WO2006121770A2 - Hydrothermal treatment of phosphorus-modified zeolite catalysts - Google Patents
Hydrothermal treatment of phosphorus-modified zeolite catalysts Download PDFInfo
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- WO2006121770A2 WO2006121770A2 PCT/US2006/017206 US2006017206W WO2006121770A2 WO 2006121770 A2 WO2006121770 A2 WO 2006121770A2 US 2006017206 W US2006017206 W US 2006017206W WO 2006121770 A2 WO2006121770 A2 WO 2006121770A2
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- WIPO (PCT)
- Prior art keywords
- catalyst
- zeolite
- phosphorus
- zsm
- zeolite catalyst
- Prior art date
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- 239000003054 catalyst Substances 0.000 title claims abstract description 136
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical class O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 title claims abstract description 104
- 238000010335 hydrothermal treatment Methods 0.000 title description 2
- 239000010457 zeolite Substances 0.000 claims abstract description 101
- 229910021536 Zeolite Inorganic materials 0.000 claims abstract description 99
- 229910052698 phosphorus Inorganic materials 0.000 claims abstract description 56
- 239000011574 phosphorus Substances 0.000 claims abstract description 56
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 claims abstract description 49
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 37
- 229910001868 water Inorganic materials 0.000 claims abstract description 35
- 238000000034 method Methods 0.000 claims abstract description 34
- 238000010025 steaming Methods 0.000 claims abstract description 22
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 claims abstract description 17
- 229910052751 metal Inorganic materials 0.000 claims abstract description 15
- 239000002184 metal Substances 0.000 claims abstract description 15
- 238000005804 alkylation reaction Methods 0.000 claims abstract description 14
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 claims abstract description 12
- -1 phosphorus compound Chemical class 0.000 claims abstract description 10
- 125000003118 aryl group Chemical group 0.000 claims abstract description 9
- 150000001875 compounds Chemical class 0.000 claims abstract description 9
- 239000000377 silicon dioxide Substances 0.000 claims abstract description 9
- 239000002168 alkylating agent Substances 0.000 claims abstract description 8
- 229940100198 alkylating agent Drugs 0.000 claims abstract description 8
- 230000029936 alkylation Effects 0.000 claims abstract description 8
- 150000004945 aromatic hydrocarbons Chemical class 0.000 claims abstract description 7
- YXFVVABEGXRONW-UHFFFAOYSA-N Toluene Chemical compound CC1=CC=CC=C1 YXFVVABEGXRONW-UHFFFAOYSA-N 0.000 claims description 111
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical group OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 61
- 238000006243 chemical reaction Methods 0.000 claims description 17
- 239000008096 xylene Substances 0.000 claims description 15
- 238000007069 methylation reaction Methods 0.000 claims description 13
- 230000011987 methylation Effects 0.000 claims description 11
- CTQNGGLPUBDAKN-UHFFFAOYSA-N O-Xylene Chemical compound CC1=CC=CC=C1C CTQNGGLPUBDAKN-UHFFFAOYSA-N 0.000 claims description 6
- 238000001354 calcination Methods 0.000 claims description 6
- URLKBWYHVLBVBO-UHFFFAOYSA-N Para-Xylene Chemical group CC1=CC=C(C)C=C1 URLKBWYHVLBVBO-UHFFFAOYSA-N 0.000 description 34
- NBIIXXVUZAFLBC-UHFFFAOYSA-N Phosphoric acid Chemical compound OP(O)(O)=O NBIIXXVUZAFLBC-UHFFFAOYSA-N 0.000 description 18
- 239000002002 slurry Substances 0.000 description 14
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 11
- 239000000843 powder Substances 0.000 description 11
- 235000011007 phosphoric acid Nutrition 0.000 description 10
- 229910000147 aluminium phosphate Inorganic materials 0.000 description 9
- 229960004838 phosphoric acid Drugs 0.000 description 9
- 230000000694 effects Effects 0.000 description 7
- 239000007788 liquid Substances 0.000 description 7
- 239000000047 product Substances 0.000 description 6
- 229910052782 aluminium Inorganic materials 0.000 description 5
- 239000007789 gas Substances 0.000 description 5
- 238000010438 heat treatment Methods 0.000 description 5
- KKEYFWRCBNTPAC-UHFFFAOYSA-N Terephthalic acid Chemical compound OC(=O)C1=CC=C(C(O)=O)C=C1 KKEYFWRCBNTPAC-UHFFFAOYSA-N 0.000 description 4
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 239000011261 inert gas Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 230000004048 modification Effects 0.000 description 4
- 238000012986 modification Methods 0.000 description 4
- 239000000725 suspension Substances 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 239000002245 particle Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- 239000002253 acid Substances 0.000 description 2
- 238000001116 aluminium-27 magic angle spinning nuclear magnetic resonance spectrum Methods 0.000 description 2
- 239000007864 aqueous solution Substances 0.000 description 2
- 150000001491 aromatic compounds Chemical class 0.000 description 2
- 230000015572 biosynthetic process Effects 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000000571 coke Substances 0.000 description 2
- 239000013078 crystal Substances 0.000 description 2
- 239000008367 deionised water Substances 0.000 description 2
- 229910021641 deionized water Inorganic materials 0.000 description 2
- 230000008021 deposition Effects 0.000 description 2
- MNNHAPBLZZVQHP-UHFFFAOYSA-N diammonium hydrogen phosphate Chemical compound [NH4+].[NH4+].OP([O-])([O-])=O MNNHAPBLZZVQHP-UHFFFAOYSA-N 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 230000014509 gene expression Effects 0.000 description 2
- 150000002739 metals Chemical class 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 150000002938 p-xylenes Chemical class 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000001228 spectrum Methods 0.000 description 2
- 238000012360 testing method Methods 0.000 description 2
- 150000003738 xylenes Chemical class 0.000 description 2
- 238000001970 27Al magic angle spinning nuclear magnetic resonance spectroscopy Methods 0.000 description 1
- 238000005004 MAS NMR spectroscopy Methods 0.000 description 1
- MKYBYDHXWVHEJW-UHFFFAOYSA-N N-[1-oxo-1-(2,4,6,7-tetrahydrotriazolo[4,5-c]pyridin-5-yl)propan-2-yl]-2-[[3-(trifluoromethoxy)phenyl]methylamino]pyrimidine-5-carboxamide Chemical compound O=C(C(C)NC(=O)C=1C=NC(=NC=1)NCC1=CC(=CC=C1)OC(F)(F)F)N1CC2=C(CC1)NN=N2 MKYBYDHXWVHEJW-UHFFFAOYSA-N 0.000 description 1
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 1
- 230000002378 acidificating effect Effects 0.000 description 1
- 150000007513 acids Chemical class 0.000 description 1
- VXAUWWUXCIMFIM-UHFFFAOYSA-M aluminum;oxygen(2-);hydroxide Chemical compound [OH-].[O-2].[Al+3] VXAUWWUXCIMFIM-UHFFFAOYSA-M 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 1
- 239000011230 binding agent Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 229910052793 cadmium Inorganic materials 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000006555 catalytic reaction Methods 0.000 description 1
- 238000001833 catalytic reforming Methods 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 239000003153 chemical reaction reagent Substances 0.000 description 1
- 239000004927 clay Substances 0.000 description 1
- 229910052570 clay Inorganic materials 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 238000002425 crystallisation Methods 0.000 description 1
