University of California

Other

The United States of America As Represented by the United States Energy

Gas Technology Institute

Hydro-chlor International, Inc.

Scott D Lynn

Donald N Hanson

Steven F Sciamanna

Aldo F Sciamanna

Howard S Meyer

Dennis Leppin

Arunabha Basu

James R Wangerow

David T Clay

Bernard J Dubs

Gavin P Towler

The present general inventive concept is directed to a chainsaw sharpening device including a cutting tooth sharpener, a base coupled to the cutting tooth sharpener, a first side member coupled to the base and configured to face a first side of a chainsaw bar, a second side member coupled to the base and configured to face a second side of the chainsaw bar, and a guide member coupled to the base and configured to be slidable along a plurality of top plates of a respective plurality of cutting teeth of a saw chain mounted on the chainsaw bar, wherein the chainsaw sharpening device is configured to be moved to a desired cutting tooth of the mounted saw chain to perform a sharpening procedure without being fixed to the chainsaw bar.

Chainsaw sharpening device, system, and method

A multi-stage UCSRP process and system for removal of sulfur from a gaseous stream in which the gaseous stream, which contains a first amount of HS, is provided to a first stage UCSRP reactor vessel operating in an excess SOmode at a first amount of SO, producing an effluent gas having a reduced amount of SO, and in which the effluent gas is provided to a second stage UCSRP reactor vessel operating in an excess HS mode, producing a product gas having an amount of HS less than said first amount of HS.

Process and system for removing sulfur from sulfur-containing gaseous streams

HS-containing gases, particularly such gases at elevated pressure, are treated to remove HS by reaction in a liquid medium with SO, the SObeing present in stoichiometric excess with respect to the HS. The SOis produced by combustion of sulfur, preferably sulfur produced in the reaction between HS and SO, preferably with oxygen. The process produces a treated gas that is substantially free of both HS and SO. An acid-gas absorber/stripper system or other system typically found in such processes to raise or concentrate the HS level in the gas to be treated, is not needed in operations according to the invention.

Process for sulfur removal suitable for treating high-pressure gas streams

H S is removed from an H S-rich gas, and sulfur is produced, by a process in which the H S-rich gas is reacted with SO in a reactor in the presence of an organic solvent and a catalyst, an H S-containing off-gas is removed from the reactor and is combusted to produce an SO -rich combustion gas. Preferably, the reactor off-gas is combusted with a substoichiometric amount of oxygen so that the combustion gas also contains water vapor and sulfur vapor. The combustion gas is cooled by direct quench or indirect heat exchange to produce an aqueous stream comprising primarily water and containing suspended solid sulfur and polythionic acids, e.g., a Wackenroder's liquid, and the aqueous stream is used to provide cooling for the H S&mdash;SO reaction. Problems associated with production and handling of Wackenroder's liquids are overcome and sulfur values in these materials are recovered.

Method of recovering sulfurous components in a sulfur-recovery process

Elemental sulfur is recovered from the hydrogen sulfide present in natural gases and other process gases by treating the hydrogen sulfide-containing gas in a series arrangement of a liquid-phase reactor; a furnace and a sulfur dioxide absorber. The hydrogen sulfide-containing gas and a sulfur dioxide-containing gas are fed into the liquid-phase reactor where they are dissolved into a solvent, such as polyglycol monoethers, diethers of ethylene glycol, diethers of propylene glycol, etc., and react in the presence of a catalyst, such as tertiary amine, pyridine, isoquinoline, etc., to produce elemental sulfur. The feed rates of the hydrogen sulfide-containing gas and the sulfur dioxide-containing gas are selected so that there will be an excess of hydrogen sulfide in the solvent thereby ensuring that the reaction products will include, not only the elemental sulfur, but also residual, unreacted hydrogen sulfide. The residual, unreacted hydrogen sulfide is fed into a furnace, where it is combusted into a sulfur dioxide-containing gas. The sulfur dioxide-containing gas is fed into a sulfur dioxide absorber, where the sulfur dioxide is extracted from the gas and recycled back to the liquid phase reactor as the aforementioned sulfur dioxide-containing gas.

