Other

Hri, Inc.

Hydrocarbon Research, Inc.

Headwaters Technology Innovation, LLC

Ifp North America, Inc.

Lawrence M Abrams

Steven J Hildebrandt

John E Duddy

Lap-Keung Lee

Hashim Sardar

An expanded bed hydroprocessing system and related method includes at least one expanded bed reactor that employs a solid catalyst to catalyze hydroprocessing reactions involving hydrogen and a high molecular weight hydrocarbon feedstock (e.g., a Fischer-Tropsch wax) that is contaminated with solid particulates. Hydroprocessing the high molecular weight hydrocarbon feedstock in an expanded bed reactor results in formation of a hydroprocessed material from the hydrocarbon feedstock, while eliminating the risk of plugging of the supported catalyst bed by the solid particulates as compared to a reactor including a stationary catalyst bed.

Expanded bed reactor system and method for hydroprocessing wax produced by Fischer-Tropsch reaction and contaminated with solids

A process for catalytic two-stage hydrodesulfurization of metal-containing petroleum residua feedstocks to achieve at least about 75% desulfurization of the liquid product while also providing at least about 40% reduction in catalyst consumption. In the process, used catalyst having a catalyst equilibrium age of 0.3-5.0 bbl oil feed/lb catalyst is withdrawn from the second stage reactor, rejuvenated so as to remove 10-50 wt. % of the contaminant metals and at least 80 wt. % of carbon deposited on the catalyst, and then cascaded forward and added to the first stage reactor. Sufficient fresh make-up catalyst is added to the second stage reactor to replace the used catalyst withdrawn there, and only sufficient fresh catalyst is added to the first stage reactor to replace any catalyst transfer losses. Used catalyst having a catalyst equilibrium age of 0.6 to 10.0 bbl. oil per lb. catalyst is withdrawn from the first stage reactor for discard.

Catalytic multi-stage hydrodesulfurization of metals-containing

A process and apparatus for rejuvenating particulate used catalysts in a single rejuvenation vessel and providing a rejuvenated catalyst material having properties that result in activity substantially equal to new catalyst. The pressurizable vertically-oriented vessel has inlet and outlet openings for the catalyst and washing liquids, and is arranged to facilitate successive solvent liquid washing, water washings, and acid treatment steps for the used particulate catalyst provided in a bed in the vessel conical-shaped lower portion which contains catalyst rotary stirring means. After rejuvenation of the used catalyst, it is withdrawn from the vessel conical-shaped lower portion downwardly through a central withdrawal conduit and control valve for further processing. The water-soluble solvent and acid treatment liquids can be usually recovered by distillation for reuse in the catalyst rejuvenation process. The solvent-washed and acid-treated catalyst is separately heated and oxidized to remove carbon deposits and provide a completely rejuvenated catalyst material.

Catalyst rejuvenation process

Hydrocarbon feedstocks containing tetra-hydro-dicyclo-penta-diene (THDCPD) dissolved in a suitable solvent is substantially totally reformed and hydroconverted in a non-catalytic reactor having length/internal diameter ratio between 10/1 and 30/1 at critical controlled reaction conditions, including molar ratio of hydrogen-to-THDCPD of 5.0:1-12.0:1, reaction temperature of 1100.degree.-1350.degree. F., reactor pressure of 550-650 psig, and feedstream reactor residence time of 10-50 seconds so as to yield primarily benzene product together with minor aromatic materials. Suitable solvent materials can be an aromatic solvent, a non-aromatic solvent containing naphthenic and paraffinic compounds, or a combination of each. When the solvent is predominantly an alkyl aromatics mixture, these components are hydrodealkylated while the THDCPD material undergoes simultaneous reformation in the reactor. Heavy mono-aromatic materials contained in the reactor effluent may be recycled back to the reactor to ultimately yield additional benzene, with minimal aromatics loss. Heavy fractions of biphenyl and alkyl-biphenyls may also be recycled to the reactor to minimize formation of new biphenyl molecules.

