| 序号 | 专利名 | 申请号 | 申请日 | 公开（公告）号 | 公开（公告）日 | 发明人 |
|---|---|---|---|---|---|---|
| 201 | Method and apparatus for steam hydro-gasification in a fluidized bed reactor | US11879267 | 2007-07-16 | US07619012B2 | 2009-11-17 | Joseph M. Norbeck; Chan Seung Park; Surinder P. Singh |
| A method and apparatus for converting carbonaceous material to a stream of methane and carbon monoxide rich gas by heating the carbonaceous material in a fluidized bed reactor using hydrogen, as fluidizing medium, and using steam, under reducing conditions at a temperature and pressure sufficient to generate a stream of methane and carbon monoxide rich gas but at a temperature low enough and/or at a pressure high enough to enable the carbonaceous material to be fluidized by the hydrogen. In particular embodiments, the carbonaceous material is fed as a slurry feed, along with hydrogen, to a kiln type reactor before being fed to the fluidized bed reactor. Apparatus is provided comprising a kiln type reactor, a slurry pump connected to an input of the kiln type reactor, means for connecting a source of hydrogen to an input of the kiln type reactor; a fluidized bed reactor connected to receive output of the kiln type reactor for processing at a fluidizing zone, and a source of steam and a source of hydrogen connected to the fluidized bed reactor below the fluidizing zone. Optionally, a grinder can be provided in the kiln type reactor. | ||||||
| 202 | Process and Apparatus for the Separation of Methane from a Gas Stream | US12395330 | 2009-02-27 | US20090260287A1 | 2009-10-22 | Francis S. Lau |
| Processes for conversion of a carbonaceous composition into a gas stream comprising methane are provided, where an energy-efficient process and/or apparatus is used to separate methane out of a gas stream comprising methane, carbon monoxide, and hydrogen. Particularly, methane can be separated from hydrogen and carbon monoxide using novel processes and/or apparatuses that generate methane hydrates. Because hydrogen and carbon monoxide do not readily form hydrates, the methane is separated from a gas stream. The methane can be captured as a substantially pure stream of methane gas by dissociating the methane from the hydrate and separating out any residual water vapor. | ||||||
| 203 | Processes for Making Syngas-Derived Products | US12342628 | 2008-12-23 | US20090165381A1 | 2009-07-02 | Earl T. Robinson |
| 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. | ||||||
| 204 | HYDROGEN AND CARBON UTILIZATION IN SYNTHETIC FUELS PRODUCTION PLANTS | US12207978 | 2008-09-10 | US20090064584A1 | 2009-03-12 | Sergio Mohedas; Mark Ibsen |
| A method of utilizing hydrogen in synthesis gas production by forming synthesis gas from one or more carbonaceous materials, the synthesis gas comprising hydrogen and carbon monoxide; separating a hydrogen-rich product and a hydrogen-lean product from the synthesis gas to yield an adjusted synthesis gas product; and activating a hydrocarbon synthesis catalyst with at least a portion of the hydrogen-lean product. A system for carrying out the method is also provided, the system including at least one hydrogen extraction unit and an activation reactor operable to activate hydrocarbon synthesis catalyst, wherein the activation reactor comprises an inlet fluidly connected with the at least one hydrogen extraction unit whereby at least a portion of a hydrogen-lean gas stream, at least a portion of a hydrogen-rich gas stream, or at least a portion of both may be introduced into the activation reactor. | ||||||
| 205 | Method and apparatus for steam hydro-gasification with increased conversion times | US12218653 | 2008-07-16 | US20080312348A1 | 2008-12-18 | Chan Seung Park; Joseph M. Norbeck |
| A method and apparatus for converting carbonaceous material to a stream of carbon rich gas, comprising heating a slurry feed containing the carbonaceous material in a hydrogasification process using hydrogen and steam, at a temperature and pressure sufficient to generate a methane and carbon monoxide rich stream in which the conversion time in the process is between 5 and 45 seconds. In particular embodiments, the slurry feed containing the carbonaceous material is fed, along with hydrogen, to a kiln type reactor before being fed to the fluidized bed reactor. Apparatus is provided comprising a kiln type reactor, a slurry pump connected to an input of the kiln type reactor, means for connecting a source of hydrogen to an input of the kiln type reactor; a fluidized bed reactor connected to receive output of the kiln type reactor for processing at a fluidizing zone, and a source of steam and a source of hydrogen connected to the fluidized bed reactor below the fluidizing zone. Optionally, a grinder can be provided in the kiln type reactor. | ||||||