- 230000008025 crystallization Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000003795 desorption Methods 0.000 description 1
- 229910000388 diammonium phosphate Inorganic materials 0.000 description 1
- JIKVJUUIMIGAAO-UHFFFAOYSA-N diphenylphosphinous acid Chemical compound C=1C=CC=CC=1P(O)C1=CC=CC=C1 JIKVJUUIMIGAAO-UHFFFAOYSA-N 0.000 description 1
- 238000007323 disproportionation reaction Methods 0.000 description 1
- 150000002148 esters Chemical class 0.000 description 1
- 239000000835 fiber Substances 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000005470 impregnation Methods 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 238000006317 isomerization reaction Methods 0.000 description 1
- 238000000449 magic angle spinning nuclear magnetic resonance spectrum Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910017604 nitric acid Inorganic materials 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 239000003921 oil Substances 0.000 description 1
- 239000001301 oxygen Substances 0.000 description 1
- 230000000737 periodic effect Effects 0.000 description 1
- 150000003016 phosphoric acids Chemical class 0.000 description 1
- 229920000728 polyester Polymers 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- HBMJWWWQQXIZIP-UHFFFAOYSA-N silicon carbide Chemical compound [Si+]#[C-] HBMJWWWQQXIZIP-UHFFFAOYSA-N 0.000 description 1
- 238000007613 slurry method Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
- 239000010935 stainless steel Substances 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 238000004230 steam cracking Methods 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
Classifications
-
- 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
- B01J29/00—Catalysts comprising molecular sieves
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C2/00—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms
- C07C2/54—Preparation of hydrocarbons from hydrocarbons containing a smaller number of carbon atoms by addition of unsaturated hydrocarbons to saturated hydrocarbons or to hydrocarbons containing a six-membered aromatic ring with no unsaturation outside the aromatic ring
- C07C2/64—Addition to a carbon atom of a six-membered aromatic ring
- C07C2/66—Catalytic processes
-
- 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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
-
- 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
- B01J29/00—Catalysts comprising molecular sieves
- B01J29/04—Catalysts comprising molecular sieves having base-exchange properties, e.g. crystalline zeolites
- B01J29/06—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof
- B01J29/40—Crystalline aluminosilicate zeolites; Isomorphous compounds thereof of the pentasil type, e.g. types ZSM-5, ZSM-8 or ZSM-11, as exemplified by patent documents US3702886, GB1334243 and US3709979, respectively
-
- 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
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/10—After treatment, characterised by the effect to be obtained
- B01J2229/18—After treatment, characterised by the effect to be obtained to introduce other elements into or onto the molecular sieve itself
-
- 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
- B01J2229/00—Aspects of molecular sieve catalysts not covered by B01J29/00
- B01J2229/30—After treatment, characterised by the means used
- B01J2229/36—Steaming
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Definitions
- the invention relates generally to the alkylation of aromatic compounds and catalysts used for such alkylation.
- Para-xylene is a valuable substituted aromatic compound because of its great demand for its oxidation to terephthalic acid, a major component in forming polyester fibers and resins. It can be commercially produced from hydrotreating of naphtha (catalytic reforming), steam cracking of naphtha or gas oil, and toluene disproportionation.
- Thermodynamic equilibrium compositions of o-, m-, and p-xylenes may be around 25, 50 and 25 mole%, respectively, at a reaction temperature of about 500 0 C. Such toluene methylation may occur over a wide range of temperatures, however. Byproducts such as C9+ and other aromatic products can be produced by secondary alkylation of the xylene product.
- Para-xylene can be separated from mixed xylenes by a cycle of adsorption and isomerization. Such cycle may have to be repeated several times because of the low isomeric concentration in the equilibrium mixture.
- a high purity grade (99+%) p-xylene is desirable for its oxidation to terephthalic acid.
- the production cost for such a high purity grade p-xylene can be very high, however.
- a different method that employs crystallization techniques can be used and may be less expensive where the concentration of p-xylene is around 80% or higher in the initial xylene product. Thus, higher than equilibrium concentrations of p-xylene may be desirable.
- a significantly higher amount of p-xylene can be obtained in toluene methylation reaction if the catalyst has shape selective properties.
- Shape selective properties can be obtained in modified zeolite catalysts by narrowing zeolite pore opening size, inactivation of the external surface of the zeolite or controlling zeolite acidity. Toluene methylation may occur over modified ZSM-5 or ZSM-5-type zeolite catalyst giving xylene products containing significantly greater amounts of p-xylene than the thermodynamic concentration.
- FIGURE 1 shows 27 Al MAS NMR spectra of a P-modified ZSM-5 before steaming (spectrum a) and after steaming at 610 0 C for 13 days (spectrum b).
- ZSM-5-type is meant to refer to those zeolites that are isostructurally the same as ZSM-5 zeolites. Additionally, the expressions “ZSM-5" and “ZSM-5-type” may also be used herein interchangeably to encompass one another and should not be construed in a limiting sense. As used herein, catalytic activity can be expressed as the % moles of toluene converted with respect to the moles of toluene fed and can be defined as:
- Mole% p-Xylene Selectivity (X p /X mx ) x 100 (4) where, X p is the number of moles of p-xylene.
- selectivity for methanol may be expressed as:
- the ZSM-5 zeolite catalysts and their preparation are described in U.S. Patent No. 3,702,886, which is herein incorporated by reference.
- the ZSM-5 zeolite catalyst may include those having a silica/alumina molar ratio of from 200 or more, more particularly from about 250 or more, and still more particularly from about 280 to about 1000 or more, prior to modification.
- the zeolite may have a crystal particle size of 0.5 micron or more, more particularly from about 0.5 to about 5.0 microns, and still more particularly from about 0.5 to 1.0 microns.
- the starting ZSM-5 zeolite may be a NH 4 -ZSM-5 zeolite or an H-ZSM-5 zeolite, or other cation-exchanged ZSM-5 zeolite.
- the ZSM-5 zeolite may be modified by treating with phosphorus (P)- containing compounds.
- P phosphorus
- Such modified catalysts may be treated to provide a phosphorus content in an amount of from about 0.01 g P/g zeolite or more, more particularly from about 0.08 to about 0.15 g P/g zeolite, still more particularly from about 0.09 to about 0.13 g P/g zeolite.
- phosphorus-containing compounds may include, for example, phosphonic, phosphinous, phosphorus and phosphoric acids, salts and esters of such acids and phosphorous halides.
