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Upgrading light paraffins
Patent
Repoti
Preferably, a V getter additive is present as separate particles to act as a V sink. The catalyst and process may be used in fluidized-bed catalytic crgcking.or in moving-bed catalytic cracking units.
Oxidation D.R.C
Exxon PCT
Integrated process N.Y.
Mobil U.S.
catalytic
Chen;
A.B.
dewaxing
Ketkar;
R.D.
Partridge
1990;
Appl.
and
catalytic
cracking
July
31,
Chemical Int. Appl.
26,
Patents
1988
M. Hesse;
BASF
W.
Preparation
Amoco U.S.
light
paraffins
M.
4,950,828,
Aug
21,
1990;
Appl.
June
30,
gas treatment
90.144.153,
June
1,199O;
Appl.
Nov.
22,
The title catalyst comprises a crystalline aluminosilicate containing Cu formed over the surface of micropores of activated A1203. The catalyst provides a high diffusivity of gases to the active catalyst sites, and shows good performance at high power and lean gas operation of automobile engines.
for boiler
M. Yoshimoto;
T. Nakatsuji;
Industry
Chemical
Jpn Kokai 1988
Tokkyo
Koho
NO, is removed from presence of a catalyst CeOz. LazOz, TazOs. type zeolite support which zfx is s 0.3:1,
Catalysts
90,95,444,
M. Yoshimoto;
T. Nakatsuji;
Industrial
Tokkyo
Appl.
Oct.
Koho
K. Nagano
Co.
Ltd.
90,99,143,
Apr.
11,
1900;
Appl.
Oct.
N.Y.
Mobil U.S.
Chen;
cellulosic L.R.
materials
to hydrocarbon
6, the the the y/x
products
June
12,
1990;
Appl.
Sept.
30,
1982
Cellulosic materials are converted to hydrocarbons by hydrolysis, fermentation of the hydrolysate, and conversion of the fermentation product to hydrocarbons using highly siliceous crystalline zeolite catalyst. The cellulosic material first is hydrolyzed to a mixture of fermentable sugar and furfural or its derivatives. The hydrolysate is incubated with a microorganism. The fermentation product and the furfural is then mixed with MeOH and reacted in the presence of a zeolite catalyst for conversion to hydrocarbon.
752
ZEOLITES,
of ascorbic
1991, Vol 11, September/October
Appl.
Feb.
8, 1989
acid
W.
3,843,389,
et a/.
Steck
June
of benzene
Arganbright; 4,950,834,
28,
1990;
to make
D. Hearn Aug. 21, 1990;
cracking
Angevine;
Appl.
Dec.
23,
1988
of 2-keto-L-gulonates
over
cumene
Appl.
July
26,
1989
catalyst
R.G.
Bundens;
J.A.
Herbst
et al.
Oil Corp. 4,956,075,
Sept.
11,
1990;
Appl.
Dec.
22,
1988
The use of a catalyst containing Mn, a large-pore crystalline zeolite, and, optionally, rare earth metals in catalytic cracking is described. This catalyst gives high gasoline selectivity with low coke yields and is suitable for gas oil or resid cracking applications.
Catalsyts
for nitrogen
S. Kasahara;
Tosoh
oxide
K. Kamiyama;
removal
from
exhaust
gases
K. lgawa
Corp. 90,164,451;
90,164,453,
June
25, 1990;
The title catalysts are zeolites containing univalent or divalent Cu and NH3 in NH&u 5 0.2 atomic ratio, and their preparation involves Cu ion-exchange treatment using an aqueous Cu salt- and NHIcontaining solution. NO, removal from exhaust gas is carried out by bringing the gas into contact with the catalysts. The catalysts are also applicable for combustion gases and flue gases and have high NO, decomposition activity owing to the Cu ion, which works as an active center for contact decomposition of NO,.
Preparation of amines amines to olefins V. Taglieber;
Koenig
Oil Corp. 4,933,283,
9, 1990;
prepared by reaction of HzNCHzCHzNHz and over a Al-, 8-, Ga-, or Fe-silicate zeolite.
Jpn Kokai Tokkyo Koho Appls. Dec. 16, 1988
NO. is removed from boiler flue gases by reduction with NH3 in presence of a metal-exchanged modernite-type zeolite having composition M~H~,,b~Na~X~~((AIOz)X(SiOz~y).mHzO, in which valence of metal M is (b+c)/l, but (z-cl/x s 0.35:1; l/x > 0.3:1; 3 5:l.
Converting
3,
flue gas denitration
Sakai
Jpn Kokai 1988
6, 1990;
boiler flue gases by reduction with NH3 in the comprising 2 1 active metal oxides (e.g., or Nbz05) loaded on an acid-type mordeniteof formula H,~,.Na,.((AIOz).(SiOz)~).mHzO, in and y/x is > 5:~.
for boiler
Chemical
Apr.
et a/.
Steck
Aug.
H. Lermer;
Offen.
Catalytic
U.S.
K. Nagano
8, 1988 presence
A.-G.
Mobil
Co. Ltd.