| 206 | Method And Apparatus For Separating Gases | US11686982 | 2007-03-16 | US20080223214A1 | 2008-09-18 | John Eugene Palamara; Kevin Boyle Fogash |
| A method and apparatus for removing carbon dioxide from a synthesis gas stream containing hydrogen is disclosed. The method includes absorbing the carbon dioxide using a physical solvent under high pressure and then liberating the carbon dioxide in a series of expansion stages where the pressure on the solvent is reduced. The expansion ratio increases with each expansion stage. The apparatus includes expansion stages having throttling devices and expansion tanks operated at increasing expansion ratios. Carbon dioxide is liberated in this manner so as to minimize the energy required compress for transport via a pipe line for sequestration of the gas. Sequestration of the carbon dioxide is preferred to atmospheric venting to curb the release of greenhouse gases. | ||||||
| 207 | Operation of a steam methane reformer by direct feeding of steam rich producer gas from steam hydro-gasification | US11489308 | 2006-07-18 | US20080021119A1 | 2008-01-24 | Joseph M. Norbeck; Chan Seung Park |
| An improved, economical alternative method to supply steam and methane to a steam methane reformer (SMR) is accomplished by a combination of procedures, wherein product gas from a steam hydro-gasification reactor (SHR) is used as the feedstock for the SMR by removing impurities from the product stream from the SHR with a gas cleanup unit that operates substantially at process temperatures and pressures and is located between the SHR and SMR. | ||||||
| 208 | Method of operating fuel cell system and fuel cell system | US10582491 | 2004-12-10 | US20070122666A1 | 2007-05-31 | Qingquan Su; Toshihiro Horie; Masaki Ando; Takahide Haga |
| To provide a fuel cell power generation system which has no assist combustion system and thus is simple in structure and a method for starting the fuel cell power generation system and controlling the operation of the fuel cell power generation system, in order to provide a fuel cell power generation system which operates stably with a high reliability. In a fuel cell power generation system having a reforming section 5 for reforming a raw material fuel m to produce reformate r; a combustion section 4 for burning the raw material fuel to heat the reforming section; carbon monoxide reduction section 6 and 7 for reducing the content of carbon monoxide in the reformate to produce carbon monoxide reduced gas g; and a fuel cell 30 which uses the carbon monoxide reduced gas as fuel gas, the raw material fuel is supplied to the combustion section to heat the reforming section to a predetermined temperature, supply of the raw material fuel to the combustion section is stopped, the raw material fuel is supplied to the reforming section to produce reformate, the reformate is introduced into the carbon monoxide reduction section to heat the carbon monoxide reduction section, and the carbon monoxide reduced gas generated in the carbon monoxide reduction section is introduced into the fuel cell to generate electric power. | ||||||
| 209 | Solid waste refining and conversion to methanol | US486394 | 1990-02-28 | US5104419A | 1992-04-14 | Harald F. Funk |
| A process for converting solid waste into a synthesis suitable for producing liquid fuel, comprising (a) partially oxidizing and combusting solid waste material in a closed combustion zone at a temperature of 800.degree.-1000.degree. C. and at a pressure below ambient to produce combustion gases by introducing into the combustion zone a gaseous oxidant comprising oxygen having a purity of at least 95% by volume and carbon dioxide in an oxygen to carbon dioxide ratio, by volume, of about 50:50, (b) conducting the combustion gases, oxygen and carbon dioxide through the solid waste material; (c) withdrawing a producer gas comprising the combustion gases and any unreacted oxygen and carbon dioxide; (d) removing particulate matter from the producer gas; (e) separating carbon dioxide from the producer gas and recycling a portion of the separated carbon dioxide to the combustion zone; (f) separating the less volatile, condensable components of the carbon dioxide-free producer gas, from the more volatile, non-condensable synthesis gas components thereof, and (g) compressing the producer gas at some time prior to the completion step (e). In a preferred embodiment, the more volatile components and at least a portion of the separated carbon dioxide from step (e) are admixed and the resulting admixed gas mixture is reacted to form methanol. Preferably, the less volatile components are converted by chemical reaction to hydrogen and the hydrogen is recycled into admixture with the producer gas at some time prior to the commencement of step (e). | ||||||
