co- precipitation.
  • solid mixing method the various components are physically mixed together with optional grinding using any method known to those skilled in the art, such as, by way of example and not limitation, shear, extensional, kneading, extrusion, and others.
  • an aqueous solution or suspension of the various components, including one or more of the phosphate compounds is prepared, followed by optional filtration and heating to remove solvents and volatile materials (e.g., water, nitric acid, carbon dioxide, ammonia, or acetic acid).
  • solvents and volatile materials e.g., water, nitric acid, carbon dioxide, ammonia, or acetic acid.
  • the heating is typically done using any method known to those skilled in the art, such as, by way of example and not limitation, convection, conduction, radiation, microwave heating, and others.
  • the catalyst is calcined.
  • Calcination is a process that allows chemical reaction and/or thermal decomposition and/or phase transition and/or removal of volatile materials.
  • the calcination process is carried out with any equipment known to those skilled in the art, such as, by way of example and not limitation, furnaces or reactors of various designs, including shaft furnaces, rotary kilns, hearth furnaces, and fluidized bed reactors.
  • the calcination temperature is, in one embodiment, about 200°C to about 1200°C; in another embodiment, the calcination temperature is about 250°C to about 900°C; and in yet another embodiment, the calcination temperature is about 300°C to 600°C.
  • the calcination time is, in one embodiment, about one hour to about seventy-two hours.
  • the catalyst is, in one embodiment, ground and sieved to provide a more uniform product.
  • the particle size distribution of the catalyst particles includes a particle span that, in one embodiment, is less than about 3 ; in another embodiment, the particle size distribution of the catalyst particles includes a particle span that is less than about 2; and in yet another embodiment, the particle size distribution of the catalyst particles includes a particle span that is less than about 1.5.
  • the catalyst is sieved to a median particle size of about 50 ⁇ to about 500 ⁇ . In another embodiment of the invention, the catalyst is sieved to a median particle size of about 100 ⁇ to about 200 ⁇ .
  • the catalyst is prepared by the following steps, which comprise: (a) combining a phosphorus containing compound, a nitrate salt, phosphoric acid, and water to form a wet mixture, wherein the molar ratio between phosphorus and the cations in both said phosphorus containing compound and said nitrate salt is about 1, (b) calcining said wet mixture stepwise at about 50°C, about 80°C, about 120°C, and about 450°C to about 550°C to produce a dried solid, and (c) grinding and sieving said dried solid to about 100 ⁇ to about 200 ⁇ , to produce said catalyst.
  • the catalyst is prepared by the following steps, which comprise: (a) combining MnP0 4 qH 2 0, KNO 3 , and H 3 PO 4 , in a molar ratio of about 0.3:1:1, on an anhydrous basis, and water to give a wet mixture, (b) calcining said wet mixture stepwise at about 50°C, about 80°C, about 120°C, and about 450°C to about 550°C to give a dried solid, and (c) grinding and sieving said dried solid to about 100 ⁇ to about 200 ⁇ , to produce said catalyst.
  • the catalyst is prepared by the following steps, which comprise: (a) combining Ca 2 P 2 07, KNO 3 , and H 3 PO 4 , in a molar ratio of about 1.6:1:1, and water to give a wet mixture, (b) calcining said wet mixture stepwise at about 50°C, about 80°C, about 120°C, and about 450°C to about 550°C to give a dried solid, and (c) grinding and sieving said dried solid to about 100 ⁇ to about 200 ⁇ , to produce said catalyst.
  • the catalyst is prepared by the following steps, which comprise: (a) combining a phosphorus containing compound, a nitrate salt, phosphoric acid, and water to give a wet mixture, wherein the molar ratio between phosphorus and the cations in both the phosphorus containing compound and nitrate salt is about 1 , (b) heating said wet mixture to about 80°C with stirring until near dryness to form a wet solid, (c) calcining said wet solid stepwise at about 50°C, about 80°C, about 120°C, and about 450°C to about 550°C to give a dried solid, and (d) grinding and sieving said dried solid to about 100 ⁇ to about 200 ⁇ , to produce said catalyst.
  • the catalyst is prepared by the following steps, which comprise: (a) combining Ba(NC>3) 2 , K 2 HP0 4 , and H 3 PO4, in a molar ratio of about 3:1:4, and water to give a wet mixture, (b) heating said wet mixture to about 80°C with stirring until near dryness to form a wet solid, (c) calcining said wet solid stepwise at about 50°C, about 80°C, about 120°C, and about 450°C to about 550°C to give a dried solid, and (d) grinding and sieving said dried solid to about 100 ⁇ to about 200 ⁇ , to produce said catalyst.
