Phillips Petroleum Company

William S Stewart

Gary L Funk

Dexter E Smith

John E Blaesi

Guy S Pennington, Jr

John D Hottovy

Warren H Huang

James W Hobbs

George P McAllister

Adam Loren Freund

Russel A Buss

Virgil R Spurgeon

The present disclosure provides a weed trimmer apparatus including: a belt having: a power clip first portion, a belt power source, a plurality of second power transmission wires extending through the belt and electrically connecting the belt power source to the power clip first portion, a belt clip; a trimmer including: a trimmer base having: a motor, a trimmer power source receiver, a shaft, a debris shield, a trimmer head secured below the debris shield, a plurality of cutting swaths, a first handle portion extending orthogonally from the shaft, a second handle extending from the first handle and configured to axially rotate around the first handle; and a power source configured to secure to either the first power source receiver or the trimmer, wherein the power source, when secured to the trimmer power source receiver, is configured to provide electrical output to the motor of the trimmer.

Weed trimmer apparatus and system

Smartphone chest holster

Desktop accessory

Combined barrier free tub and shower

In an absorption process in which an absorption medium is utilized to absorb H.sub.2 S from a feed gas containing H.sub.2 S, the flow rate of the lean absorption medium is manipulated so as to maintain the actual H.sub.2 S concentration in the product gas stream from the absorption process substantially equal to a desired value for the H.sub.2 S concentration. However, if the H.sub.2 S concentration in the rich absorption medium stream exceeds a high limit, the control of the lean absorption medium flow rate so as to maintain a desired H.sub.2 S concentration in the product gas stream is overridden until such time as the H.sub.2 S concentration in the rich absorption medium stream is below the high limit.

Control of a H.sub.2 S absorber

For parallel heat exchangers, one using a more preferred heat exchange medium as a heat exchange source and another using a less preferred heat exchange medium, maximum use of the more preferred heat exchange medium is used prior to use of the less preferred heat exchange medium in achieving a desired total heat exchange through the parallel heat exchange system. In employing such a heat exchange system in a cracking process it is combined with individual control of flows of feed fluid and diluent fluid to a plurality of individual cracking tubes in a cracking furnace to maintain a desired mass flow of feed fluid and ratio of mass diluent fluid to steam fluid to each such cracking tube.

Cracking furnace control

Catalytic crackins process control

A delayed coker control system wherein the hydrocarbon feed flows to the coker furnace is automatically limited to the lowest of the maximum allowable flows to avoid furnace zone flooding, an air-limited furnace and overfilling of the coke drum in the cycle time. Flows among the separate furance zones are adjusted to balance heat loads on each stream and to redistribute excess flow to non-flooding zones.

Method and device for controlling a delayed coker system

A feedforward control system for a multiple-effect evaporator is provided wherein control is based on maintaining desired values for inferential variables of concentration and boiling point rise for a solution of a solid inorganic substance.

Automatic control of a multiple-effect evaporator

Process control for parallel heat exchangers

An integrated control system for a vinyl acetate process. A desired production rate of vinyl acetate is achieved by maintaining a desired reactor temperature. At the same time, the concentration of oxygen in the vinyl acetate reactor and condenser are maximized and the reactor pressure is maximized, all in a safe manner, so as to increase the selectivity of the process to the production of vinyl acetate. Also, the overall process is controlled so as to improve the efficiency of energy and materials usage.

Control of a vinyl acetate process

Control of an isomerization process is based on a known relationship between the octane number and temperature of a reaction at equilibrium; and a predetermined relationship between octane number and temperature of the reaction product of a reactor using a specific catalyst. In use, measurements of actual octane number and temperature are compared with the octane number and temperature of a reaction at equilibrium to determine if the reaction is at equilibrium. If the reaction is not at equilibrium, a control signal is developed to restore equilibrium. Thus control of an isomerization process is accomplished so as to substantially maximize the efficiency of the isomerization process both from a production standpoint and from an energy usage standpoint by maintaining the isomerization reaction at desired equilibrium conditions. Also, for a dual reactor system, the differential temperature between the two reactors is manipulated so as to maintain more favorable isomerization conditions in the tail reactor. Energy efficiency is improved by substantially minimizing the amount of heating fluid utilized to preheat the feed to the isomerization process.

Control of an isomerization process

In an aromatic extraction process, the flow rate of aromatics to the extraction column is utilized to control the downstream stripping column so as to maintain a desired purity of the aromatic extract stream withdrawn from the stripping column. Also, the flow rate of solvent to the extraction column is manipulated so as to maintain a desired aromatic concentration in the raffinate stream withdrawn from the extraction column. This control, together with other interactive control functions, results in a control of the aromatic extraction process which substantially maximizes the profitability of the extraction process.

Control of an aromatic extraction

A reforming furnace having a radiant section containing cracking tubes, a convection section and a stack is controlled so as to maintain a desired synthesis gas temperature unless such maintenance would result in the violation of a process constraint. The desired excess oxygen concentration in the combustion gases withdrawn from the radiant section is also maintained while maintaining the desired synthesis gas temperature. As for the convection section, the temperature of a fluid stream passing through the convection section is maintained while still maintaining a desired excess oxygen concentration in the stack gas.

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Bartlesville, OK, United States of America

William S Stewart