Nov. in the
Cumene is produced in a catalytic distillation column reactor having an upper bed of omega-type zeolite cat’alyst and a lower bed of Y-type zeolite catalyst. CsHs and propylene are reacted in the upper bed where the omega-type zeolite is more selective to cumene than the Y-type catalyst. Part of the reaction mixture flows down the column to the Y zeolite catalyst bed where CsHs reacts with any unreacted propylene to produce cumene. Additionally, CsHs reacts with dipropylbenzene in the Y zeolite catalyst bed to produce more cumene.
P.J.
flue gas denitration
Sakai
3,903,622,
Alkylation R.P. U.S.
Appl.
by HzOz
Ascorbic acid is prepared by lactonization borosilicate zeolite catalysts.
containing comprises a catalyst a Pt com-
catalyst
S. Matsumoto Toyota Motor Corp. Jpn Kokai Tokkyo Koho 1988
Catalyst
Hesse;
Ger.
1989
A process for converting a gaseous hydrocarbon feed C3-s paraffinic hydrocarbons to aromatic hydrocarbons contacting the feed under conversion conditions with composition comprising a crystalline borosilicate zeolite, ponent and Ga component.
Exhaust
Offen.
BASF
Corp.
Belg.
oxidized
A.-G.
Upgrading Shum
17, 1990;
were catalyst.
of 1,4-diazabicyclo[2.2.2)octane
The title compound was O-200 mol % piperazine
V.K.
May
H. Lermer;
Dewaxing, preferably catalytic dewaxing over zeolite beta or ZSM-5, improves the crackability of a heavy waxy feed to a catalytic unit. When the catalytic dewaxing occurs, using ZSM-5 dewaxing catalyst, high-octane gasoline is obtained as a byproduct.
Ger.
chains
Inc.
90,05,126,
Preparation Oct.
hydrocarbon
The saturated hydrocarbons of a Ti-containing silicalite
Oil Corp. 4,944,862,
of saturated
Huybrechts
W.
BASF
A.-G.
U.S.
4,929,759,
NH3 or primary of a borosilicate
Selective N. Ito;
Toa
by
Hoelderich; May
addition
R. Kummer
29, 1990;
Appl.
July
of
ammonia
or
et al. 23,
1984
or secondary amines add to olefins in the presence or borogermanate pentasil-type zeolite catalyst.
preparation
of p-dichlorobenzene
T. Hattori
Gosei
Jpn Kokai 1988
Chemical Tokkyo
Industry Koho
Co. Ltd.
90,180,843,
July
13, 1990;
Appl.
Dec.
29,
Repoti
Preferably, a V getter additive is present as separate particles to act as a V sink. The catalyst and process may be used in fluidized-bed catalytic crgcking.or in moving-bed catalytic cracking units.
Oxidation D.R.C
Exxon PCT
Integrated process N.Y.
Mobil U.S.
catalytic
Chen;
A.B.
dewaxing
Ketkar;
R.D.
Partridge
1990;
Appl.
and
catalytic
cracking
July
31,
Chemical Int. Appl.
26,
Patents
1988
M. Hesse;
BASF
W.
Preparation
Amoco U.S.
light
paraffins
M.
4,950,828,
Aug
21,
1990;
Appl.
June
30,
gas treatment
90.144.153,
June
1,199O;
Appl.
Nov.
22,
The title catalyst comprises a crystalline aluminosilicate containing Cu formed over the surface of micropores of activated A1203. The catalyst provides a high diffusivity of gases to the active catalyst sites, and shows good performance at high power and lean gas operation of automobile engines.
for boiler
M. Yoshimoto;
T. Nakatsuji;
Industry
Chemical
Jpn Kokai 1988
Tokkyo
Koho
NO, is removed from presence of a catalyst CeOz. LazOz, TazOs. type zeolite support which zfx is s 0.3:1,
Catalysts
90,95,444,
M. Yoshimoto;
T. Nakatsuji;
Industrial
Tokkyo
Appl.
Oct.
Koho
K. Nagano
Co.
Ltd.
90,99,143,
Apr.
11,
1900;
Appl.
Oct.
N.Y.
Mobil U.S.
Chen;
cellulosic L.R.
materials
to hydrocarbon
6, the the the y/x
products
June
12,
1990;
Appl.
Sept.
30,
1982
Cellulosic materials are converted to hydrocarbons by hydrolysis, fermentation of the hydrolysate, and conversion of the fermentation product to hydrocarbons using highly siliceous crystalline zeolite catalyst. The cellulosic material first is hydrolyzed to a mixture of fermentable sugar and furfural or its derivatives. The hydrolysate is incubated with a microorganism. The fermentation product and the furfural is then mixed with MeOH and reacted in the presence of a zeolite catalyst for conversion to hydrocarbon.
752
ZEOLITES,
of ascorbic
1991, Vol 11, September/October
Appl.
Feb.
8, 1989
acid
W.
3,843,389,
et a/.
Steck
June
of benzene
Arganbright; 4,950,834,
28,
1990;
to make
D. Hearn Aug. 21, 1990;
cracking
Angevine;
Appl.