- phosphoric acid H 3 PO 4
- ammonium hydrogen phosphate (NH 4 ) 2 HPO 4 ) are particularly well suited for use as the phosphorus-containing compound to provide a catalyst for toluene methylation with shape selective properties to give high p-xylene concentration.
- the phosphorus treatment may be carried out by various techniques. This, may include slurry evaporation and wet incipient methods.
- slurry evaporation the phosphorus may be incorporated into the catalyst by preparing an aqueous slurry of the zeolite and an aqueous solution of the phosphorus compound. Heating of the slurry may be used to facilitate treatment of the zeolite and evaporation of liquids. Heating of the slurry to temperatures of 70 °C and higher is suitable. The slurry may also be stirred or agitated during this step to ensure uniform treatment.
- Heating the zeolite slurry to near complete evaporation of the liquid causes the formation of dough which can be dried or calcined to form powder or chunks.
- an aqueous solution of the phosphorus compound is added, such as by spraying, to dry the zeolite without forming a slurry.
- the dry zeolite which may be initially in the form of a powder, may be mixed with the phosphorus compound to form a dough. If necessary, water may be added to the mixture to facilitate formation of the zeolite dough.
- the dough may then be dried or calcined to obtain the phosphorus-modified zeolite powder or particles.
- the ZSM-5 zeolite structurally contains Al, Si and O, and may contain no or only trace amounts of any other metal (egs. B, Be, Ca, Cd, Co, Fe, Mg, etc.) other than phosphorus, including any metals of Groups IA, HA, IIIA, IVA, VA, VIA, VIIA 1 VIIIA, IB, HB, IIIB, IVB or VB of the Periodic Chart of the Elements that serve to enhance the para-selectivity properties of the catalyst.
- the ZSM-5 zeolite may undergo no treatment to provide any other such metals other than phosphorus to enhance the para-selective properties of the catalyst.
- the ZSM-5 zeolite may contain less than 0.05% by weight of the catalyst of such metal, more particularly, less than 0.01% by weight of the catalyst of such metal, and still more particularly less than 0.001% by weight of the catalyst of such metal.
- the catalyst may be bound or unbound.
- suitable binders include such materials as alumina, clay, and silica. Those techniques used for preparing the bound catalyst are well known in the art.
- the phosphorus-modified zeolite catalyst, bound or unbound may be calcined at a temperature of 400 0 C or more in an environment containing oxygen, typically air. Calcining may take place over time, typically from several minutes to one hour or more. Calcining may also take place by gradually increasing the temperature over time.
- the calcined P-modified ZSM-5 zeolite may have a BET surface area of 150-200 m 2 /g determined by N 2 adsorption techniques.
- the total pore volume may be in the range of 0.10-0.18 ml/g catalyst.
- the catalyst may have acidity showing broad peak(s) with peak maxima between 250°C and 350°C, as characterized by ammonia temperature programmed desorption (NH 3 -TPD) technique.
- the phosphorus-treated ZSM-5 zeolite catalyst is steamed at low or mild temperatures.
- the steaming may occur by contacting the zeolite catalyst with steam in the presence of hydrogen gas or air, or other inert gas. Steaming temperatures may range from about 150°C to about 25O 0 C, 300 0 C or 35O 0 C. This may be accomplished separately or in situ within the reactor, prior to any aromatic alkylation reaction or introduction of any reaction feed. Steaming may be carried out by contacting the catalyst in the presence of hydrogen or air or other inert gas. Steaming may be conducted from a few minutes to several hours. Such steaming of the phosphorus treated ZSM-5 zeolite causes no removal of aluminum (Al) from the zeolite framework as evidenced by Al MAS NMR study.
- the water may be fed at a ratio of from about 0.2 to 1.2 moles water per mole of aromatic hydrocarbon and alkylating agent, more particularly, from about 0.3 to about 0.9 mole water per mole of aromatic hydrocarbon and alkylating agent.
- the addition of water (or steam) as cofeed may be done in combination with or without hydrogen cofeed or with the introduction of any inert gas.
- the water cofeed may be fed into the reactor wherein the conditions are such that substantially no structural aluminum loss of the catalyst results due to the presence of such additional water within the reactor.
- the toluene and methanol feed may be premixed prior to introduction into the reactor as a single mixed feed stream.
- the feed may also contain small quantities of water, C9 + aromatics and other compounds.
- the liquid hourly space velocities presented herein, however, are based upon a toluene/methanol feed without the inclusion of any other components.
- the toluene/methanol molar ratio in the feed can range from 0.5 to 10.0, more particularly 1.0 to 5.0.
- a cofeed gas can be added with the toluene/methanol and steam.
- the cofeed gas may include hydrogen, nitrogen, helium or other inert gas.
- the cofeed gas may be provided at a molar ratio of less than about 10 with respect to toluene and methanol.
- the reactor temperature used herein referred as catalyst bed inlet temperature and a reactor temperature between 400 0 C and 700 °C is provided.
- the reactor inlet pressure may remain generally constant during the catalytic test run.
- the reactor inlet pressure may be about 10 psig or more.
- the reaction may be carried out in a fixed bed, continuous flow-type reactor in a down flow mode. Single or multi reactors in series and/or parallel are suitable for carrying out the reaction.
- the reactor temperature can be gradually increased. Initially, upon introduction of feed into the reactor, the reactor temperature may be about 200 0 C or above. The temperature may then be increased to the desired temperature. This temperature may be increased gradually at a rate of from about 0.1 °C/min to about 10 °C/min to provide a temperature of from about 400 °C to about 700 °C. [0026] The following examples better serve to illustrate the invention.
- phosphorus treated zeolite Catalysts A, B, and C were prepared using ZSM-5 zeolite powder as starting material. Phosphoric acid was used to treat the zeolite.
- the starting zeolite powder was a NH 4 - ZSM-5 zeolite powder having a SiO 2 ZAl 2 O 3 mole ratio of about 280.
- the crystal particle size of the starting zeolite powder was from about 0.5 to 1.0 micron.
- a phosphorus-modified ZSM-5 catalyst was made by a slurry method as follows.
- a slurry containing 450.0 g of NH 4 -ZSM-5 zeolite and 900 ml of deionized water was prepared in a 2000 ml beaker.
- the beaker was placed on a hot plate and the zeolite suspension was stirred using a mechanical (overhead) stirrer at 250-300 rpm.
- the temperature of the suspension was slowly raised to about 80-85 °C at which time phosphoric acid was added slowly.
- Phosphoric acid in an amount of 205.2 g (85 wt% in aqueous) was added to the slurry.
- the slurry temperature was further increased to between 95-100 °C and heating was continued until all liquid was evaporated to form a dough.
- the phosphoric-acid modified zeolite was calcined in a convection oven in air at the following temperature program: 90°C to 120 °C for four hours; at 340 °C to 360 0 C for three hours; and 520 °C to 530 °C under air for 10 hours.