Process for recovering sulfur from H2S-bearing gas

Elemental sulfur is recovered from the hydrogen sulfide present in natural gas or other process gases by passing the hydrogen sulfide contaminated gas through a hydrogen sulfide absorber so as to obtain a natural or other process gas having a diminished amount of hydrogen sulfide and stripping the hydrogen sulfide out the resulting hydrogen sulfide rich solution so as to obtain a hydrogen sulfide rich gas; feeding the hydrogen sulfide rich gas and sulfur dioxide into a reactor so that the following reaction takes occurs, 2H.sub.2 S+SO.sub.2 .fwdarw.3/2S.sub.2 +2H.sub.2 O under such conditions that there is approximately a 50 percent stoichiometric excess of hydrogen sulfide; combusting the residual, unreacted hydrogen sulfide to convert it into sulfur dioxide, and passing the resulting sulfur dioxide back into the reactor where the reaction between hydrogen sulfide and sulfur dioxide occurs.

Process employing single-stage reactor for recovering sulfur from H.sub.2 S

An electrolytic chlorine gas generating system is disclosed. The system includes an electrolytic cell generating the chlorine gas, a brine tank supplying saturated brine to the anode compartment of the cell, and an acid feed tank containing hydrochloric acid at sufficient concentration to maintain the anolyte brine at less than about pH 4.0. In operation, the brine tank contains solid sodium chloride which dissolves in the brine and replenishes the anolyte brine solution as chloride ion is consumed during electrolysis. The acid feed tank is in fluid communication with the brine tank so that the brine is maintained at a constant volume during electrolysis. A caustic system is also disclosed including a means for controlling caustic delivery.

Caustic concentration regulator for chlorine generators

Elemental sulfur is recovered from the H.sub.2 S present in gases derived from fossil fuels by heating the H.sub.2 S with CO.sub.2 in a high-temperature reactor in the presence of a catalyst selected as one which enhances the thermal dissociation of H.sub.2 S to H.sub.2 and S.sub.2. The equilibrium of the thermal decomposition of H.sub.2 S is shifted by the equilibration of the water-gas-shift reaction so as to favor elemental sulfur formation. The primary products of the overall reaction are S.sub.2, CO, H.sub.2 and H.sub.2 O. Small amounts of COS, SO.sub.2 and CS.sub.2 may also form. Rapid quenching of the reaction mixture results in a substantial increase in the efficiency of the conversion of H.sub.2 S to elemental sulfur. Plant economy is further advanced by treating the product gases to remove byproduct carbonyl sulfide by hydrolysis, which converts the COS back to CO.sub.2 and H.sub.2 S. Unreacted CO.sub.2 and H.sub.2 S are removed from the product gas and recycled to the reactor, leaving a gas consisting chiefly of H.sub.2 and CO, which has value either as a fuel or as a chemical feedstock and recovers the hydrogen value from the H.sub.2 S.

Process for recovery of sulfur from acid gases

An electrolytic chlorine gas generating system is disclosed. The system includes an electrolytic cell generating the chlorine gas, a brine tank supplying saturated brine to the anode compartment of the cell, and an acid feed tank containing hydrochloric acid at sufficient concentration to maintain the anolyte brine at less than about pH 4.0. In operation, the brine tank contains solid sodium chloride which dissolves in the brine and replenishes the anolyte brine solution as chloride ion is consumed during electrolysis. The acid feed tank is in fluid communication with the brine tank so that the brine is maintained at a constant volume during electrolysis.

Chlorine generator

A process of removing hydrogen sulfide from a gas stream in which the hydrogen sulfide is dissolved in an absorption zone by a solvent having a good solvent power for hydrogen sulfide and a much greater solvent power for sulfur dioxide. The resultant solution is divided into a major stream and a minor stream. The major stream is contacted with a small excess of sulfur dioxide over that required for reaction with hydrogen sulfide. Most of this solution is recycled to the absorption zone. The minor stream withdrawn from the absorption zone is mixed with the solution formed in the reaction zone which is not recycled, the proportion being such that there remains a small excess of hydrogen sulfide in solution. This solution is then stripped of hydrogen sulfide. By this means only a small fraction of the solution has to be stripped. Preferred solvents are those which promote the reaction of hydrogen sulfide with sulfur dioxide.