| 210 | Process for gasification of cellulosic materials | US865056 | 1986-05-20 | US4699632A | 1987-10-13 | Suresh P. Babu; Gerald L. Anderson; Satyendra P. Nandi |
| A process for gasification of cellulosic materials in a single gasification vessel wherein the cellulosic materials are introduced directly into a single back-mixed fluidized bed of high heat capacity inert solids. The fluidized bed is maintained at temperatures of about 1200.degree. to about 1600.degree. F., pressures of up to about 500 psig devolatilizing the cellulosic materials. A substantial portion of the heavier hydrocarbons produced by devolatilization of the cellulosic materials is reformed within the gasification vessel and a substantial portion of the devolatilized cellulosic materials is gasified by reaction with hydrogen and steam within the fluidized bed. Cellulosic materials residue is combusted in an oxygen-rich atmosphere in the lower portion of the fluidized bed to principally form heat and cellulosic materials ash. The highly back-mixed fluidized bed results in temperature variation along the height of the bed, including the combustion zone, of less than 100.degree. F. and preferably less than about 90.degree. F. Introduction of cellulosic materials feed to the fluidized bed is vertically adjustable and maintained at a position where the combustion consumes principally cellulosic materials residue. Formed gases, vapor and biomass ash are removed from the top of the gasification vessel in the gas stream. The process provides high throughput, efficient production of low and medium Btu fuel gas. The medium Btu fuel gas may be readily upgraded to high Btu SNG. At least half of the methane required for SNG is produced in the gasification vessel. | ||||||
| 211 | Process for increasing the heating value of fuel gas mixtures containing hydrogen | US375110 | 1982-05-05 | US4569890A | 1986-02-11 | Gunter Barthel |
| Fuel gas mixtures of different composition containing hydrogen may be the main products or by-products of chemical conversion processes such as, without limitation, processes for the conversion of solid or liquid fuels. Such gas mixtures are, however, normally not fit for public gas supplies, as their heating value and their density and other properties would normally not conform to the standards and the codes of practice for gas properties. Methanation is a known process for the conversion of hydrogen-rich fuel gas mixtures into gases conforming to standard specifications. During the exothermal reaction of methanation, more than 15% of the enthalphy of the reactants may be lost.The invention allows the increase of the heating value of hydrogen-rich fuel gas mixtures, said increase being achieved at a high efficiency and maximizing the recovery of useful energy in the form of gas conforming to standards and electric power.The invention employs a fuel cell unit to which the complete gas mixture is supplied and in which part or all of the hydrogen contained in said gas mixture is oxidized by an electrochemical reaction and from which the constituents not so oxidized are removed inclusive of any hydrogen which may not have been so oxidized. | ||||||
| 212 | Process of producing a synthesis gas which has a low inert gas content | US488472 | 1983-04-25 | US4515604A | 1985-05-07 | Karl-Heinz Eisenlohr; Hans Gaensslen; Manfred Kriebel; Heiner Tanz |
| In a process of producing a synthesis gas which has a low inert gas content and is intended for the synthesis of alcohols, particularly of methanol, and of hydrocarbons, and which is produced from coal or heavy hydrocarbons, by a gasification under pressure with oxygen and steam, whereafter the raw gas is cooled, the impurities are removed by a scrubbing with methanol, and the methanol is removed by means of molecular sieves from the cold pure gas. The pure gas is then cooled further and partly liquefied, the remaining gas is further cooled by a pressure relief and methane is distilled from the liquid part with simultaneous recovery of the synthesis gas, which consists of hydrogen and carbon monoxide and has a low methane content. All or part of the methane is compressed and is subsequently reacted with steam and oxygen to produce carbon monoxide and hydrogen. The produced gas is admixed to the synthesis gas or to the partly purified raw gas. | ||||||
| 213 | Method for processing coke oven gas | US928468 | 1978-07-27 | US4235624A | 1980-11-25 | Dietrich Wagener; Claus Flockenhaus; Joachim F. Meckel |