- the calcined zeolite was then crushed and sized using 20 and 40 mesh screens.
- the phosphorus-modified ZSM-5 zeolite catalyst contained 9.01 g P/g zeolite.
- a phosphorus-modified ZSM-5 catalyst was made by impregnation method as follows. Zeolite powder in an amount of 50.01 g was placed in a 500 ml beaker. To this was slowly added 22.68 g of H 3 PO 4 acid (85% in aqueous) while mixing vigorously. Water was sprayed to moisten the zeolite powder and to form a dough. The catalyst dough was transferred to a ceramic dish and was calcined in a convection oven in air at the following temperature program: 90°C to 120 °C for four hours; at 340 °C to 360 °C for three hours; and 510 °C to 530 °C under air for 10 hours. The calcined zeolite was then crushed and sized using 20 and 40 mesh screens. The phosphorus-modified ZSM-5 zeolite catalyst contained 9.02 g P/g zeolite.
- a phosphorus-modified ZSM-5 bound catalyst was prepared as follows. A slurry containing 450.0 g of NHU-ZSM-5 zeolite and 900 ml of deionized water was prepared in a 2000 ml beaker. The beaker was placed on a hot plate and the zeolite suspension was stirred using a mechanical (overhead) stirrer at 250-300 rpm. The temperature of the suspension was slowly raised to about 80-85. °C at which time phosphoric acid was added slowly. A weighted 205.2 g of phosphoric acid (85 wt% in aqueous) was added to the slurry.
- the slurry temperature was further increased to between 95-100 °C and heating was continued until all liquid was evaporated to form a dough.
- the phosphoric-acid modified zeolite was calcined in a convection oven in air at the following temperature program: 9O 0 C to 120 °C for four hours; 340 °C to 360 °C for three hours; and 510 0 C to 520 0 C under air for 10 hours. A part of the calcined zeolite was then crushed and was sieved using 80 mesh screen.
- the P/ZSM- 5 catalyst contained 9.36 g P/g zeolite.
- the powder P/ZSM-5 was bound with 10 wt% alumina (commercial grade alumina, Alcoa, HiQ-40, pseudoboehmite type alumina).
- the alumina was first peptized with nitric acid (3-:l wt ratio) and then mixed with the P/ZSM-5 powder and mixed vigorously and sprayed with water to form a dough.
- the dough was calcined by using the same calcination temperature profile used for the P/ZSM-5.
- the calcined zeolite was then crushed and sized using 20 and 40 mesh screens for testing for reactions.
- the bound catalyst contained 8.4 g P/g catalyst.
- Catalyst A was used in toluene methylation.
- a catalyst charge of 5.4 ml of Catalyst A was placed within a V ⁇ -inch tubular reactor at about its midpoint. Layers of silicon carbide (SiC) were added to both ends of the catalyst bed.
- the reactor was tested for leaks in the system at 60-80 psig.
- the catalyst was then dried at 200 0 C under H 2 flow for at least one hour before use.
- the reactor feed was introduced without any further catalyst pretreatment, that is, without catalyst pre- steaming.
- Example 2 and 4 in order to examine the effect of catalyst steaming, the catalyst was first dried and then was steamed by flowing hydrogen gas containing H 2 O (10-12 mole%) at 200°C overnight.
- the feed was made by mixing toluene and methanol at a molar ratio of 4.5.
- the pre-mixed toluene/methanol liquid feed were introduced at a LHSV of 2.0-2.1 hr "1 .
- water was optionally added to the reactor feed, the water was introduced at a H 2 ⁇ /(toluene-t-methanol) molar ratio of 0.8 (see Examples 2 and 4).
- Example 7 The effect of catalyst steaming was examined on Catalyst B. In all cases, the catalyst was first dried at 200°C for an hour under hydrogen gas flow. In Example 7, the catalyst was not pre-steamed. In Example 8, after drying the catalyst it was then steamed overnight by flowing hydrogen gas containing from 10-12 mole% H 2 O at 200°C. The same reaction conditions as those of Example 4 were used. The results are summarized in Table 3 below.
- Example 8 Selectivity, mole% Catalyst B, Non-steamed, Catalyst B, Steamed at (Cofeed H2O) 200°C, (Cofeed H2O)
- Example 9 The effect of catalyst steaming was also examined on Catalyst C. In all cases, the catalyst was first dried at 200 0 C for an hour under hydrogen gas flow. In Example 9, the catalyst was not pre-steamed, whereas in Example 10, after drying the catalyst it was then steamed overnight by flowing hydrogen gas containing from 10- 12 mole% H 2 O at 200°C. The same reaction conditions as those of Example 4 using a water cofeed were used. The results are summarized in Table 4 below.
- Catalyst C Non-steamed, Catalyst C, Steamed at (Cofeed H2O) 200°C, (Cofeed H2O)
Abstract
A method of treating a ZSM-5-type zeolite catalyst is carried out by treating a ZSM-5 zeolite catalyst having a silica/alumina mole ratio of at least about 200 with a phosphorus compound. The phosphorus-treated ZSM-5 zeolite catalyst is calcined and steamed. Steaming of the catalyst is carried out at a temperature of less than about 300 °C. The phosphorus-treated ZSM-5 zeolite catalyst has less than 0.05 % by weight of the catalyst of any other metal other than phosphorus provided from any treatment of the ZSM-5 zeolite with a compound containing said other metal. The catalyst may be used in aromatic alkylation by contacting the catalyst with feed of an aromatic hydrocarbon and an alkylating agent within a reactor under reactor conditions suitable for aromatic alkylation. Water cofeed may be introduced water into the reactor during the aromatic alkylation reaction.
Description
HYDROTHERMAL TREATMENT OF PHOSPHORUS-MODIFIED ZEOLITE CATALYSTS
TECHNICAL FIELD
[0001] The invention relates generally to the alkylation of aromatic compounds and catalysts used for such alkylation.
BACKGROUND
[0002] Para-xylene is a valuable substituted aromatic compound because of its great demand for its oxidation to terephthalic acid, a major component in forming polyester fibers and resins. It can be commercially produced from hydrotreating of naphtha (catalytic reforming), steam cracking of naphtha or gas oil, and toluene disproportionation.
[0003] Alkylation of toluene with methanol, which is also known as toluene methylation, has been used in laboratory studies to produce para-xylene. Toluene methylation has been known to occur over acidic catalyst, particularly over zeolite or zeolite-type catalyst. In particular, ZSM-5-type zeolite, zeolite Beta and silicaamminophosphate (SAPO) catalysts have been used for this process. Generally, a thermodynamic equilibrium mixture of ortho (o)-, meta (m)- and para (p)-xylenes can be formed from the methylation of toluene, as is illustrated by the reaction below.
[0004] Thermodynamic equilibrium compositions of o-, m-, and p-xylenes may be around 25, 50 and 25 mole%, respectively, at a reaction temperature of about 500 0C. Such toluene methylation may occur over a wide range of temperatures, however. Byproducts such as C9+ and other aromatic products can be produced by secondary alkylation of the xylene product.
