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Crystalline zirconium phosphates with zeolite-like porous structure
Patent
Manufacture
of zeolite
4A from
R.A. Puerto; J.F. Benito Foret S.A. U.S. 5,401,487, Mar. 28, 1995;
Appl.
bauxite
Dec.
Crystalline zirconium rous structures
3, 1991
The process includes digesting bauxite at atmospheric pressure and 90-100°C using a 211% NaOH solution; filtering the product obtained; passing the filtrate through a bed of hydrophobic resin to remove organic material; reacting the treated filtrate at 60-70°C with an alkaline solution of silica with a SiOdNa,O molar ratio of 2.0-2.5 to obtain a sodium aluminosilicate gel; crystallizing the gel to produce the desired zeolite; treating the residue from the filtration step with H,SO, to recover metals in the form of an aqueous metal sulfate and recycling the silica residue for preparation of the alkaline solution of the silica used in the reaction step; and recycling the mother liquor remaining after crystallization of the gel to the digestion step.
Manufacture
of zeolite
crystal
Appl.
Oct.
12,
A process for the manufacture of zeolite crystal membranes comprises impregnating AI,O, substrates with slurries containing zeolite crystals in binder solutions; optionally washing and drying the substrates; and hydrothermally reacting the substrates containing adhered zeolite crystals by immersion in a solution containing zeolite precursor raw materials. The binders may be water glass or SiO, sol.
of A-type
K. Inoe; S. Tsunematsu; Kogyo Gijutsuin Jpn. Kokai Tokkyo Koho 1993
zeolites H. Yamada Apr.
of alkali
R.B. Edwards; Crosfield Ltd. PCT Int. Appl.
metal
25, 1995;
aluminosilicates
Appl.
Oct.
4,
of zeolite
P. Graham 95,12,546,
May
11, 1995;
U.K.
Appl.
Nov.
2, 1993
A process for the manufacture of alkali metal aluminosilicates of zeolite P-type comprises mixing and reacting a sodium silicate solution in a first reaction zone with a sodium aluminate solution and NaOH to form an amorphous aluminosilicate having the general formula (2.5-7.5) Na,O: (2.0-3.0) SiO,: AI,O,: (80250) H,O and a supersaturated mother liquor; transferring the mixture, having degree of crystallinity ~30, preferably 20%, from the first reaction zone to a second reaction zone and allowing the material to convert fully into P-type zeolite; filtering; washing; and drying the resulting product having the general formula M,,, 0: AI,O,: (2.0-2.66) SiO,: y H,O.
Synthetic
ZSM-5
Y. Suzuki; Nok Corp. Jpn. Kokai 1993
T. Nanba Tokkyo
zeolite
Koho
crystals
95,118,010,
and their
May
9, 1995;
Apr.
zeolite-like
18, 1995;
Appl.
po-
July
22,
Crystalline zirconium phosphates with zeolite-like porous structures have formulas: NH,Zr,(PO,),: mH,O (0 s m 5 2), HZr,(PO,), and HZr,(PO,),: mH,O (0 < m 5 2), specified X-ray diffraction patterns, and oxide mol ratios 4Zr0,:3P,O,. The phosphates can be used for ion exchangers (cation exchangers), adsorbents, catalysts, and porous ceramic materials.
CATALYSIS
F.C. Wilhelm; T.R. Gaffney; G.E. Parris et al. Air Products and Chemicals, Inc. Can. Pat. Appl. 2,126,834, Jan. 2, 1995; U.S. Appl.
manufacture
Appl.
Oct.
15,
Square pillar-like ZSM-5 zeolite crystals are manufactured from aqueous reaction mixtures containing lower alkoxysilanes as silica sources, alumina sources, alkali metal sources, and tetrapropylammonium salts as crystallization agents by hydrothermal reaction in an autoclave at 160-200°C. The crystals have large apparent surface area.
July
1, 1993
A nonequilibrium distribution of methylamines is prepared by the catalyzed reaction of methanol and/or dimethyl ether with ammonia followed by the catalytic reforming of the methylamine-containing feedstock produced. The process selectively affords a reaction product enriched in monoand dimethylamines and low in trimethylamine, at high conversion of methanol or dimethyl ether. The low trimethylamine selectivity at high conversion is achieved by the use of a microporous zeolite, preferably chabazite, catalyst having a geometric selectivity index ~3 and a shape selectivity index >5.
Integrated
95,109,117,
A process for the manufacture of A-type zeolites comprises heating mixtures containing fly ash and solid NaOH at 90-180°C for 260 min, preferably at IOO-150°C for 5-20 h. to obtain a slurry; mixing with more NaOH and water; and hydrothermally reacting the slurry. The mixtures may contain 5fl-I:2 (weight ratio) of fly ash and solid NaOH. The fly ash may contain 215% AI,O, and 250% SiO,.