Regeneration of solvent in H.sub.2 S removal from gases

Method of crystallizing from aqueous solution an inorganic solute, whose solubility in water varies relatively litter with temperature such that crystallizing by adjustment of temperature results in low yield, such method comprising contacting a concentrated aqueous solution of the solute with a hydrophilic organic solvent at a temperature T.sub.1, T.sub.1 and the organic solvent being selected such that at T.sub.1 a water-rich phase is formed in which the ratio of solute to water is less than the ratio found in the incoming aqueous solution, resulting in formation of crystals of solute. The resulting wet, organic-rich phase is separated and dried by contact with a concentrated aqueous solution of the solute at T.sub.2. T.sub.2 differs from T.sub.1, preferably being less than T.sub.1 if the solute dissolves exothermically in water and preferably being greater than T.sub.1 if the solute dissolves endo- thermically in water. The resulting dried organic phase is recycled to the crystallizing zone. The resulting diluted aqueous solution is used to dissolve solid solute to provide the concentrated solution. In some cases the wet organic phase will separate into two phases at T.sub. 2, one solvent-rich phase and one water-rich phase, and the water-rich phase may then be treated to remove water from the process. A portion of the diluted aqueous solution may be employed to adjust the concentration of solution going to the crystallizing zone to the desired concentration.

Method of crystallizing salts from aqueous solutions

Method of treating an aqueous solution of a non-volatile inorganic solute to produce a more concentrated solution or to crystallize solid solute from the solution. The solution is contacted at a higher temperature T.sub.1 with a suitable organic liquid to extract water and form an organic phase (organic liquid contacting water). The organic phase, separated, cooled and contacted at a lower temperature T.sub.2 with a drying medium to dry the organic liquid which is then re-used to treat a further quantity of aqueous solution. The drying medium may be a portion of the concentrated aqueous solution resulting from the first step, or it may be a concentrated aqueous solution or a slurry from an outside source, or it may be a combination of two such drying media.

Method of treating aqueous solutions

Method of concentrating aqueous solutions of non-volatile, ionic solutes by extracting water from the solution by means of a polar organic liquid (or a solution of a polar organic liquid and a non-polar organic liquid) at an elevated temperature and cooling the organic liquid to separate a water phase, the extractant and the temperatures being chosen such that water has a relatively high solubility in the extractant at the higher temperature and a relatively low solubility at the lower temperature; the extractant being also chosen to meet certain other criteria such as inertness toward the solution and equipment. Advantage is taken of the diminished activity coefficient of water in polar organic liquids at elevated temperatures and in the case of certain solutions, advantage is also taken of the increased activity coefficient of water in aqueous ionic solution at elevated temperatures.

Method of concentrating aqueous solutions

Process of carrying out oxidation-reduction reactions such as oxidation of hydrogen sulfide to sulfur, in which a polyvalent metal chelate with a certain class of polycarboxylic acid is employed, the metal being reduced from a higher valence state to a lower valence state during reduction and back to the higher valence state by oxidation. The class of polycarboxylic acids are those which have a substituent which enhances acidity yet is stable toward oxidation.

Method of oxidizing a polyvalent metal

Presented is an apparatus and method for producing small quantities of chlorine and sodium hydroxide or sodium hypochlorite, useful in many applications where the major investment of a full-blown chemical plant capable of producing tons of product per day is not economically feasible. The apparatus of the invention includes the use of an electrolytic cell embodying an anode chamber charged with an acidic, concentrated sodium chloride solution and a cathode chamber charged with a basic aqueous solution and through which an electric current may be passed under controlled conditions to initiate and maintain a reaction that produces chlorine gas in the anode chamber and hydrogen gas and a solution of sodium hydroxide in the cathode chamber. The anode and cathode chambers are separated by a chemically-resistant ion-exchange membrane permeable only to positively charged ions. Anolyte and catholyte feed tanks are arranged in association with appropriate anolyte and catholyte surge tanks connected to the electrolytic cell in such a way that the reaction proceeds continuously without the need for mechanical pumps. The chlorine and the sodium hydroxide solution may leave the apparatus as separate product streams, or, in a second aspect of the invention, may be combined to form (as yet another product) a solution of sodium hypochlorite.

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Tellico Plains, TN, United States of America

Scott D Lynn