[0005] Para-xylene can be separated from mixed xylenes by a cycle of adsorption and isomerization. Such cycle may have to be repeated several times because of the low isomeric concentration in the equilibrium mixture. A high purity grade (99+%) p-xylene is desirable for its oxidation to terephthalic acid. The production cost for such a high purity grade p-xylene can be very high, however. A different method that employs crystallization techniques can be used and may be less expensive where the concentration of p-xylene is around 80% or higher in the initial xylene product. Thus, higher than equilibrium concentrations of p-xylene may be desirable.
[0006] A significantly higher amount of p-xylene can be obtained in toluene methylation reaction if the catalyst has shape selective properties. Shape selective properties can be obtained in modified zeolite catalysts by narrowing zeolite pore opening size, inactivation of the external surface of the zeolite or controlling zeolite acidity. Toluene methylation may occur over modified ZSM-5 or ZSM-5-type zeolite catalyst giving xylene products containing significantly greater amounts of p-xylene than the thermodynamic concentration.
[0007] In Kaeding, et al, Selective Alkylation of Toluene with Methanol to Produce para-Xylene, Journal of Catalysis, Vol. 67, pp. 159-174 (1981), a procedure of making a ZSM-5 catalyst by incorporating 5% phosphorus was described in which the catalyst was impregnated with a solution of diphenylphosphinous acid in toluene. The ZSM-5 catalyst thus modified showed toluene methylation activity with 84-90% para isomer in the xylene product. In another procedure, a catalyst was modified by incorporating 8.51% phosphorus from an aqueous phosphoric acid reagent. The catalyst showed p-xylene selectivity as high as 97%, however, the catalyst showed a decreasing activity within hours due to coke deposition.
[0008] Unfortunately, there are a number of technical hurdles for toluene methylation to be commercially successful and improvements are needed.
BRIEF DESCRIPTION OF THE DRAWINGS
[0009] For a more complete understanding of the present invention, reference is now made to the following descriptions taken in conjunction with the accompanying figures, in which:
[0010] FIGURE 1 shows 27Al MAS NMR spectra of a P-modified ZSM-5 before steaming (spectrum a) and after steaming at 610 0C for 13 days (spectrum b).
DETAILED DESCRIPTION
[0011] Modification of ZSM-5-type zeolite catalysts with phosphorus-containing compounds has been shown to yield significantly greater amounts of p-xylene than the thermodynamic equilibrium value in toluene methylation using unmodified catalysts. Such modification has been shown to provide selectivity for p-xylenes of greater than 80%. Although such phosphorus-treated ZSM-5 catalysts may have a high selectivity for p-xylene, they tend to deactivate at a very fast rate, for example, the catalyst may lose greater than 50% of its initial activity within a day. This may possibly be due to coke deposition on the catalyst.
[0012] As used herein, the expression "ZSM-5-type" is meant to refer to those zeolites that are isostructurally the same as ZSM-5 zeolites. Additionally, the expressions "ZSM-5" and "ZSM-5-type" may also be used herein interchangeably to encompass one another and should not be construed in a limiting sense. As used herein, catalytic activity can be expressed as the % moles of toluene converted with respect to the moles of toluene fed and can be defined as:
Mole% Toluene Conversion = [(T; - T0)ATj] x 100 (2) where, T; is the number of moles of toluene fed and T0 is the number of moles toluene unreacted. As used herein, selectivity for mixed-xylenes may be expressed as:
Mole% Mixed Xylene Selectivity = [Xmx/(Tj-T0)] x 100 (3) where, Xmx is the number of moles of total (o-, m- or p-) xylenes in the product. As used herein, selectivity for p-xylene may be expressed as:
Mole% p-Xylene Selectivity = (Xp/Xmx) x 100 (4) where, Xp is the number of moles of p-xylene.
As used herein, selectivity for methanol may be expressed as:
Mole% Methanol Selectivity = [Xrax/(Mi-M0)] x 100 (5) where, Xmx is the number of moles of mixed-xylenes, Mj is the number of moles of methanol fed and M0 is the number of moles methanol unreacted.
[0013] The ZSM-5 zeolite catalysts and their preparation are described in U.S. Patent No. 3,702,886, which is herein incorporated by reference. In the present invention, the ZSM-5 zeolite catalyst may include those having a silica/alumina molar ratio of from 200 or more, more particularly from about 250 or more, and still more particularly from about 280 to about 1000 or more, prior to modification. The zeolite may have a crystal particle size of 0.5 micron or more, more particularly from about 0.5 to about 5.0 microns, and still more particularly from about 0.5 to 1.0 microns. The starting ZSM-5 zeolite may be a NH4-ZSM-5 zeolite or an H-ZSM-5 zeolite, or other cation-exchanged ZSM-5 zeolite.
[0014] The ZSM-5 zeolite may be modified by treating with phosphorus (P)- containing compounds. Such modified catalysts may be treated to provide a phosphorus content in an amount of from about 0.01 g P/g zeolite or more, more particularly from about 0.08 to about 0.15 g P/g zeolite, still more particularly from about 0.09 to about 0.13 g P/g zeolite. Such phosphorus-containing compounds may include, for example, phosphonic, phosphinous, phosphorus and phosphoric acids, salts and esters of such acids and phosphorous halides. In particular, phosphoric acid (H3PO4) and ammonium hydrogen phosphate ((NH4)2HPO4) are particularly well suited for use as the phosphorus-containing compound to provide a catalyst for toluene methylation with shape selective properties to give high p-xylene concentration.
[0015] The phosphorus treatment may be carried out by various techniques. This, may include slurry evaporation and wet incipient methods. In slurry evaporation, the phosphorus may be incorporated into the catalyst by preparing an aqueous slurry of the zeolite and an aqueous solution of the phosphorus compound. Heating of the slurry may be used to facilitate treatment of the zeolite and evaporation of liquids. Heating of the slurry to temperatures of 70 °C and higher is suitable. The slurry may also be stirred or agitated during this step to ensure uniform treatment. Heating the zeolite slurry to near complete evaporation of the liquid causes the formation of dough which can be dried or calcined to form powder or chunks. [0016] In the wet incipient method, an aqueous solution of the phosphorus compound is added, such as by spraying, to dry the zeolite without forming a slurry. The dry zeolite, which may be initially in the form of a powder, may be mixed with the phosphorus compound to form a dough. If necessary, water may be added to the
mixture to facilitate formation of the zeolite dough. The dough may then be dried or calcined to obtain the phosphorus-modified zeolite powder or particles. [0017] It should be noted that the ZSM-5 zeolite structurally contains Al, Si and O, and may contain no or only trace amounts of any other metal (egs. B, Be, Ca, Cd, Co, Fe, Mg, etc.) other than phosphorus, including any metals of Groups IA, HA, IIIA, IVA, VA, VIA, VIIA1 VIIIA, IB, HB, IIIB, IVB or VB of the Periodic Chart of the Elements that serve to enhance the para-selectivity properties of the catalyst. The ZSM-5 zeolite may undergo no treatment to provide any other such metals other than phosphorus to enhance the para-selective properties of the catalyst. If a metal other than phosphorus is provided from any such treatment, the ZSM-5 zeolite may contain less than 0.05% by weight of the catalyst of such metal, more particularly, less than 0.01% by weight of the catalyst of such metal, and still more particularly less than 0.001% by weight of the catalyst of such metal.