| Hot coke oven gas is subjected, immediately after the discharge thereof from coke ovens, and without any preliminary cooling operation, to partial oxidation and cracking with an oxygen-containing gas, thereby forming a hot cracked gas rich in carbon monoxide and hydrogen. The hot coke oven gas may be subjected to a desulfurization operation prior to the partial oxidation and cracking. Alternatively, the hot cracked gas may be subjected to a desulfurization operation after the partial oxidation and cracking. When the coke ovens are part of an overall metallurgical installation which includes an air separation and dissociation plant for obtaining substantially pure oxygen, the oxygen-containing gas employed in the partial oxidation and cracking may comprise oxygen enriched gas which is taken from an intermediate stage of the air separation and dissociation plant. | ||||||
| 214 | Process for the manufacture of fuel gas | US974221 | 1978-12-29 | US4211540A | 1980-07-08 | David Netzer |
| An improved process is disclosed for the production of fuel gas such as synthetic natural gas from coal. A sized coal feed of larger particle size is gasified in a moving bed gasifier such as the British Gas/Lurgi slagging gasifier, and forms a methane rich synthesis gas containing heavy and light organics which is quenched to form a water phase containing dissolved phenolic and other compounds. The water phase is separated from the gas phase and insoluble organics and mixed with a second portion of the coal containing fine particles which are not suitable for moving bed gasification to form a slurry. This coal-phenolic water slurry is gasified in an entrained bed gasifier, for example, the Texaco partial oxidation process, and forms a methane lean synthesis gas. The phenol, ammonia and dissolved organics in the water phase are destroyed and converted to valuable product gas. At least part of this product gas may be blended with the moving bed product gas for further processing to produce the desired fuel gas product. The product gas from the entrained bed gasifier is also suitable for production of hydrogen, ammonia, or methanol. | ||||||
| 215 | Process for conveying hot crude coke oven gas from coke ovens to a position of utilization while preventing condensation of higher hydrocarbons | US865723 | 1977-12-29 | US4178266A | 1979-12-11 | Rudolf Burkert; Claus Flockenhaus; Joachim F. Meckel; Dietrich Wagener |
| As hot crude coke oven gas is conveyed from coke ovens to a position of utilization, condensation of higher hydrocarbons from the coke oven gas is prevented by increasing the temperature of the coke oven gas to a temperature such that higher hydrocarbons are prevented from condensing therefrom. This increase in temperature may be achieved by injecting oxygen-containing gas into the hot crude coke oven gas, to thereby produce a partial combustion of the coke oven gas. Alternatively, when the coke oven gas is being conveyed to a thermal cracking reactor wherein the coke oven gas is thermally cracked to form a cracked gas, the temperature of the coke oven gas may be increased by passing the coke oven gas through a heat exchanger in indirect heat exchange relation with the cracked gas. | ||||||
| 216 | Process for enhancing the fuel value of low BTU gas | US817576 | 1977-07-21 | US4134907A | 1979-01-16 | Frank M. Stephens, Jr. |
| A process for increasing the fuel value of a gas mixture of carbon monoxide and hydrogen by converting part of the hydrogen and part of the carbon in the carbon monoxide of the gas mixture to methane, which comprises continuously introducing the gas mixture into a fluid bed in the presence of iron under conditions of pressure and temperature which promote the reduction of carbon monoxide to carbon, the formation of iron carbide from the iron and carbon, and the formation of methane and iron from iron carbide and hydrogen, and continuously removing from the fluid bed a methane enriched gas mixture including carbon monoxide and hydrogen having a substantially increased fuel value over the gas mixture introduced into the fluid bed. | ||||||
| 217 | Lng refrigerant for fractionator overhead | US3524897D | 1968-10-17 | US3524897A | 1970-08-18 | KNIEL LUDWIG |
| 218 | Utilization of propane recovered from liquefied natural gas | US3456032D | 1966-03-14 | US3456032A | 1969-07-15 | KNIEL LUDWIG |
| 219 | Method of removing carbon monoxide from gas mixtures | US16031661 | 1961-12-18 | US3185540A | 1965-05-25 | BRECK DONALD W; CASTOR CHARLES R; MILTON ROBERT M |
| 220 | Carbon dioxide removal from vapor mixtures | US336460 | 1960-01-19 | US3078639A | 1963-02-26 | MILTON ROBERT M |
QQ群二维码
意见反馈
意见反馈