  • the catalyst is prepared by the following steps, which comprise: (a) combining ⁇ ( ⁇ 3 ) 2 ⁇ 4 ⁇ 2 0, K 2 HP0 4 , and H 3 PO4, in a molar ratio of about 1:1.5:2, and water to give a wet mixture, (b) heating said wet mixture to about 80°C with stirring until near dryness to form a wet solid, (c) calcining said wet solid stepwise at about 50°C, about 80°C, about 120°C, and about 450°C to about 550°C to give a dried solid, and (d) grinding and sieving said dried solid to about 100 ⁇ to about 200 ⁇ , to produce said catalyst.
  • the catalyst is prepared by the following steps, which comprise: (a) combining Ca 2 P 2 C>7 and ⁇ 2 ⁇ 0 4 in a molar ratio of about 3: 1 to give a solid mixture, and (b) calcining said solid mixture stepwise at about 50°C, about 80°C, about 120°C, and about 450°C to about 550°C, to produce said catalyst.
  • the catalyst can be utilized to catalyze several chemical reactions.
  • Non-limiting examples of reactions are: dehydration of hydroxypropionic acid to acrylic acid (as described in further detail below), dehydration of glycerin to acrolein, dehydration of aliphatic alcohols to alkenes or olefins, dehydrogenation of aliphatic alcohols to ethers, other dehydrogenations, hydrolyses, alkylations, dealkylations, oxidations, disproportionations, esterifications, cyclizations, isomerizations, condensations, aromatizations, polymerizations, and other reactions that may be apparent to those having ordinary skill in the art.
  • a method for dehydrating hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof to acrylic acid, acrylic acid derivatives, or mixtures thereof includes contacting a stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof containing with a catalyst comprising: (a) at least one condensed phosphate anion selected from the group consisting of formulae (I), (II), and (III),
  • n is at least 2 and m is at least 1, and (b) at least two different cations, wherein the catalyst is essentially neutrally charged, and further, wherein the molar ratio of phosphorus to the at least two different cations is between about 0.7 and about 1.7, whereby acrylic acid, acrylic acid derivatives, or mixtures thereof are produced as a result of said stream being contacted with the catalyst.
  • Alternative catalysts comprising anions selected from the group consistsing of non- phosphorus containing anions, he teropoly anions, and phosphate adducts, and at least two different cations, wherein the catalyst is essentially neutrally charged, can be utilized for dehydrating hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof to acrylic acid, acrylic acid derivatives, or mixtures thereof.
  • Non-limiting examples of non- phosphorus containing anions are arsenates, condensed arsenates, nitrates, sulfates, vanadates, niobates, tantalates, selenates, and others that may be apparent to those having ordinary skill in the art.
  • Non-limiting examples of heteropolyanions are heteropolyphosphates, such as arsenatophosphates, phosphoaluminates, phosphoborates, phosphocromates, phosphomolybdates, phosphosilicates, phosphosulfates, phosphotungstates, and others that may be apparent to those having ordinary skill in the art.
  • Non-limiting examples of phosphate adducts are adducts of phosphate anions with telluric acid, halides, borates, carbonates, nitrates, sulfates, chromates, silicates, oxalates, mixtures thereof, or others that may be apparent to those having ordinary skill in the art.
  • Hydroxypropionic acid can be 3-hydroxypropionic acid, 2-hydroxypropionic acid (also called, lactic acid), or mixtures thereof.
  • the hydroxypropionic acid is lactic acid.
  • Derivatives of hydroxypropionic acid can be metal or ammonium salts of hydroxypropionic acid, alkyl esters of hydroxypropionic acid, hydroxypropionic acid oligomers, cyclic di-esters of hydroxypropionic acid, hydroxypropionic acid anhydride, or a mixture thereof.
  • Non-limiting examples of metal salts of hydroxypropionic acid are sodium hydroxypropionate, potassium hydroxypropionate, and calcium hydroxypropionate.
  • Non-limiting examples of alkyl esters of hydroxypropionic acid are methyl hydroxypropionate, ethyl hydroxypropionate, or mixtures thereof.
  • a non-limiting example of cyclic di-esters of hydroxypropionic acid is dilactide.
  • Acrylic acid derivatives can be metal or ammonium salts of acrylic acid, alkyl esters of acrylic acid, acrylic acid oligomers, or a mixture thereof.
  • metal salts of acrylic acid are sodium acrylate, potassium acrylate, and calcium acrylate.
  • alkyl esters of acrylic acid are methyl acrylate, ethyl acrylate, or mixtures thereof.
  • the stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof can include a liquid stream and an inert gas (i.e., a gas otherwise inert to the reaction mixture under the conditions of the method) that can be separately or jointly fed into an evaporation vessel upstream of the catalyst reactor for the stream to become gaseous.
