Robert K Irvine Deceased4930 N Highland Ave, Kansas City, MO 64118

2002004, Apr 18, 2002

Aug 22, 2001

09/934759

Robert Irvine - Overland Park KS, US

B01D024/00
B01D029/62

210/661000, 210/660000, 210/263000

A continuous adsorption facility is used to purify a liquid stream that contains impurities. A solid adsorbent is used having a special affinity for the impurities over the desired components in the liquid feed. An adsorber is constructed, employing gravity for the transfer of adsorbent between stages with a series of stages each having fluidized beds with limited bed expansion characteristics where the solid adsorbent countercurrent-contacts the upwardly flowing fresh feed introduced at the base. The adsorbent is regenerated with return of most of the desired components from the porous solids becoming part of the adsorber-treated product. Impurities are further removed during regeneration and disposed of separately. Using a novel regeneration arrangement, the reactivating gas may be reduced to below 4% of prior requirements. Capital investment and operating costs economically afford ultra-low sulfur clean gasoline meeting standards imposed by auto manufacturers worldwide.

2002015, Oct 24, 2002

Jan 25, 2002

10/057180

Robert Irvine - Overland Park KS, US

B01D011/00
C02F001/42
C02F001/44

210/634000, 210/639000, 210/670000, 210/676000, 210/677000, 210/774000

A continuous adsorption facility is used to purify a liquid stream that contains impurities. A solid adsorbent is used having a special affinity for the impurities over the desired components in the liquid feed. An adsorber is constructed, employing gravity for the transfer of adsorbent between stages with a series of stages each having fluidized beds with limited bed expansion characteristics where the solid adsorbent countercurrent- contacts the upwardly flowing fresh feed introduced at the base. The adsorbent is regenerated with return of most of the desired components from the porous solids becoming part of the adsorber-treated product. Impurities are further removed during regeneration and disposed of separately. Using a novel regeneration arrangement, the reactivating gas may be reduced to below 5% of prior requirements. Capital investment and operating costs economically afford ultra-low sulfur clean gasoline meeting standards imposed by auto manufacturers worldwide.

5730860, Mar 24, 1998

Aug 14, 1995

8/514948

Robert L. Irvine - Overland Park KS

The Pritchard Corporation - Overland Park KS

C10G 100

208213

An apparatus and method for treating a liquid hydrocarbon stream useful as a precursor for transportation fuel and which contains an unacceptably high level of heteroatom compounds is provided for the removal of a significant portion of the heteroatom compounds from the hydrocarbon stream. The method and apparatus employ an adsorbent which is brought into countercurrent contact with a hydrocarbon stream in an adsorption zone to form a product hydrocarbon stream and a spent adsorbent stream. The adsorbent is recirculated to a desorption zone and is thereafter brought into cross-current contact with a reactivating medium, such as hydrocarbon gas, at elevated temperatures to form a reactivated adsorbent stream and a hydrogen/heteroatom stream. The regenerated adsorbent is recirculated back to the adsorption zone to form the adsorbent stream.

5268515, Dec 7, 1993

Mar 1, 1993

8/024525

Robert L. Irvine - Overland Park KS

The Pritchard Corporation - Overland Park KS

C07C 2904
C07C 4100

568895

Propene is reacted with water in a multi-stage, fluidized bed catalytic reactor to produce an oxygenate motor fuel additive containing a major proportion of isopropanol, a minor proportion of diisopropyl ether, and some water. The molar ratio of water to propene introduced into each catalytic stage of the multi-stage reactor is maintained within a range of from about 2:1 to about 6:1. The temperature of the reactants in each of the catalytic stages is maintained within a range of from about 250. degree. F. to about 320. degree. F. and the pressure at a level of from about 1200 psia to about 3600 psia. The temperature in each catalytic stage increases from the initial catalytic stage to the final catalytic stage with the temperature increase being limited to a value within a range of from about 8. degree. F. to about 1. degree. F. The pressure of the final stage of the catalytic section is controlled so that the reaction product containing the organic constituents including oxygenates provides a concentrated, less dense liquid stream which may be easily separated from the aqueous liquid phase in the final stage.

5191129, Mar 2, 1993

May 1, 1992

7/877642

Robert L. Irvine - Overland Park KS

The Pritchard Corporation - Overland Park KS

C07C 2904
C07C 4100

568895

Propene is reacted with water in a multi-stage, fluidized bed catalytic reactor to produce an oxygenate motor fuel additive containing a major proportion of isopropanol (IPA), some diisopropyl ether (IPE) and some water. The molar ratio of water to propene introduced into each catalytic stage of the multi-stage reactor is maintained within a range of from about 2:1 to about 6:1. The temperature of the reactants in each of the catalytic stages is maintained within a range of from about 250. degree. F. to about 300. degree. F. and the pressure at a level of from about 1200 psia to about 3000 psia. The temperature in each catalytic stage increases from the initial catalytic stage to the final catalytic stage with the temperature increase being limited to a value within a range of from about 8. degree. F. to about 2. degree. F. The pressure of the final stage of the catalytic section is controlled so that the reaction product containing the organic constituents including oxygenates provides a concentrated, less dense liquid stream which may be easily separated from the aqueous liquid phase in the final stage.