Roy Earl Pratt, Age 851733 Green Oaks Dr, Port Neches, TX 77651

5043056, Aug 27, 1991

Feb 24, 1989

7/314867

Roy E. Pratt - Port Neches TX
Jitendra A. Patel - Wappingers Falls NY

Texaco, Inc. - White Plains NY

C10G 4700
C10G 4706
C10G 4726

208108

In an ebullated bed process, a residual hydrocarbon oil and a hydrogen containing gas is passed upwardly through an ebullated bed of catalyst in a hydrocracking zone at a temperature in the range of 650. degree. F. to 950. degree. F. and pressure of 1000 psia to 5000 psia. The hydrogen containing gas comprises hydrogen sulfide in an amount to maintain the sulfur content of the oil in the hydrocracking zone at 2 wt % to 10 wt %. A hydrocracked oil is recovered characterized by having a reduced sediment content.

4243630, Jan 6, 1981

Mar 19, 1979

6/021651

Howard C. Kliesch - Thousand Oaks CA
Daniel N. McWilliams - Baton Rouge LA
Roy E. Pratt - Groves TX
Donald H. Schmude - Trumbull CT

Texaco Inc. - White Plains NY

C10G 2100
G06G 758

422 62

A monitor determines the yields of constituents of a product provided by a fluid catalytic cracking unit (FCCU) receiving fresh feed and recycle feed. The monitor includes sensors providing signals corresponding to sensed operating parameters of the FCCU. Analyzers analyze the fresh feed and the recycle feed and provide signals corresponding to the API gravities of the fresh and recycle feeds and to the viscosities of the fresh and recycle feeds. A circuit provides signals corresponding to the Watson K factors associated with the fresh and recycle feeds and the catalyst in accordance with the signals from the analyzers and sensors. A network provides signals representative of the yields of the constituents of the product from FCCU. Display apparatus provides a visual display of the yields.

4388176, Jun 14, 1983

Nov 19, 1981

6/323097

Roy E. Pratt - Port Neches TX
Scott M. Sayles - Nederland TX
Kerry W. Bowers - Birmingham AL
Richard P. Scott - late of Groves TX

Texaco Inc. - White Plains NY

C10G 1105
C10G 2503
C10G 5106
C10G 5508

208 80

A process for conversion of paraffinic base petroleum cracking stocks to high octane motor fuels and petrochemical feedstocks in which paraffinic components are separated from the cracking stock to yield a deparaffined fraction which is hydrotreated and catalytically cracked and a paraffin fraction which is separately catalytically cracked whereby improved yields of normally gaseous olefins and normally liquid products including high octane motor fuel components are obtained.

5318689, Jun 7, 1994

Nov 16, 1992

7/976771

Hsu-Hui Hsing - Nederland TX
Roy E. Pratt - Port Neches TX

Texaco Inc. - White Plains NY

C10G 6908
C10G 5700
C07C10700

208 70

A straight run naphtha is fractionated to yield on intermediate naphtha and the heaviest 10 vol % as heavy naphtha. The intermediate naphtha is catalytically reformed to yield reformed naphtha having a 90 vol % temperature (T90) of 310. degree. F. (155. degree. C. ). The heavy naphtha is subjected to fluid catalytic cracking (FCC) to yield liquid fuel and lighter, including C. sub. 4 olefins and a cracked naphtha having a research octane number suitable for gasoline blending.

5416054, May 16, 1995

Feb 25, 1993

8/077807

Gerald V. Nelson - Nederland TX
Govanon Nongbri - Port Neches TX
Roy E. Pratt - Port Neches TX
David E. Sherwood - Beaumont TX

Texaco Inc. - White Plains NY

B01J 2719
B01J 27188
B01J 2718

502211

Heavy oils may be hydrotreated in the presence of a porous alumina support bearing metals of Group VIII and VI-B and optionally phosphorus, the catalyst having a Total Surface Area of 165-230 m. sup. 2 /g, a Total Pore Volume of 0. 5-0. 8 cc. g, and a Pore Diameter Distribution whereby less than about 5% the Total Pore Volume is present as primary micropores of diameter less than 80. ANG. , and secondary micropores of diameter of +20. ANG. of a Pore Mode of 100-135. ANG. are present in amount of at least about 65% of the micropore volume having pores with diameter less than 250. ANG. , and 22-29% of the Total Pore Volume is present as macropores of diameter >250. ANG. The process of the instant invention is particularly effective in achieving desired levels of hydrodemetallation, hydrodesulfurization, and hydrocracking of asphaltenes in the fraction of hydrotreated/hydrocracked petroleum resid product having a boiling point greater than 1000. degree. F.

5028310, Jul 2, 1991

Nov 8, 1989

7/433103

Roy E. Pratt - Port Neches TX
David E. Self - Port Neches TX
Joseph C. Demeter - Port Neches TX

Texaco Inc. - White Plains NY

C10G 1118

208121

SO. sub. x in regenerator off gas in a fluid cracking unit is decreased by providing in the regenerator bed, a metal grid bearing a layer of rare earth oxide.

5468371, Nov 21, 1995

Apr 11, 1994

8/226191

Gerald V. Nelson - Nederland TX
Govanon Nongbri - Port Neches TX
Roy E. Pratt - Port Neches TX

Texaco Inc. - White Plains NY

C10G 4504
C10G 4712

208216PP

Heavy hydrocarbons are hydrotreated to increase content of components boiling below 1000. degree. F. by contact with Group VIII non-noble metal oxide and Group VIB metal oxide on alumina having a Total Surface Area of 175-220 m. sup. 2 /g, a Total Pore Volume (TPV) of 0. 6-0. 8, and a Pore Diameter Distribution whereby. ltoreq. 33% of the TPV is present as primary micropores of diameter. ltoreq. 100. ANG. , at least about 41% of TPV is present as secondary micropores of diameter of about 100. ANG. -200. ANG. , and about 16%-26% of the TPV is present as mesopores of diameter. gtoreq. 200. ANG. Phosphorus containing compounds are avoided during catalyst preparation.

4304659, Dec 8, 1981

Mar 5, 1980

6/127792

Roy E. Pratt - Port Neches TX
William R. Menzies - Austin TX
Leonce F. Castagnos - Nederland TX

Texaco, Inc. - White Plains NY

C10G 1118

208164

An improved method for controlling the fluidized dense catalyst phase temperature in the regeneration zone of a fluid catalytic cracking unit. In this method, the level of the fluidized catalyst bed above the riser discharge in the reaction vessel is adjusted in response to a change detected in the temperature of the fluidized dense catalyst phase of the regeneration zone. Adjustment of the catalyst bed level in the reaction zone affects the coke laydown on the catalyst in the reactor and, consequently, the amount of heat liberated in the regeneration zone upon combustion of the coke contained in the partially deactivated catalyst. A reactor bed level is attained where the resulting coke laydown on the catalyst is sufficient to maintain the desired temperature in the fluidized dense catalyst phase. Also, as a part of this improved method, the amount of oxygen-containing regeneration gas supplied to the regeneration zone is adjusted to provide sufficient oxygen to effect substantially complete combustion of the coke to carbon dioxide and to maintain the oxygen content of the flue gas at a desired level within the range of from about 1 to about 10 mol %. Maintaining the oxygen content of the flue gas within this range provides a flue gas having a carbon monoxide content of from 0 to 500 ppm.