[0018] The catalyst may be bound or unbound. Examples of suitable binders include such materials as alumina, clay, and silica. Those techniques used for preparing the bound catalyst are well known in the art. The phosphorus-modified zeolite catalyst, bound or unbound, may be calcined at a temperature of 400 0C or more in an environment containing oxygen, typically air. Calcining may take place over time, typically from several minutes to one hour or more. Calcining may also take place by gradually increasing the temperature over time.
[0019] The calcined P-modified ZSM-5 zeolite may have a BET surface area of 150-200 m2/g determined by N2 adsorption techniques. The total pore volume may be in the range of 0.10-0.18 ml/g catalyst. The catalyst may have acidity showing broad peak(s) with peak maxima between 250°C and 350°C, as characterized by ammonia temperature programmed desorption (NH3-TPD) technique.
[0020] The phosphorus-treated ZSM-5 zeolite catalyst is steamed at low or mild temperatures. The steaming may occur by contacting the zeolite catalyst with steam in the presence of hydrogen gas or air, or other inert gas. Steaming temperatures may range from about 150°C to about 25O0C, 3000C or 35O0C. This may be accomplished separately or in situ within the reactor, prior to any aromatic alkylation reaction or introduction of any reaction feed. Steaming may be carried out by contacting the catalyst in the presence of hydrogen or air or other inert gas. Steaming may be conducted from a few minutes to several hours. Such steaming of the phosphorus
treated ZSM-5 zeolite causes no removal of aluminum (Al) from the zeolite framework as evidenced by Al MAS NMR study.
[0021] Where phosphorus-treated ZSM-5 zeolite catalysts have been steamed according to the present invention, increased catalyst activity and selectivity for the catalyst in aromatic alkylation reactions has been observed. This is compared to the same phosphorus-treated ZSM-5 zeolite catalyst used under the same or similar reaction conditions that has not been steamed or where steaming is conducted at higher temperatures. Increases in para-selectivity have been observed, as well as increases in selectivity of the alkylating agent. In particular, significant increases in methanol selectivity have been observed for the catalyst when used in toluene methylation reactions.
[0022] Further increases in selectivity and catalyst activity of the mildly steamed phosphorus-modified ZSM-5 zeolite catalyst can also be achieved by additionally introducing water or steam into the reactor as cofeed during the alkylation reaction. Such introduction of steam during the reaction has been described in copending U.S. Patent Application Serial No. 10/675,780, filed September 30, 2003, which is herein incorporated by reference. The water introduced into the reactor may be fed into the reactor at a ratio of from about 0.1 or more, and may be less than about 10 moles water per mole of aromatic hydrocarbon and alkylating agent, more particularly, from about 0.3 to about 5, 6 or 7 moles water per mole of aromatic hydrocarbon and alkylating agent. In certain instances, the water may be fed at a ratio of from about 0.2 to 1.2 moles water per mole of aromatic hydrocarbon and alkylating agent, more particularly, from about 0.3 to about 0.9 mole water per mole of aromatic hydrocarbon and alkylating agent. The addition of water (or steam) as cofeed may be done in combination with or without hydrogen cofeed or with the introduction of any inert gas. The water cofeed may be fed into the reactor wherein the conditions are such that substantially no structural aluminum loss of the catalyst results due to the presence of such additional water within the reactor.
[0023] In carrying out the aromatic alkylation reactions with the P-modified ZSM-5 catalyst with or without catalyst steaming and both with and without water cofeed, the toluene and methanol feed may be premixed prior to introduction into the reactor as a single mixed feed stream. The feed may also contain small quantities of water, C9 + aromatics and other compounds. The liquid hourly space velocities presented herein,
however, are based upon a toluene/methanol feed without the inclusion of any other components. The toluene/methanol molar ratio in the feed can range from 0.5 to 10.0, more particularly 1.0 to 5.0. Optionally, a cofeed gas can be added with the toluene/methanol and steam. The cofeed gas may include hydrogen, nitrogen, helium or other inert gas. The cofeed gas may be provided at a molar ratio of less than about 10 with respect to toluene and methanol. The reactor temperature used herein referred as catalyst bed inlet temperature and a reactor temperature between 400 0C and 700 °C is provided.
[0024] The reactor inlet pressure may remain generally constant during the catalytic test run. The reactor inlet pressure may be about 10 psig or more. [0025] The reaction may be carried out in a fixed bed, continuous flow-type reactor in a down flow mode. Single or multi reactors in series and/or parallel are suitable for carrying out the reaction. The reactor temperature can be gradually increased. Initially, upon introduction of feed into the reactor, the reactor temperature may be about 200 0C or above. The temperature may then be increased to the desired temperature. This temperature may be increased gradually at a rate of from about 0.1 °C/min to about 10 °C/min to provide a temperature of from about 400 °C to about 700 °C. [0026] The following examples better serve to illustrate the invention.
EXAMPLES
[0027] Using the procedure described below, phosphorus treated zeolite Catalysts A, B, and C were prepared using ZSM-5 zeolite powder as starting material. Phosphoric acid was used to treat the zeolite. The starting zeolite powder was a NH4- ZSM-5 zeolite powder having a SiO2ZAl2O3 mole ratio of about 280. The crystal particle size of the starting zeolite powder was from about 0.5 to 1.0 micron.
Catalyst A
[0028] A phosphorus-modified ZSM-5 catalyst was made by a slurry method as follows. A slurry containing 450.0 g of NH4-ZSM-5 zeolite and 900 ml of deionized water was prepared in a 2000 ml beaker. The beaker was placed on a hot plate and the zeolite suspension was stirred using a mechanical (overhead) stirrer at 250-300 rpm. The temperature of the suspension was slowly raised to about 80-85 °C at which time phosphoric acid was added slowly. Phosphoric acid in an amount of 205.2 g (85 wt% in aqueous) was added to the slurry. The slurry temperature was further increased to between 95-100 °C and heating was continued until all liquid was evaporated to form a dough. The phosphoric-acid modified zeolite was calcined in a convection oven in air at the following temperature program: 90°C to 120 °C for four hours; at 340 °C to 360 0C for three hours; and 520 °C to 530 °C under air for 10 hours. The calcined zeolite was then crushed and sized using 20 and 40 mesh screens. The phosphorus-modified ZSM-5 zeolite catalyst contained 9.01 g P/g zeolite.