Manufacture P-type
K. Ito; Y. Takada; K. Kunibe Daiichi Kigenso Kagaku Kogyo Jpn. Kokai Tokkyo Koho 95,101,711, 1993
with
Chabazite catalysts for the preparation of methylamines from ammonia and methanol or dimethyl ether
membranes
A. Saji; H. Noda; K. Hashimoto et al. Chubu Electric Power; Ngk Insulators Ltd. Jpn. Kokai Tokkyo Koho ~5,109,116, Apr. 25, 1995; 1993
Manufacture
phosphates
report
catalytic
cracking
and olefin
cess M.C. Kerbv: R. Bearden. Jr.: S.M. Davis Exxon Res’earch and Engineering Co. Eur. Pat. Appl. 654,519; 654,520; 654,521; U.S. Appls. Nov. 19, 1993
producing
654,523,
May
pro-
24, 1995;
A combined catalytic cracking and olefin production process uses a coked catalytic cracking catalyst as a dehydrogenation catalyst to dehydrogenate an alkane feed and form an olefin-rich product. Preferably the coked catalytic cracking catalyst has a carbon content of -0.2-10%. The method uses a staged back mixed regeneration system to form the dehydrogenation catalyst and to reactivate fully the deactivated cracking catalyst for reuse in the cracking reaction. The catalyst preferably comprises a crystalline tetrahedral framework oxide component, particularly zeolite 0.
Gasoline cracking
upgrading
process
D.L. Fletcher; T.L. Hilbert; Mobil Oil Corp. U.S. 5,413,696; 5,413,698,
by hydrodesulfurization
S.J.
McGovern
May
9, 1995;
and
et al. Appls.
Aug.
15, 1991
Low sulfur gasoline of relatively high octane number is produced from a catalytically cracked, sulfur-containing naphtha by hydrodesulfurization followed by treatment over an acidic catalyst comprising zeolite p. The treatment over the acidic catalyst in the second step restores the octane loss that takes place as a result of the hydrogenative treatment and results in a low sulfur gasoline product with an octane number comparable to that of the feed naphtha.
Epoxidation of olefins zeolite p catalyst
with
hydrogen
R.J. Saxton; J.G. Zajacek; G.L. Crocco Arco Chemical Technology L.P. U.S. 5,412,122, May 2, 1995; Appl. Dec.
peroxide
using
a
23, 1993
A process is claimed for the epoxidation of an olefin involving contacting the olefin with hydrogen peroxide in the presence of a catalytically effective amount of a crystalline titanium-
Zeolites
17:314-319,
1996
315
Manufacture
of zeolite
4A from
R.A. Puerto; J.F. Benito Foret S.A. U.S. 5,401,487, Mar. 28, 1995;
Appl.
bauxite
Dec.
Crystalline zirconium rous structures
3, 1991
The process includes digesting bauxite at atmospheric pressure and 90-100°C using a 211% NaOH solution; filtering the product obtained; passing the filtrate through a bed of hydrophobic resin to remove organic material; reacting the treated filtrate at 60-70°C with an alkaline solution of silica with a SiOdNa,O molar ratio of 2.0-2.5 to obtain a sodium aluminosilicate gel; crystallizing the gel to produce the desired zeolite; treating the residue from the filtration step with H,SO, to recover metals in the form of an aqueous metal sulfate and recycling the silica residue for preparation of the alkaline solution of the silica used in the reaction step; and recycling the mother liquor remaining after crystallization of the gel to the digestion step.
Manufacture
of zeolite
crystal
Appl.
Oct.
12,
A process for the manufacture of zeolite crystal membranes comprises impregnating AI,O, substrates with slurries containing zeolite crystals in binder solutions; optionally washing and drying the substrates; and hydrothermally reacting the substrates containing adhered zeolite crystals by immersion in a solution containing zeolite precursor raw materials. The binders may be water glass or SiO, sol.
of A-type
K. Inoe; S. Tsunematsu; Kogyo Gijutsuin Jpn. Kokai Tokkyo Koho 1993
zeolites H. Yamada Apr.
of alkali
R.B. Edwards; Crosfield Ltd. PCT Int. Appl.
metal
25, 1995;
aluminosilicates
Appl.
Oct.
4,
of zeolite
P. Graham 95,12,546,
May
11, 1995;
U.K.
Appl.
Nov.
2, 1993
A process for the manufacture of alkali metal aluminosilicates of zeolite P-type comprises mixing and reacting a sodium silicate solution in a first reaction zone with a sodium aluminate solution and NaOH to form an amorphous aluminosilicate having the general formula (2.5-7.5) Na,O: (2.0-3.0) SiO,: AI,O,: (80250) H,O and a supersaturated mother liquor; transferring the mixture, having degree of crystallinity ~30, preferably 20%, from the first reaction zone to a second reaction zone and allowing the material to convert fully into P-type zeolite; filtering; washing; and drying the resulting product having the general formula M,,, 0: AI,O,: (2.0-2.66) SiO,: y H,O.