  • the liquid stream can include the hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof and a diluent.
  • Non-limiting examples of the diluent are water, methanol, ethanol, acetone, C3 to C8 linear and branched alcohols, C5 to C8 linear and branched alkanes, ethyl acetate, non-volatile ethers (including diphenyl ether), and mixtures thereof.
  • the diluent is water.
  • the liquid stream comprises an aqueous solution of lactic acid or lactic acid derivatives selected from the group consisting of lactide, lactic acid oligomers, salts of lactic acid, and alkyl lactates.
  • the liquid stream includes from about 2 wt to about 95 wt lactic acid or lactic acid derivatives, based on the total weight of the liquid stream. In another embodiment, the liquid steam includes from about 5 wt to about 50 wt lactic acid or lactic acid derivatives, based on the total weight of the liquid stream. In another embodiment, the liquid stream includes from about 10 wt to about 25 wt lactic acid or lactic acid derivatives, based on the total weight of the liquid stream. In another embodiment, the liquid stream includes about 20 wt lactic acid or lactic acid derivatives, based on the total weight of the liquid stream. In another embodiment, the liquid stream comprises an aqueous solution of lactic acid along with derivatives of lactic acid.
  • the liquid stream comprises less than about 30 wt of lactic acid derivatives, based on the total weight of the liquid stream. In another embodiment, the liquid stream comprises less than about 10 wt of lactic acid derivatives, based on the total weight of the liquid stream. In yet another embodiment, the liquid stream comprises less than about 5 wt of lactic acid derivatives, based on the total weight of the liquid stream.
  • the inert gas is a gas that is otherwise inert to the reaction mixture under the conditions of the method.
  • Non-limiting examples of the inert gas are nitrogen, air, helium, argon, carbon dioxide, carbon monoxide, steam, and mixtures thereof.
  • the inert gas is nitrogen.
  • the stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof can be in the form of a gaseous mixture when contacting the catalyst.
  • the concentration of hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof based on the total moles of said stream (calculated under STP conditions) is from about 0.5 mol to about 50 mol .
  • the concentration of hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof based on the total moles of said stream (calculated under STP conditions) is from about 1 mol to about 10 mol .
  • the concentration of hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof based on the total moles of said stream (calculated under STP conditions) is between about 1.5 mol to about 3.5 mol . In yet another embodiment, the concentration of hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof based on the total moles of said stream (calculated under STP conditions) is about 2.5 mol . In one embodiment, the temperature at which said stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof contacts the catalyst is between about 120°C and about 700°C.
  • the temperature at which said stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof contacts the catalyst is between about 150°C and about 500°C. In another embodiment, the temperature at which said stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof contacts the catalyst is between about 300°C and about 450°C. In yet another embodiment, the temperature at which said stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof contacts the catalyst is between about 325°C and about 400°C.
  • the stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof contacts the catalyst at a GHSV between about 720 h "1 and about 36,000 h "1 . In another embodiment, the stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof contacts the catalyst at a GHSV between about 1,800 h "1 to about 7,200 h "1 . In another embodiment, the stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof contacts the catalyst at a GHSV about 3,600 h "1 .
  • the stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof contacts the catalyst at a pressure between about 0 psig and about 550 psig. In another embodiment, the stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof contacts the catalyst at a pressure of about 360 psig.
  • the stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof contacts the catalyst in a reactor having an interior surface comprising material selected from the group consisting of quartz, borosilicate glass, silicon, hastelloy, inconel, manufactured sapphire, stainless steel, and mixtures thereof.
  • the stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof contacts the catalyst in a reactor having an interior surface comprising material selected from the group consisting of quartz or borosilicate glass.
  • the stream comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof contacts the catalyst in a reactor having an interior surface comprising borosilicate glass.
  • the method includes contacting the catalyst with a gaseous mixture comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof under conditions sufficient to produce acrylic acid, acrylic acid derivatives, or mixtures thereof in a yield of at least 50%.
  • the method includes contacting the catalyst with a gaseous mixture comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof under conditions are sufficient to produce acrylic acid, acrylic acid derivatives, or mixtures thereof in a yield of at least about 70%
  • the method includes contacting the catalyst with a gaseous mixture comprising hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof under conditions are sufficient to produce acrylic acid, acrylic acid derivatives, or mixtures thereof in a yield of at least about 80%.
  • the method conditions are sufficient to produce acrylic acid, acrylic acid derivatives, or mixtures thereof with a selectivity of at least about 50%.
