6186 results about "Reaction zone" patented technology

A process for the selective production of ethylene by vapor phase reaction of acetic acid over a hydrogenating catalyst composition to form ethylene in a single reaction zone is disclosed and claimed. In an embodiment of this invention reaction of acetic acid and hydrogen over either a copper supported on iron oxide, copper-aluminum catalyst, cobalt supported on H-ZSM-5, ruthenium-cobalt supported on silica or cobalt supported on carbon selectively produces ethylene in a vapor phase at a temperature in the range of about 250° C. to 350° C.

A method for forming a single-phase multi-element film on a substrate in a reaction zone by PEALD repeating a single deposition cycle. The single deposition cycle includes: adsorbing a precursor on the substrate in the absence of reactant and plasma; decomposing the precursor adsorbed on the substrate by an inert gas plasma; and reacting the decomposed precursor with a reactant gas plasma in the presence of the inert gas plasma. The multi-element film contains silicon and at least two non-metal elements constituting a matrix of the film, the precursor contains silicon and optionally at least one non-metal element to be incorporated in the matrix, and the reactant gas contains at least one non-metal element to be incorporated in the matrix.

The present invention is an apparatus for deliverying high purity gallium trichloride in the vapor phase to a gallium nitride reactor, comprising; a source of carrier gas at an elevated pressure; a purifier to remove moisture from the carrier gas; a heater capable of heating the carrier gas to at least 80° C.; a container having a supply of gallium trichloride, a valve controlled inlet for the carrier gas having a dip tube with an outlet below the level of the gallium trichloride, a valve controlled outlet for removing the carrier gas and entrained gallium trichloride; a heater capable of heating sufficient to melt the gallium trichloride; a delivery line connected to the valve controlled outlet for carrying the entrained gallium trichloride to a reaction zone for gallium nitride. A process is also described for the apparatus.

The present invention is an industrial waste water microwave electrodeless ultraviolet photocatalysis-dual membrane separation coupling treatment device, the device mainly consists of a reactor (1), a membrane separation system (2), a microwave electrodeless ultraviolet light source system (4), an aeration system, and an ozone tail gas decomposition device (7) connected to the reactor, and an inlet and outlet water system, wherein: the upper and lower parts of the reactor are respectively the reaction zone and the aeration zone, which are separated by a water distribution plate (5); the membrane separation system The microwave electrodeless ultraviolet light source system is located in the reaction zone and is separated by a corrugated partition (3); the aeration system is composed of a microporous aeration head (6) and a blower (8), and the microporous aeration head is located in the aeration At the bottom of the zone, the blower sends air to the aeration zone through the air duct. The invention has the characteristics of high reaction rate, complete degradation of organic matter, long-term operation and the like, and has strong operability and high safety. It is suitable for the treatment of refractory organic industrial wastewater, and it is also suitable for sterilization and disinfection in the field of water supply.

A biosensor in the form of a strip. In one embodiment, the biosensor strip comprises an electrode support, a first electrode, i.e., a working electrode, a second electrode, i.e., a counter electrode, and a third electrode, i.e., a reference electrode. Each of the electrodes is disposed on and supported by the electrode support. Each of the electrodes is spaced apart from the other two electrodes. The biosensor strip can include a covering layer, which defines an enclosed space over the electrodes. This enclosed space includes a zone where an analyte in the sample reacts with reagent(s) deposited at the working electrode. This zone is referred to as the reaction zone. The covering layer has an aperture for receiving a sample for introduction into the reaction zone. The biosensor strip can also include at least one layer of mesh interposed in the enclosed space between the covering layer and the electrodes in the reaction zone. This layer of mesh facilitates transporting of the sample to the electrodes in the reaction zone. In another embodiment, a biosensor strip can be constructed to provide a configuration that will allow the sample to be introduced to the reaction zone by action of capillary force. In this embodiment, the layer of mesh can be omitted. The invention also provides a method for determining the concentration of glucose in a sample of whole blood by using the biosensor of this invention.

A method and an apparatus for growing a thin film onto a substrate by the ALD process. The apparatus comprises a reaction chamber into which the substrate can be disposed; a plurality of inlet channels communicating with said reaction chamber, said inlet channels being suited for feeding the reactants employed in a thin-film growth process in the form of vapor-phase pulses into said reaction chamber; at least one outlet channel communicating with said reaction chamber, said outlet channel being suited for the outflow of reaction products and excess amounts of reactants from said reaction space; and a pre-reaction chamber arranged immediately upstream of the reaction chamber, said pre-reaction chamber forming a first reaction zone, in which the reactants of successive vapor-phase pulses can be reacted with each other in the vapor phase to form a solid product, whereas said reaction chamber forming a second reaction zone can be operated under conditions conducive to ALD growth of a thin film.