Thermal reforming of naphthenic and hydrodealkylation of aromatic

A flush device comprising an inlet and an outlet chamber separated by a wall also includes two apertures in the wall. One of the apertures has a small diameter, the other having a large diameter. A serpentine-shaped capillary tube is formed along the wall surface in the inlet chamber and coaxial with the axis of the larger diameter aperture. The exit end of the tube is connected to the smaller diameter aperture for providing a controlled fluid path from the inlet to the outlet chamber. A plunger is positioned coaxially with the axis of the larger diameter aperture and is biased to normally close the larger diameter aperture. The plunger also is operative to open the larger diameter aperture for forming a large diameter path for fluids for a flush operation.

Flush device

A flow sensing apparatus has an obstruction extending across the tube to form two openings. The obstruction is at an angle to the tube axis and includes a portion with reduced dimension. Pressure sensors are located on opposite sides of the obstruction.

Fluid flow monitoring device

Patient pressure monitoring systems require constant monitoring and adjustment by patient care specialists because of erroneous indications of changes in blood pressure readings which occur is such systems. The changes are due to errors produced by the sensing system caused by patient movement with respect to the pressure sensor. Such erroneous changes are eliminated by the addition of a second fluid path which is maintained at atmospheric pressure and controllably is connected to the prime fluid path to normalize any change in pressure in the prime path due to changes in relative positions of the sensor and the patient.

Pressure-compensated fluid administering apparatus

A flow rate sensing device, particularly for use in regulating the rate of flow in a system for parenteral administration of liquids to patients. The liquid emerges from a storage reservoir and is fed into a housing through an upstream flow passage portion and then is made to pass through a narrow throat passage wherein the velocity of the liquid increases while its pressure decreases. The liquid then emerges into a downstream flow through passage and flows through an outlet from the housing. In an intravenous fluid administration system, the housing outlet is connected to a terminal tubing section and an intravenous needle. A pressure transducer, consisting of two chambers separated by a resilient deformable diaphragm, has its upstream chamber in fluid and pressure communication with the upstream flow path portion and its downstream chamber in fluid and pressure communication with the flow emerging from the throat passage. Variations in the flow rate through the throat passage effect changes in the pressure differential between the transducer chambers and thus cause variable degrees of displacement of the transducer diaphragm. The mechanical signals created by the movement of the diaphragm can be transduced to an arrangement for controlling the rate of fluid flow through the system. Alternatively, the mechanical signal created by the diaphragm can be transduced to flow rate monitoring or flow rate coordinating systems.

Flow rate sensing device

A process for high hydroconversion of petroleum residua containing at least about 25 V % material boiling above 1000.degree. F. to produce lower boiling hydrocarbon liquid products and avoid undesirable precipitation of asphaltene compounds. In the process, the feedstock is at least about 50 percent catalytically hydroconverted to material boiling below 975.degree. F. and containing a mixture of gas and liquid fractions, after which the gas fraction is removed and the resulting liquid fractions is pressure-reduced and quenched to a temperature below about 775.degree. F. To avoid precipitation of asphaltene compounds which causes operational difficulties in the downstream equipment, the quench liquid used should have an API gravity not more than about 22.degree. API higher than the API gravity of the first pressure-reduced liquid fraction. The resulting liquid fraction is distilled to produce hydrocarbon liquid products, and a residual bottoms fraction is usually recycled to the catalytic reaction step to obtain increased percent conversion to lower boiling liquid products.

Quenching hydrocarbon effluent from catalytic reactor to avoid

A method for controlling the temperature and composition of a vapor feedstream into a second reactor connected in series flow arrangement with a first reactor. The effluent stream from the first reactor containing vapor and liquid fractions is first cooled against a vapor stream and then further cooled against a suitable external fluid, then is phase separated to provide vapor and liquid fractions. The separated vapor fraction is reheated against the first reactor effluent stream and passed at an intermediate temperature into the second reactor. The first reactor is preferably an ebullated bed type catalytic reactor and the second reactor is preferably a fixed bed type catalytic reactor which is operated at an inlet temperature 20.degree.-200.degree. F. lower than the first reactor effluent stream temperature. If desired, the effluent stream from the first reactor can be initially phase separated into vapor and liquid factions, and the vapor fraction only passed to the first heat exchange step for cooling to a first lower temperature.

Growing community of inventors

Cherry Hill, NJ, United States of America

Lawrence M Abrams