Synthetic
ZSM-5
Y. Suzuki; Nok Corp. Jpn. Kokai 1993
T. Nanba Tokkyo
zeolite
Koho
crystals
95,118,010,
and their
May
9, 1995;
Apr.
zeolite-like
18, 1995;
Appl.
po-
July
22,
Crystalline zirconium phosphates with zeolite-like porous structures have formulas: NH,Zr,(PO,),: mH,O (0 s m 5 2), HZr,(PO,), and HZr,(PO,),: mH,O (0 < m 5 2), specified X-ray diffraction patterns, and oxide mol ratios 4Zr0,:3P,O,. The phosphates can be used for ion exchangers (cation exchangers), adsorbents, catalysts, and porous ceramic materials.
CATALYSIS
F.C. Wilhelm; T.R. Gaffney; G.E. Parris et al. Air Products and Chemicals, Inc. Can. Pat. Appl. 2,126,834, Jan. 2, 1995; U.S. Appl.
manufacture
Appl.
Oct.
15,
Square pillar-like ZSM-5 zeolite crystals are manufactured from aqueous reaction mixtures containing lower alkoxysilanes as silica sources, alumina sources, alkali metal sources, and tetrapropylammonium salts as crystallization agents by hydrothermal reaction in an autoclave at 160-200°C. The crystals have large apparent surface area.
July
1, 1993
A nonequilibrium distribution of methylamines is prepared by the catalyzed reaction of methanol and/or dimethyl ether with ammonia followed by the catalytic reforming of the methylamine-containing feedstock produced. The process selectively affords a reaction product enriched in monoand dimethylamines and low in trimethylamine, at high conversion of methanol or dimethyl ether. The low trimethylamine selectivity at high conversion is achieved by the use of a microporous zeolite, preferably chabazite, catalyst having a geometric selectivity index ~3 and a shape selectivity index >5.
Integrated
95,109,117,
A process for the manufacture of A-type zeolites comprises heating mixtures containing fly ash and solid NaOH at 90-180°C for 260 min, preferably at IOO-150°C for 5-20 h. to obtain a slurry; mixing with more NaOH and water; and hydrothermally reacting the slurry. The mixtures may contain 5fl-I:2 (weight ratio) of fly ash and solid NaOH. The fly ash may contain 215% AI,O, and 250% SiO,.
Manufacture P-type
K. Ito; Y. Takada; K. Kunibe Daiichi Kigenso Kagaku Kogyo Jpn. Kokai Tokkyo Koho 95,101,711, 1993
with
Chabazite catalysts for the preparation of methylamines from ammonia and methanol or dimethyl ether
membranes
A. Saji; H. Noda; K. Hashimoto et al. Chubu Electric Power; Ngk Insulators Ltd. Jpn. Kokai Tokkyo Koho ~5,109,116, Apr. 25, 1995; 1993
Manufacture
phosphates
report
catalytic
cracking
and olefin
cess M.C. Kerbv: R. Bearden. Jr.: S.M. Davis Exxon Res’earch and Engineering Co. Eur. Pat. Appl. 654,519; 654,520; 654,521; U.S. Appls. Nov. 19, 1993
producing
654,523,
May
pro-
24, 1995;
A combined catalytic cracking and olefin production process uses a coked catalytic cracking catalyst as a dehydrogenation catalyst to dehydrogenate an alkane feed and form an olefin-rich product. Preferably the coked catalytic cracking catalyst has a carbon content of -0.2-10%. The method uses a staged back mixed regeneration system to form the dehydrogenation catalyst and to reactivate fully the deactivated cracking catalyst for reuse in the cracking reaction. The catalyst preferably comprises a crystalline tetrahedral framework oxide component, particularly zeolite 0.
Gasoline cracking
upgrading
process
D.L. Fletcher; T.L. Hilbert; Mobil Oil Corp. U.S. 5,413,696; 5,413,698,
by hydrodesulfurization
S.J.
McGovern
May
9, 1995;
and
et al. Appls.
Aug.
15, 1991
Low sulfur gasoline of relatively high octane number is produced from a catalytically cracked, sulfur-containing naphtha by hydrodesulfurization followed by treatment over an acidic catalyst comprising zeolite p. The treatment over the acidic catalyst in the second step restores the octane loss that takes place as a result of the hydrogenative treatment and results in a low sulfur gasoline product with an octane number comparable to that of the feed naphtha.
Epoxidation of olefins zeolite p catalyst
with
hydrogen
R.J. Saxton; J.G. Zajacek; G.L. Crocco Arco Chemical Technology L.P. U.S. 5,412,122, May 2, 1995; Appl. Dec.
peroxide
using
a
23, 1993
A process is claimed for the epoxidation of an olefin involving contacting the olefin with hydrogen peroxide in the presence of a catalytically effective amount of a crystalline titanium-
Zeolites
17:314-319,
1996
315