  • the method conditions are sufficient to produce acrylic acid, acrylic acid derivatives, or mixtures thereof with a selectivity of at least about 70%. In another embodiment, the method conditions are sufficient to produce acrylic acid, acrylic acid derivatives, or mixtures thereof with a selectivity of at least about 80%. In another embodiment, the method conditions are sufficient to produce acrylic acid, acrylic acid derivatives, or mixtures thereof with propanoic acid as an impurity, wherein the propanoic acid selectivity is less than about 5%. In another embodiment, the method conditions are sufficient to produce acrylic acid, acrylic acid derivatives, or mixtures thereof with propanoic acid as an impurity, wherein the propanoic acid selectivity is less than about 1%.
  • the method conditions are sufficient to produce acrylic acid, acrylic acid derivatives, or mixtures thereof with a conversion of said hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof of more than about 50%. In another embodiment, the method conditions are sufficient to produce acrylic acid, acrylic acid derivatives, or mixtures thereof with a conversion of said hydroxypropionic acid, hydroxypropionic acid derivatives, or mixtures thereof of more than about 80%.
  • the conditions are sufficient to produce propionic acid in a yield of less than about 6% from lactic acid present in the gaseous mixture. In another embodiment, the conditions are sufficient to produce propionic acid in a yield of less than about 1%, from lactic acid present in the gaseous mixtureln one embodiment, the conditions are sufficient to produce each of acetic acid, pyruvic acid, 1,2-propanediol, and 2,3-pentanedione in a yield of less than about 2% from lactic acid present in the gaseous stream.
  • the conditions are sufficient to produce each of acetic acid, pyruvic acid, 1,2-propanediol, and 2,3- pentanedione in a yield of less than about 0.5%, from lactic acid present in the gaseous stream. In one embodiment, the conditions are sufficient to produce acetaldehyde in a yield of less than about 8% from lactic acid present in the gaseous mixture. In another embodiment, the conditions are sufficient to produce acetaldehyde in a yield of less than about 4% from lactic acid present in the gaseous mixture. In another embodiment, the conditions are sufficient to produce acetaldehyde in a yield of less than about 3%, from lactic acid present in the gaseous mixture. These yields are believed to be, heretofore, unattainably low. Yet, these benefits are indeed achievable as further evidenced in the Examples set out below.
  • a method for dehydrating glycerin to acrolein includes contacting a glycerin containing stream with a catalyst comprising: (a) at least one condensed phosphate anion selected from the group consisting of formulae (I), (II), and (III),
  • n is at least 2 and m is at least 1, and (b) at least two different cations, wherein the catalyst is essentially neutrally charged, and further, wherein the molar ratio of phosphorus to the at least two different cations is between about 0.7 and about 1.7, whereby acrolein is produced as a result of said glycerin being contacted with the catalyst.
  • Acrolein is an intermediate which can be converted to acrylic acid using conditions similar to what are used today in the second oxidation step in the propylene to acrylic acid process.
  • Examples 1 through 7 describe the preparation of different mixed condensed phosphate catalysts in accordance with various embodiments described above.
  • Examples 8 through 12 describe the preparation of catalysts not according to the invention.
  • the final pH of the suspension was about 1.6.
  • the acid-containing suspension was then dried slowly in a glass beaker at 80°C using a heating plate while magnetically stirring the suspension until the liquid was evaporated and the material was almost completely dried. After evaporation, the material was transferred to a crushable ceramic.
  • Heating was continued in a oven with air circulation (N30/80 HA; Nabertherm GmbH, Lilienthal, Germany) at 50°C for 10 h, then at 80°C for 10 h (0.5°C/min ramp), 120°C for 2 hours (0.5°C/min ramp) to remove residual water followed by calcination at 450°C for 4 hours (2°C/min ramp).
  • air circulation N30/80 HA; Nabertherm GmbH, Lilienthal, Germany
  • 80°C for 10 h 0.5°C/min ramp
  • 120°C for 2 hours 0.5°C/min ramp
  • calcination the material was left inside the oven until it cooled down by itself at a temperature below 100°C before it was taken out of the oven.
  • the catalyst was ground and sieved to about 100 ⁇ to about 200 ⁇ .
  • the material was analyzed by X-ray diffraction (XRD) and energy dispersive spectroscopy coupled to scanning electron microscopy (EDS/SEM) allowing the identification of o-Ba 2 P 2 07, a-Ba3P 4 0i3, Ba(N03) 2 , and KPO 3 with some incorporation of K within the Ba- containing phases.
  • XRD X-ray diffraction
  • EDS/SEM scanning electron microscopy
  • the molar ratio between phosphorus (P) and the cations (M 1 and M n ) in the identified condensed phosphate salts was about 1 to about 1.3.