Hydrogen is produced from solid or liquid carbon-containing fuels in a two-step process. The fuel is gasified with hydrogen in a hydrogenation reaction to produce a methane-rich gaseous reaction product, which is then reacted with water and calcium oxide in a hydrogen production and carbonation reaction to produce hydrogen and calcium carbonate. The calcium carbonate may be continuously removed from the hydrogen production and carbonation reaction zone and calcined to regenerate calcium oxide, which may be reintroduced into the hydrogen production and carbonation reaction zone. Hydrogen produced in the hydrogen production and carbonation reaction is more than sufficient both to provide the energy necessary for the calcination reaction and also to sustain the hydrogenation of the coal in the gasification reaction. The excess hydrogen is available for energy production or other purposes. Substantially all of the carbon introduced as fuel ultimately emerges from the invention process in a stream of substantially pure carbon dioxide. The water necessary for the hydrogen production and carbonation reaction may be introduced into both the gasification and hydrogen production and carbonation reactions, and allocated so as transfer the exothermic heat of reaction of the gasification reaction to the endothermic hydrogen production and carbonation reaction.

Space and time co-divided atomic layer deposition (ALD) apparatuses and methods are provided. Substrates are moved (e.g., rotated) among multiple reaction zones, each of which is exposed to only one ALD reactant. At the same time, reactants are pulsed in each reaction zone, with purging or other gas removal methods between pulses. Separate exhaust passages for each reactant and purging during wafer movement minimizes particle contamination. Additionally, preferred embodiments permit different pulsing times in each reaction space, thus permitting flexibility in pulsing.

A two stage hydrodesulfurizing process for producing low sulfur distillates. A distillate boiling range feedstock containing in excess of about 3,000 wppm sulfur is hydrodesulfurized in a first hydrodesulfurizing stage containing one or more reaction zones in the presence of hydrogen and a hydrodesulfurizing catalyst. The liquid product stream thereof is passed to a first separation stage wherein a vapor phase product stream and a liquid product stream are produced. The liquid product stream, which has a substantially lower sulfur and nitrogen content then the original feedstream is passed to a second hydrodesulfurizing stage also containing one or more reaction zones where it is reacted in the presence of hydrogen and a second hydrodesulfurizing catalyst at hydrodesulfurizing conditions. The catalyst in any one or more reaction zones is a bulk multimetallic catalyst comprised of at least one Group VIII non-noble metal and at least two Group VIB metals.

The present invention provides processes for making syngas-derived products. For example, one aspect of the present invention provides a process for making a syngas-derived product, the process comprising (a) providing a carbonaceous feedstock; (b) converting the carbonaceous feedstock in a syngas formation zone at least in part to a synthesis gas stream comprising hydrogen and carbon monoxide; (c) conveying the synthesis gas stream to a syngas reaction zone; (d) reacting the synthesis gas stream in the syngas reaction zone to form the syngas-derived product and heat energy, a combustible tail gas mixture, or both; (e) recovering the syngas-derived product; and (f) recovering the heat energy formed from the reaction of the synthesis gas stream, burning the combustible tail gas mixture to form heat energy, or both.

This invention relates to a process to produce a polyalpha-olefin comprising: 1) contacting one or more alpha-olefin monomers having 3 to 24 carbon atoms with an unbridged substituted bis cyclopentadienyl transition metal compound having: 1) at least one non-isoolefin substitution on both cyclopentadientyl rings, or 2) at least two substitutions on at least one cyclopentadienyl ring, a non-coordinating anion activator, and optionally an alkyl-aluminum compound, where the molar ratio of transition metal compound to activator is 10:1 to 0.1:1, and if the alkyl aluminum compound is present then the molar ratio of alkyl aluminum compound to transition metal compound is 1:4 to 4000:1, under polymerization conditions wherein: i) hydrogen is present at a partial pressure of 0.1 to 50 psi, based upon the total pressure of the reactor or the concentration of the hydrogen is from 1 to 10,000 ppm or less by weight; ii) wherein the alpha-olefin monomer(s) having 3 to 24 carbon atoms are present at 10 volume % or more based upon the total volume of the catalyst/activator/alkylaluminum compound solutions, monomers, and any diluents or solvents present in the reaction; iii) the residence time of the reaction is at least 5 minutes; iv) the productivity of the process is at least 43,000 grams of total product per gram of transition metal compound; v) the process is continuous or semi-continuous, and vi) the temperature in the reaction zone does not rise by more than 10° C. during the reaction; and vii) ethylene is not present at more than 30 volume % of the monomers entering the reaction zone; and 2) obtaining a polyalpha-olefin (PAO), optionally hydrogenating the PAO, wherein the PAO comprises at least 50 mole % of a C3 to C24 alpha-olefin monomer, and wherein the PAO has a kinematic viscosity at 100° C. of 20 cSt or less.

A process for production of an agglomerate comprises the steps of: passing a flow of one or more gaseous reactants into a reactor; reacting the one or more gaseous reactants within a reaction zone of the reactor to form product particles; agglomerating the product particles into an agglomerate; and applying a force to the agglomerate to displace it continuously away from the reaction zone.