Catalyst B
[0029] A phosphorus-modified ZSM-5 catalyst was made by impregnation method as follows. Zeolite powder in an amount of 50.01 g was placed in a 500 ml beaker. To this was slowly added 22.68 g of H3PO4 acid (85% in aqueous) while mixing vigorously. Water was sprayed to moisten the zeolite powder and to form a dough. The catalyst dough was transferred to a ceramic dish and was calcined in a convection oven in air at the following temperature program: 90°C to 120 °C for four hours; at 340 °C to 360 °C for three hours; and 510 °C to 530 °C under air for 10 hours. The calcined zeolite was then crushed and sized using 20 and 40 mesh screens. The phosphorus-modified ZSM-5 zeolite catalyst contained 9.02 g P/g zeolite.
Catalyst C
[0030] A phosphorus-modified ZSM-5 bound catalyst was prepared as follows. A slurry containing 450.0 g of NHU-ZSM-5 zeolite and 900 ml of deionized water was prepared in a 2000 ml beaker. The beaker was placed on a hot plate and the zeolite suspension was stirred using a mechanical (overhead) stirrer at 250-300 rpm. The temperature of the suspension was slowly raised to about 80-85. °C at which time
phosphoric acid was added slowly. A weighted 205.2 g of phosphoric acid (85 wt% in aqueous) was added to the slurry. The slurry temperature was further increased to between 95-100 °C and heating was continued until all liquid was evaporated to form a dough. The phosphoric-acid modified zeolite was calcined in a convection oven in air at the following temperature program: 9O0C to 120 °C for four hours; 340 °C to 360 °C for three hours; and 510 0C to 520 0C under air for 10 hours. A part of the calcined zeolite was then crushed and was sieved using 80 mesh screen. The P/ZSM- 5 catalyst contained 9.36 g P/g zeolite. The powder P/ZSM-5 was bound with 10 wt% alumina (commercial grade alumina, Alcoa, HiQ-40, pseudoboehmite type alumina). The alumina was first peptized with nitric acid (3-:l wt ratio) and then mixed with the P/ZSM-5 powder and mixed vigorously and sprayed with water to form a dough. The dough was calcined by using the same calcination temperature profile used for the P/ZSM-5. The calcined zeolite was then crushed and sized using 20 and 40 mesh screens for testing for reactions. The bound catalyst contained 8.4 g P/g catalyst.
Example 1-4
[0031] Catalyst A was used in toluene methylation. A catalyst charge of 5.4 ml of Catalyst A was placed within a V^-inch tubular reactor at about its midpoint. Layers of silicon carbide (SiC) were added to both ends of the catalyst bed. The reactor was tested for leaks in the system at 60-80 psig. The catalyst was then dried at 2000C under H2 flow for at least one hour before use. In Examples 1 and 3, the reactor feed was introduced without any further catalyst pretreatment, that is, without catalyst pre- steaming. In Examples 2 and 4, however, in order to examine the effect of catalyst steaming, the catalyst was first dried and then was steamed by flowing hydrogen gas containing H2O (10-12 mole%) at 200°C overnight. The feed was made by mixing toluene and methanol at a molar ratio of 4.5. The pre-mixed toluene/methanol liquid feed were introduced at a LHSV of 2.0-2.1 hr"1. Where water was optionally added to the reactor feed, the water was introduced at a H2θ/(toluene-t-methanol) molar ratio of 0.8 (see Examples 2 and 4). Hydrogen gas was added to the feed at a predetermined rate to maintain a selected H2/(toluene+methanoi) molar ratio of 7-8. The catalyst bed inlet temperature was raised to approximately 55O0C. When catalyst performance reached steady conditions, conversion and selectivity were calculated using Equations
2-4. Conversion and selectivity obtained in Examples 1-4 are presented below in Table 1.
TABLE 1
Examples 5-6
[0032] The effect of catalyst steaming temperature was examined on Catalyst A. In all cases, the catalyst was first dried at 200°C for an hour under hydrogen gas flow. The catalyst was then steamed overnight by flowing hydrogen gas containing from 10-12 mole% H2O at either 200°C, 3000C or 500°C. The same reaction conditions as those of Example 4 were used. The results are summarized in Table 2 below.
TABLE 2
Examples 7-8
[0033] The effect of catalyst steaming was examined on Catalyst B. In all cases, the catalyst was first dried at 200°C for an hour under hydrogen gas flow. In Example 7, the catalyst was not pre-steamed. In Example 8, after drying the catalyst it was then steamed overnight by flowing hydrogen gas containing from 10-12 mole% H2O at 200°C. The same reaction conditions as those of Example 4 were used. The results are summarized in Table 3 below.
TABLE 3
Conversion/ Example 7 Example 8 Selectivity, mole% Catalyst B, Non-steamed, Catalyst B, Steamed at (Cofeed H2O) 200°C, (Cofeed H2O)
Xϊoluene 12.1 15.0
^Mixed-Xylenes 97.0 97.0
Sp-Xylene 91.4 90.0
^Methanol 62.7 73.1
Examples 9-10
[0034] The effect of catalyst steaming was also examined on Catalyst C. In all cases, the catalyst was first dried at 2000C for an hour under hydrogen gas flow. In Example 9, the catalyst was not pre-steamed, whereas in Example 10, after drying the catalyst it was then steamed overnight by flowing hydrogen gas containing from 10- 12 mole% H2O at 200°C. The same reaction conditions as those of Example 4 using a water cofeed were used. The results are summarized in Table 4 below.
TABLE 4
Conversion/ Example 9 Example 10 Selectivity
Catalyst C, Non-steamed, Catalyst C, Steamed at (Cofeed H2O) 200°C, (Cofeed H2O)
XToluene 13.4 14.2
^Mixed-Xylenes 98.2 98.2
Sp-Xylene 96.3 95.8
^Methanol 64.8 66.0
Example 11
[0035] The 27Al MAS NMR spectra were recorded for P-modified ZSM-5 catalyst (e.g., catalyst A). Steaming was carried out by placing about 5.4 ml of sized catalyst (20-40 mesh) in a stainless steel reactor. The catalyst was dried at 2000C under H2 or N2 flow at 50 cc/min for at least one hour. The gas flow was increased to 459 cc/min, and liquid water was introduced at 0.04 ml/min through a vaporizer at 2000C. The reactor temperature was then increased to desired steaming temperature and steaming was continued usually for overnight. Referring to Figure 1, Al MAS-NMR spectrum of non-steamed catalyst showed a weak peak at 50-55 ppm attributed to the zeolite framework aluminum. A strong peak was observed at around -12 ppm assigned to extraframework aluminum (EFAl). The 27Al MAS NMR of catalyst A after steaming at 610 0C (for 13 days), showed no or little change in framework Al or EFAl. [0036] While the invention has been shown in only some of its forms, it should be apparent to those skilled in the art that it is not so limited, but is susceptible to various changes and modifications without departing from the scope of the invention. Accordingly, it is appropriate that the appended claims be construed broadly and in a manner consistent with the scope of the invention.