  • Solid dibasic potassium phosphate, K 2 HP0 4 (36.40 g, 209 mmol, > 98%; Sigma - Aldrich Co., St. Louis, MO; catalog # P3786) was mixed quickly with an aqueous solution of barium nitrate, Ba(N0 3 ) 2 (2050 mL of a 0.08 g/mL stock solution, 627 mmol, 99.999%; Sigma - Aldrich Co., St. Louis, MO; catalog # 202754) at room temperature.
  • the final pH of the suspension was about 1.6.
  • the acid-containing suspension was then dried slowly in a glass beaker at 80°C using a heating plate while magnetically stirring the suspension until the liquid was evaporated and the material was almost completely dried.
  • Heating was continued in a oven with air circulation (G1530A, HP6890 GC; Agilent Corp., Santa Clara, CA) at 50°C for 5.3 h, then at 80°C for 10 h (0.5°C/min ramp), following by cooling down at 25°C.
  • the material was calcined at 120°C for 2 hours (0.5°C/min ramp) followed by 450°C for 4 hours (2°C/min ramp) using the same oven. After calcination, the material was left inside the oven until it cooled down by itself at a temperature below 25 °C before it was taken out of the oven. Finally, the catalyst was ground and sieved to about 100 ⁇ to about 200 ⁇ .
  • the material was analyzed by XRD and EDS/SEM allowing the identification of o-Ba 2 P 2 07, a-Ba3P 4 0i3, Ba(N03) 2 , KPO 3 , and some amorphous material with some incorporation of K within the Ba-containing phases.
  • the molar ratio of phosphorus (P) to the cations (M 1 and M n ) in the identified condensed phosphate salts was about 1 to about 1.3.
  • the material was heated in a oven with air circulation (N30/80 HA; Nabertherm GmbH, Lilienthal, Germany) at 50°C for 2 h, then at 80°C for 10 h (0.5°C/min ramp), 120°C for 2 hours (0.5°C/min ramp) to remove residual water followed by calcination at 450°C for 4 hours (2°C/min ramp). After calcination, the material was left inside the oven until it cooled down by itself at a temperature below 100°C before it was taken out of the oven. Finally, the catalyst was ground and sieved to about 100 ⁇ to about 200 ⁇ . The material was analyzed by XRD allowing the identification of P-Ca 2 P 2 C>7 and KPO 3 . The molar ratio between phosphorus (P) and the cations (M 1 and M n ) in these condensed phosphate salts was about 1.
  • the material was heated in a oven with air circulation (N30/80 HA; Nabertherm GmbH, Lilienthal, Germany) at 50°C for 2 h, then at 80°C for 10 h (0.5°C/min ramp), 120°C for 2 hours (0.5°C/min ramp) to remove residual water followed by calcination at 550°C for 4 hours (2°C/min ramp). After calcination, the material was left inside the oven until it cooled down by itself at a temperature below 100°C before it was taken out of the oven. The material was analyzed by XRD allowing the identification of ⁇ - Ca 2 P 2 0 7 and KPO 3 . The molar ratio between phosphorus (P) and the cations (M 1 and M n ) in these condensed phosphate salts was about 1. EXAMPLE 5
  • the material was heated in a oven with air circulation (N30/80 HA; Nabertherm GmbH, Lilienthal, Germany) at 50°C for 2 h, then at 80°C for 10 h (0.5°C/min ramp), 120°C for 2 hours (0.5°C/min ramp) to remove residual water followed by calcination at 450°C for 4 hours (2°C/min ramp). After calcination, the material was left inside the oven until it cooled down by itself at a temperature below 100°C before it was taken out of the oven. Finally, the catalyst was ground and sieved to about 100 ⁇ to about 200 ⁇ .
  • the material was analyzed by XRD allowing the identification of MnKP 2 07 and KPO 3 ; the molar ratio between phosphorus (P) and the cations (M 1 and M n ) in these condensed phosphate salts was about 1.
  • the material was heated in a oven with air circulation (N30/80 HA; Nabertherm GmbH, Lilienthal, Germany) at 50°C for 2 h, then at 80°C for 10 h (0.5°C/min ramp), 120°C for 2 hours (0.5°C/min ramp) to remove residual water followed by calcination at 550°C for 4 hours (2°C/min ramp). After calcination, the material was left inside the oven until it cooled down by itself at a temperature below 100°C before it was taken out of the oven. Finally, the catalyst was ground and sieved to about 100 ⁇ to about 200 ⁇ . The material was analyzed by XRD allowing the identification of MnKP 2 07 and KPO 3 . The molar ratio between phosphorus (P) and the cations (M 1 and M n ) in these condensed phosphate salts was about 1. EXAMPLE 7
  • the Ba(N0 3 ) 2 solution was added drop wise to the Na 3 P0 4 solution while stirring and heating to 60°C, forming a white slurry during the addition.