Dec.
23,
1988
of 2-keto-L-gulonates
over
cumene
Appl.
July
26,
1989
catalyst
R.G.
Bundens;
J.A.
Herbst
et al.
Oil Corp. 4,956,075,
Sept.
11,
1990;
Appl.
Dec.
22,
1988
The use of a catalyst containing Mn, a large-pore crystalline zeolite, and, optionally, rare earth metals in catalytic cracking is described. This catalyst gives high gasoline selectivity with low coke yields and is suitable for gas oil or resid cracking applications.
Catalsyts
for nitrogen
S. Kasahara;
Tosoh
oxide
K. Kamiyama;
removal
from
exhaust
gases
K. lgawa
Corp. 90,164,451;
90,164,453,
June
25, 1990;
The title catalysts are zeolites containing univalent or divalent Cu and NH3 in NH&u 5 0.2 atomic ratio, and their preparation involves Cu ion-exchange treatment using an aqueous Cu salt- and NHIcontaining solution. NO, removal from exhaust gas is carried out by bringing the gas into contact with the catalysts. The catalysts are also applicable for combustion gases and flue gases and have high NO, decomposition activity owing to the Cu ion, which works as an active center for contact decomposition of NO,.
Preparation of amines amines to olefins V. Taglieber;
Koenig
Oil Corp. 4,933,283,
9, 1990;
prepared by reaction of HzNCHzCHzNHz and over a Al-, 8-, Ga-, or Fe-silicate zeolite.
Jpn Kokai Tokkyo Koho Appls. Dec. 16, 1988
NO. is removed from boiler flue gases by reduction with NH3 in presence of a metal-exchanged modernite-type zeolite having composition M~H~,,b~Na~X~~((AIOz)X(SiOz~y).mHzO, in which valence of metal M is (b+c)/l, but (z-cl/x s 0.35:1; l/x > 0.3:1; 3 5:l.
Converting
3,
flue gas denitration
Sakai
Jpn Kokai 1988
6, 1990;
boiler flue gases by reduction with NH3 in the comprising 2 1 active metal oxides (e.g., or Nbz05) loaded on an acid-type mordeniteof formula H,~,.Na,.((AIOz).(SiOz)~).mHzO, in and y/x is > 5:~.
for boiler
Chemical
Apr.
et a/.
Steck
Aug.
H. Lermer;
Offen.
Catalytic
U.S.
K. Nagano
8, 1988 presence
A.-G.
Mobil
Co. Ltd.
Nov. in the
Cumene is produced in a catalytic distillation column reactor having an upper bed of omega-type zeolite cat’alyst and a lower bed of Y-type zeolite catalyst. CsHs and propylene are reacted in the upper bed where the omega-type zeolite is more selective to cumene than the Y-type catalyst. Part of the reaction mixture flows down the column to the Y zeolite catalyst bed where CsHs reacts with any unreacted propylene to produce cumene. Additionally, CsHs reacts with dipropylbenzene in the Y zeolite catalyst bed to produce more cumene.
P.J.
flue gas denitration
Sakai
3,903,622,
Alkylation R.P. U.S.
Appl.
by HzOz
Ascorbic acid is prepared by lactonization borosilicate zeolite catalysts.
containing comprises a catalyst a Pt com-
catalyst
S. Matsumoto Toyota Motor Corp. Jpn Kokai Tokkyo Koho 1988
Catalyst
Hesse;
Ger.
1989
A process for converting a gaseous hydrocarbon feed C3-s paraffinic hydrocarbons to aromatic hydrocarbons contacting the feed under conversion conditions with composition comprising a crystalline borosilicate zeolite, ponent and Ga component.
Exhaust
Offen.
BASF
Corp.
Belg.
oxidized
A.-G.
Upgrading Shum
17, 1990;
were catalyst.
of 1,4-diazabicyclo[2.2.2)octane
The title compound was O-200 mol % piperazine
V.K.
May
H. Lermer;
Dewaxing, preferably catalytic dewaxing over zeolite beta or ZSM-5, improves the crackability of a heavy waxy feed to a catalytic unit. When the catalytic dewaxing occurs, using ZSM-5 dewaxing catalyst, high-octane gasoline is obtained as a byproduct.
Ger.
chains
Inc.
90,05,126,
Preparation Oct.
hydrocarbon
The saturated hydrocarbons of a Ti-containing silicalite
Oil Corp. 4,944,862,
of saturated
Huybrechts
W.
BASF
A.-G.
U.S.
4,929,759,
NH3 or primary of a borosilicate
Selective N. Ito;
Toa
by
Hoelderich; May
addition
R. Kummer
29, 1990;
Appl.
July
of
ammonia
or
et al. 23,
1984
or secondary amines add to olefins in the presence or borogermanate pentasil-type zeolite catalyst.
preparation
of p-dichlorobenzene
T. Hattori
Gosei
Jpn Kokai 1988
Chemical Tokkyo
Industry Koho
Co. Ltd.
90,180,843,
July
13, 1990;
Appl.
Dec.
29,