A radiation-heated fluidized-bed reactor and a process for producing high-purity polycrystalline silicon by using this reactor are provided. In this reactor, a heater device (14) is a radiation source for thermal radiation which is arranged outside the inner reactor tube and as a cylinder around the heater zone, without being in direct contact with the inner reactor tube. The inner reactor tube is designed in such a manner that it uses thermal radiation to heat the silicon particles in the heating zone to a temperature which is such that the reaction temperature is established in the reaction zone.

The present invention relates to a device for the specific selection of target molecules, comprising: (a) at least one reaction zone comprising a microarray, wherein the microarray comprises a substrate, on which one or more species of capture molecules are immobilized, comprising one or more temperature control and/or regulating units for controlling and/or regulating the temperature within the zone; (b) at least one non-reaction zone comprising one or more temperature control and/or regulating units for controlling and/or regulating the temperature within the zone, which is in fluid connection with the reaction zone; and (c) at least one transportation means capable of generating and/or regulating a fluid flow between said reaction zone (a) and said non-reaction zone comprising one or more temperature control and/or regulating units (b). The present invention further relates to a device for the specific selection of target molecules wherein the immobilized capture molecules are organized in the microarray in the form of spots, elongated spots and/or lines. In a further aspect the present invention relates to a method of specifically selecting target molecules, comprising the introducing a medium to such a device, performing interaction reactions in a reaction zone, transporting not interacted or not bound target molecules to a zone allowing reactivation of the target molecules and performing additional interaction reactions with the reactivated target molecules at the reaction zone, as well as the use of such a device for specifically selecting target molecules, e.g. for target enrichment also referred to as microarray based genome selection (MGS) in the literature.

A sensor is provided for the determination of various concentrations of one or more components within a fluid sample. The sensor includes an injection molded body, at least two electrodes, an enzyme, and if desired, an electron transfer mediator. The body includes a reaction zone for receiving a fluid sample. The electrodes are at least partially embedded within the plastic body and extend into the reaction zone. Also contained within the reaction zone is an enzyme capable of catalyzing a reaction involving a compound within the fluid sample. Additionally, the sensor incorporates fill detection which activates a meter, attached to the sensor, for measuring the electrochemical changes occurring in the reaction zone.

High-purity polysilicon granules are prepared by depositing reaction gas on silicon granules in a fluidized bed reactor having:

• • a reactor space comprising at least two zones lying one above the other, the lower zone weakly fluidized by introduction of a silicon-free gas into silicon granules in the lower zone by a plurality of individual dilution gas nozzles, and a second, reaction zone directly abutting the lower zone,

the reaction zone heated via its outwardly bounding wall,

introducing silicon-containing reaction gas as a vertical high speed gas jet into the reaction zone by reaction gas nozzle(s), forming local reaction gas jets surrounded by bubble-forming fluidized bed, gas decomposing leading to particle growth,

wherein the reaction gas has fully or almost fully reacted to chemical equilibrium conversion before reaching the wall or bed surface.

A chemical vapor deposition method and apparatus is disclosed. The process is carried out in an apparatus having a number reactive zones, each surrounded by a corresponding exhaust zone, all of which are both contained within a buffer zone. Pressure relationships are controlled such that buffer gas from the buffer zone flows into the exhaust zones and reactive gas from the reactive zones flow into the exhaust zones. As a result, cross-contamination of gases between the reactive zones is avoided.

The present invention is related to an electrochemical biosensing test strip, biosensing meter, system and method for analyte measurement incorporating a hematocrit correction. The biosensor strip comprises a first and a second electrode sets respectively for detecting analyte concentration and hematocrit level. The first and second electrode sets are respectively corresponding to different reaction zones and a reaction reagent is only formed on the first electrode set corresponding reaction zone. Applying a first signal comprising a DC component and a second signal comprising an AC component that has a constant frequency respectively to the first and second electrode sets can respectively detect an uncorrected analyte concentration and hematocrit level. Therefore, the corrected analyte concentration is more accurate by incorporating the hematocrit correction.

A process for the partial catalytic oxidation of a hydrocarbon containing feed comprising contacting the feed with an oxygen-containing gas in the presence of a catalyst retained within a reaction zone in a fixed arrangement, wherein the catalyst comprises at least one catalytically active metal selected from the group consisting of silver and Group VIII elements supported on a porous ceramic carrier. The porous ceramic carrier has a distribution of total pores wherein about 70% of the total pores (1) have a volume-to-surface area (V/S) ration that is within about 20% of the mean V/S value for the total pores and no pores have a V/S ration that is greater than twice the mean V/S value for the total pores; (2) have a pore-to-pore distance between neighboring pores that is within about 25% of the mean pore-to-pore distance between neighboring pores; and (3) have a pore throat area that is within about 50% of the mean pore throat are for the pores. Additionally, about 50% of the total pores have a coordination number between neighboring pores that is within about 25% of the mean coordination number between neighboring pores. Preferably, the oxidation process comprises a multistage, staged oxygen, catalytic partial oxidation process having fewer than or equal to about five stages and including a first stage preheat temperature of greater than about 550° C., and wherein the temperature of the product mixture in each stage following the first stage is at least about 700° C.