  • the pH was continuously monitored and concentrated ammonium hydroxide added dropwise to maintain pH 7. Heating and stirring at 60°C continued for 60 min, at which time the solid was filtered and washed thoroughly with deionized water.
  • the solid was suspended in 2 L of deionized water and filtered again and washed thoroughly with deionized water. In a vented oven, the filter cake was dried at 120°C for 5 hours (l°C/min ramp), followed by calcination at 350°C for 4 hours (2°C/min ramp) to give Ba 3 (P0 4 ) 2 as a white solid.
  • the material was heated in a oven with air circulation (N30/80 HA; Nabertherm GmbH, Lilienthal, Germany) at 50°C for 2 h, then at 80°C for 10 h (0.5°C/min ramp), 120°C for 2 hours (0.5°C/min ramp) to remove residual water followed by calcination at 550°C for 4 hours (2°C/min ramp). After calcination, the material was left inside the oven until it cooled down by itself at a temperature below 100°C before it was taken out of the oven.
  • air circulation N30/80 HA; Nabertherm GmbH, Lilienthal, Germany
  • a mixed condensed phosphate catalyst was prepared and used for comparative purposes.
  • An aqueous solution of barium nitrate, Ba(N0 3 ) 2 (88.39 mL of a 0.08 g/mL stock solution, 27 mmol, 99.999%; Sigma - Aldrich Co., St. Louis, MO; catalog # 202754), was added to solid dibasic potassium phosphate, K 2 HP0 4 (1.57 g, 9.0 mmol, > 98%; Sigma - Aldrich Co., St. Louis, MO; catalog # P3786) at room temperature.
  • the acid-containing slurry was then dried slowly in a glass beaker at 80°C using a heating plate while stirring the suspension until the liquid was evaporated and the material was almost completely dried.
  • the material was transferred to a crushable ceramic. Heating was continued in a oven with air circulation (N30/80 HA; Nabertherm GmbH, Lilienthal, Germany) at 50°C for 2 h, then at 80°C for 10 h (0.5°C/min ramp), 120°C for 2 hours (0.5°C/min ramp) to remove residual water followed by calcination at 450°C for 4 hours (2°C/min ramp). After calcination, the material was left inside the oven until it cooled down by itself at a temperature below 100°C before it was taken out of the oven. Finally, the catalyst was ground and sieved to about 100 ⁇ to about 200 ⁇ .
  • a mixed condensed phosphate catalyst was prepared and used for comparative purposes.
  • An aqueous solution of barium nitrate, Ba(N0 3 ) 2 (88.39 mL of a 0.08 g/mL stock solution, 27 mmol, 99.999%; Sigma - Aldrich Co., St Louis, MO; catalog # 202754), was added to solid dibasic potassium phosphate, K 2 HP0 4 (1.57 g, 9.0 mmol, > 98%; Sigma - Aldrich Co., St Louis, MO; catalog # P3786) at room temperature.
  • the acid- containing solution was then dried slowly in a glass beaker at 80°C using a heating plate while stirring the suspension until the liquid was evaporated and the material was almost completely dried.
  • the material was transferred to a crushable ceramic. Heating was continued in a oven with air circulation (N30/80 HA; Nabertherm GmbH, Lilienthal, Germany) at 50°C for 2 h, then at 80°C for 10 h (0.5°C/min ramp), 120°C for 2 hours (0.5°C/min ramp) to remove residual water followed by calcination at 450°C for 4 hours (2°C/min ramp). After calcination, the material was left inside the oven until it cooled down by itself at a temperature below 100°C before it was taken out of the oven. Finally, the catalyst was ground and sieved to about 100 ⁇ to about 200 ⁇ .
  • a barium monophosphate catalyst not according to the invention, was prepared and used for comparative purposes.
  • Ammonium hydrogen phosphate (NH 4 ) 2 HP0 4 (142.20 g, 1.08 mol; Aldrich, St Louis, MO; catalog # 215996), was dissolved in 1 L deionized water.
  • Aqueous ammonium hydroxide, NH 4 OH (290 mL, 28-29%; EMD, Merck KGaA, Darmstadt, Germany; catalog # AX 1303) was added slowly and heated gently until dissolved to form an ammonium phosphate solution.
  • barium acetate, (CH 3 COO) 2 Ba (285.43 g, 1.12 mol, Aldrich, St Louis, MO; catalog # 243671)
  • the barium acetate solution was slowly added to the ammonium phosphate solution to form a white precipitate. After stirring for 45 min, the white solid was filtered. The solid was then re-suspended in 300 mL of deionized water, stirred for 10 min, and filtered again. This process was repeated two times. The resulting white solid was dried in a vented oven at 130°C overnight.