Claims
1. A method of treating a ZSM-5-type zeolite catalyst comprising:
treating a ZSM-5 zeolite catalyst having a silica/alumina mole ratio of at least about 200 with a phosphorus compound;
calcining the phosphorus treated ZSM-5 zeolite catalyst; and
steaming the phosphorus treated ZSM-5 zeolite catalyst with steam at a temperature of less than about 300°C, and wherein the phosphorus treated ZSM-5 zeolite catalyst has less than 0.05% by weight of the catalyst of any other metal other than phosphorus provided from any treatment of the ZSM-5 zeolite with a compound containing said other metal.
2. The method of claim 1, wherein:
the phosphorus treated ZSM-5 zeolite catalyst has a phosphorus content of at least about O.O&g P/g zeolite.
3. The method of claim 1 , wherein:
the phosphorus treated ZSM-5 zeolite catalyst has a phosphorus content of from at least about 0.08g P/g zeolite to about 0.15g P/g zeolite.
4. The method of claim 1 , wherein:
the ZSM-5 zeolite catalyst has a silica/alumina mole ratio of at least about 250.
5. The method of claim 1 , wherein:
the phosphorus treated ZSM-5 zeolite catalyst is steamed at a temperature of less than about 250°C.
6. The method of claim 1, wherein:
the phosphorus treated ZSM-5 zeolite catalyst is steamed at a temperature of from about 1500C to about 25O0C.
7. The method of claim 1, wherein:
the phosphorus treated ZSM-5 zeolite catalyst is calcined at a temperature of at least about 300 0C.
8. A method of preparing an alkyl aromatic product comprising:
treating a ZSM-5 zeolite catalyst having a silica/alumina mole ratio of at least about 200 with a phosphorus compound;
calcining the phosphorus treated ZSM-5 zeolite catalyst; and
steaming the phosphorus treated ZSM-5 zeolite catalyst with steam at a temperature of less than about 300°C, and wherein the phosphorus treated ZSM-5 zeolite catalyst has less than 0.05% by weight of the catalyst of any other metal other than phosphorus provided from any treatment of the ZSM-5 zeolite with a compound containing said other metal;
contacting the catalyst with feed of an aromatic hydrocarbon and an alkylating agent within a reactor under reactor conditions suitable for aromatic alkylation; and
introducing water cofeed into the reactor during the aromatic alkylation reaction.
9. The method of claim 8, wherein:
the aromatic hydrocarbon is toluene and the alkylating agent is methanol.
10. The method of claim 8, wherein:
the phosphorus treated ZSM-5 zeolite catalyst has a phosphorus content of at least about 0.08g P/g zeolite.
11. The method of claim 8, wherein:
the phosphorus treated ZSM-5 zeolite catalyst has a phosphorus content of from at least about 0.08g P/g zeolite to about 0.15g P/g zeolite.
12. The method of claim 8, wherein:
the ZSM-5 zeolite catalyst has a silica/alumina mole ratio of at least about 250.
13. The method of claim 8, wherein:
the phosphorus treated ZSM-5 zeolite catalyst is steamed at a temperature of less than about 250°C.
14. The method of claim 8, wherein:
the phosphorus treated ZSM-5 zeolite catalyst is steamed at a temperature of from about 150°C to about 250°C.
15. The method of claim 8 , wherein:
the phosphorus treated ZSM-5 zeolite catalyst is calcined at a temperature of at least about 300 °C.
16. A method of preparing a xylene product comprising :
treating a ZSM-5 zeolite catalyst having a silica/alumina mole ratio of at least about 250 with a phosphorus compound to provide a phosphorus content of from about 0.08gP/g zeolite to about 0.15g P/g zeolite ;
calcining the phosphorus treated ZSM-5 zeolite catalyst at a temperature of from about 300 °C and above;
steaming the phosphorus treated ZSM-5 zeolite catalyst with steam at a temperature of from about 150°C about 250°C, and wherein the phosphorus treated ZSM-5 zeolite catalyst has less than 0.05% by weight of the catalyst of any other metal other than phosphorus provided from any treatment of the ZSM-5 zeolite with a compound containing said other metal;
contacting the catalyst with a feed of toluene and methanol within a reactor under reactor conditions suitable for toluene methylation; and
introducing water cofeed into the reactor during the reaction.
17. The method of claim 16, wherein:
the cofeed water is fed into the reactor at from about 0.2 mole to less than about 10 moles water per mole of toluene and methanol feed.
18. The method of claim 16, wherein:
the cofeed water is fed into the reactor at 0.3 mole to about 7 moles water per mole of toluene and methanol feed.
19. The method of claim 16, wherein:
the reactor has a catalyst bed inlet temperature maintained at less than 700 0C.
20. The method of claim 16, wherein:
the toluene/methanol feed has a toluene/methanol molar ratio of from about 1 :2 to about 10:1.
Priority Applications (5)
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AT06759065T ATE493372T1 (en) | 2005-05-05 | 2006-05-05 | HYDROTHERMAL TREATMENT OF PHOSPHORUM-MODIFIED ZEOLITE CATALYSTS |
KR1020077027725A KR101287237B1 (en) | 2005-05-05 | 2006-05-05 | Hydrothermal treatment of phosphorus-modified zeolite catalysts |
CN2006800150303A CN101184710B (en) | 2005-05-05 | 2006-05-05 | Hydrothermal treatment of phosphorus-modified zeolite catalysts |
EP06759065A EP1877184B1 (en) | 2005-05-05 | 2006-05-05 | Hydrothermal treatment of phosphorus-modified zeolite catalysts |
DE602006019226T DE602006019226D1 (en) | 2005-05-05 | 2006-05-05 | HYDROTHERMAL TREATMENT OF PHOSPHORMODIFIED ZEOLITE CATALYSTS |
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JP2016506863A (en) * | 2013-01-21 | 2016-03-07 | ビーピー ケミカルズ リミテッドBp Chemicals Limited | Method for treating zeolite catalyst |
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DE602006019226D1 (en) | 2011-02-10 |
KR101287237B1 (en) | 2013-07-17 |
US20080009406A1 (en) | 2008-01-10 |
EP1877184B1 (en) | 2010-12-29 |
WO2006121770A3 (en) | 2007-12-27 |
ES2356498T3 (en) | 2011-04-08 |
CN101184710B (en) | 2011-05-18 |
EP1877184A4 (en) | 2008-11-05 |
CN101184710A (en) | 2008-05-21 |
KR20080013953A (en) | 2008-02-13 |
US7304194B2 (en) | 2007-12-04 |
US7576026B2 (en) | 2009-08-18 |
EP1877184A2 (en) | 2008-01-16 |
ATE493372T1 (en) | 2011-01-15 |
US20060252633A1 (en) | 2006-11-09 |
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