  • the solid was sieved to about 500 ⁇ to 710 ⁇ and calcined in a kiln at 500°C for 4 hours (100°C/h ramp). After calcination, a sample of the catalyst was sieved to about 100 ⁇ to about 200 ⁇ . The material was analyzed by XRD allowing the identification of Ba 3 (P0 4 ) 2 .
  • a barium diphosphate catalyst not according to the invention, was prepared and used for comparative purposes.
  • a sample of dibasic barium phosphate, BaHP0 4 (Sigma - Aldrich Co., St. Louis, MO; catalog # 31139), was calcined at 550°C for 12 h, using a ceramic crucible and a temperature ramp of 2°C/min in a gravity convection oven. After calcination, the catalyst was ground using a mortar and a pestle and sieved to about 100 ⁇ to about 200 ⁇ . The material was analyzed by XRD allowing the identification of a-Ba 2 P 2 07.
  • EXAMPLE 12 comparative
  • a barium tetraphosphate catalyst was prepared and used for comparative purposes.
  • Dibasic barium monophosphate, BaHP0 4 (23.52 g, 100.8 mmol, Sigma - Aldrich Co., St Louis, MO; catalog # 31139) and dibasic ammonium monophosphate, (NH 4 ) 2 HP0 4 (4.44 g, 33.6 mmol, Sigma - Aldrich Co., St. Louis, MO; catalog # 379980) were mixed and ground together using a mortar and pestle. The solid material was then calcined at 300°C for 14 h, using a temperature ramp of 2°C/min in a gravity convection oven.
  • the catalyst was ground again using a mortar and a pestle, followed by calcination at 500°C for 14 h using the same temperature ramp and oven as before. Finally, an additional round of grind and calcination at 750°C for 14 h was performed. The catalyst was sieved to about 100 ⁇ to about 200 ⁇ . The material was analyzed by XRD allowing the identification of a-
  • the wide-angle data (WAXS) were collected on a STADI-P transmission mode diffractometer (Stoe & Cie GmbH, Darmstadt, Germany). The generator was operated at 40kV/40mA, powering a copper anode long-fine-focus Cu x-ray tube.
  • the diffractometer incorporates an incident-beam curved germanium-crystal monochromator, standard incident- beam slit system, and an image plate-position sensitive detector with an angular range of about 124° 2 ⁇ . Data were collected in transmission mode. Samples were gently ground by hand using a mortar & pestle to fine powder consistency, if necessary, before loading into the standard sample holder for the instrument.
  • Crystalline phases were identified using the most current powder diffraction database (from ICDD) using the Search/Match routines in Jade (Materials Data, Inc. v9.4.2).
  • SEM/EDS The dry powders were dispersed onto a double sided copper or carbon tape which had been mounted onto a metal scanning electron microscope (SEM) substrate. Each specimen was coated with Au/Pd for approximately 65-80 s using a Gatan Alto 2500 Cryo preparation chamber.
  • EDS imaging & energy dispersive spectroscopy (EDS) mapping were performed using either a Hitachi S-4700 FE-SEM or Hitachi S-5200 in-lens FE-SEM (Hitachi Ltd., Tokyo, Japan) both equipped for EDS with Bruker XFlash 30 mm2 SDD detectors (Quantax 2000 system with 5030 detector; Bruker Corp., Billerica, MA). EDS mapping was performed using an accelerating voltage of 10 kV in Analysis probe current mode. All maps were generated using Bruker Esprit VI.9 software within the Hypermap module.
  • Reactor - System A (0.2 mL scale reactor): Some of these conversions were carried out in a flow reactor system with a maximum catalyst bed volume of about 0.2 mL.
  • the system comprised temperature and mass flow controllers and was supplied with separate liquid and gas feeds that were mixed together before reaching the catalyst bed.
  • the gas feed was composed of molecular nitrogen (N 2 ) and helium (He), which was added as an internal standard for the gas chromatograph (GC) analysis.
  • the liquid feed was an aqueous solution of lactic acid (20 wt L- lactic acid) and was fed to the top of the reactor while controlling the pump pressure to about 360 psig to overcome any pressure drop from the catalyst bed. Quartz or stainless steel reactors with an aspect ratio (i.e., length/diameter) of 75 were used.
  • the feed was equilibrated for 1 hour, after which time the liquid sample was collected for 2.7 hours and analyzed at the end of the experiment by offline HPLC. During this time, the gas products were analyzed online twice by GC and reported as an average. Liquid products were analyzed by high performance liquid chromatography (HPLC) using an Agilent 1200 Series instrument (Agilent Technologies, Santa Clara, CA), a Supelcogel-H column (4.6 x 250 mm; Supelco, St. Louis, MO), and a diode-array and a refraction index (RI) detectors.
  • HPLC high performance liquid chromatography
  • the TCD-A column was an Rt-Q Bond (Restek Corp., Bellefonte, PA), having 26 m in length and an I.D. of 0.32 mm with a film thickness of 10 ⁇ and using a pre-column of 2 m.
  • the pressure was set to 150 kPa, with a split flow of 10 mL/min.
  • the column oven temperature was set to 100°C with a vale oven temperature of 50°C.
  • the flow was set to 5.0 mL/min, with a carrier gas of helium.
  • the TCD-B column was a Mol sieve MS5A (Restek Corp., Bellefonte, PA), having a length of 21 m and a film thickness of 10 ⁇ and using a pre-column of 2 m.
  • the pressure was set to 200 kPa, with a split flow of 10 mL/min.
  • the column oven temperature was set to 70°C with a vale oven temperature of 50°C.
  • the flow was set to 2.0 mL/min, with a carrier gas of argon.
  • the FID column was a RTx-624 (Restek, Bellefonte, PA), having a length of 28 m and an inner diameter of 0.25 mm with a film thickness of 14 mm and using a pre-column of 2 m.
  • the pressure was set to 100 kPa, with a split flow to 20 mL/min.
  • the column oven temperature was set to 45 °C with a vale oven temperature of 50°C.
  • Reactor - System B (1.6 mL scale reactor): Some of these conversions were carried out in a packed bed flow reactor system with a catalyst bed volume of about 1.6 mL.
  • a 13 inch (330 mm) long stainless steel glass lined tube (SGE Analytical Science Pty Ltd., Ringwood, Australia) with a 4.0 mm internal diameter (ID) was packed with glass wool (3 inch/76 mm bed length), topped by catalyst (1.6 cm 3 bed volume, 5 inch/127 mm bed length) to give an 2.55 cm 3 packed bed (8 inch/203 mm) and 1.6 cm 3 (5 inch/127 mm) of free space at the top of the reactor.
  • the tube was placed inside an aluminum block and placed in a clam shell furnace series 3210 (Applied Test Systems, Butler, PA) such as the top of the packed bed was aligned with the top of the aluminum block.
  • the reactor was set-up in a down-flow arrangement and was equipped with a Knauer Smartline 100 feed pump (Berlin, Germany), a Brooks 0254 gas flow controller (Hatfield, PA), a Brooks back pressure regulator, and a catch tank.
  • the clam shell furnace was heated such that the reactor wall temperature was kept constant at about 350°C during the course of the reaction.
  • the reactor was supplied with separate liquid and gas feeds that were mixed together before reaching the catalyst bed.
  • the gas feed was composed of molecular nitrogen (N 2 ) at about 360 psig and at a flow of 45 mL/min.
  • the liquid feed was an aqueous solution of lactic acid (20 wt L-lactic acid) and was fed at 0.045 mL/min (1.7 h "1 LHSV), giving a residence time of about 1 s (3,600 h " 1 GHSV) at STP conditions.
  • the gaseous stream was cooled and the liquids were collected in the catch tank for analysis by off-line HPLC using an Agilent 1100 system (Santa Clara, CA) equipped with a diode array detector (DAD) and a Waters Atlantis T3 column (Catalog # 186003748; Milford, MA) using methods generally known by those having ordinary skill in the art.
  • the gaseous stream was analyzed on-line by GC using an Agilent 7890 system (Santa Clara, CA) equipped with a FID detector and Varian CP-Para Bond Q column (Catalog # CP7351; Santa Clara, CA).
  • Table 1 sets forth parameters of the reactions with each catalyst that were carried out in the gas phase.
  • the reported yields were determined after 222 min (3 hours and 42 min) of reaction time and quartz reactors operating at 350°C were employed.
  • the 1.6 mL scale reactor was used, a stainless steel glass lined reactor was employed and the reported yields were determined after about 150 min to about 650 min.
  • the GHSV were as follows: 3,490 h "1 in Example 1; 3,535 h "1 in Examples 2, 10, 11, and 12; 3,414 h " 1 in Examples 3, 4, and 7; 3,566 h "1 in Examples 5 and 6; and 3,379 h "1 in Examples 8 and 9.
  • N.D means that the value was not determined.
  • Catalysts in Examples 10, 11, and 12 had lower selectivity than the catalysts according to the invention, demonstrating that the presence of two different metals is important for high selectivity to acrylic acid. Furthermore, at lower molar ratios of phosphorus (P) to metals (i.e., comparative Example 8), decarboxylation (formation of C0 2 ) is favored, whereas at higher molar ratios (i.e., comparative Examples 9 and 12), decarbonylation (formation of CO) seems to be preferred.

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