Method of treating an off-gas stream and an apparatus therefor

The present invention provides a method of treating an off-gas stream ( 80 ) comprising NH 3 and H 2 S to provide a sulphate stream ( 910 ), the method comprising the steps of: (i) providing a first off-gas stream ( 80 ) comprising NH 3 , H 2 S, CO 2 and optionally one or more of HCN, COS and CS 2 ; (ii) passing the first off-gas stream ( 80 ) to an incinerator ( 300 ) to oxidise NH 3 , H 2 S, and optionally one or more of HCN, COS and CS 2 to provide a second off-gas stream ( 310 ) comprising N 2 , H 2 O, SO 2 and CO 2 ; (iii) scrubbing the second off-gas stream ( 310 ) with a first aqueous alkaline stream ( 380, 876 a ) in a caustic scrubber ( 350 ) to separate SO 2 and a part of the CO 2 from the second off-gas stream to provide a spent caustic stream ( 360 ) comprising carbonate and one or both of sulphite and bisulphite and a caustic scrubber off-gas stream ( 370 ) comprising N 2 and CO 2 ; and (iv) passing the spent caustic stream ( 360 ) to an aerator ( 900 ) comprising sulphur-oxidising bacteria in the presence of oxygen to biologically disc sulphite and bisulphite to sulphate to provide a sulphate stream ( 910 ).

Generation of hydrogen from hydrocarbon bearing materials

Disclosed are strategies for the economical microbial generation of hydrogen, useful as an alternative energy source, from hydrocarbon-rich deposits such as coal, oil and/or gas formations, oil shale, bitumen, tar sands, carbonaceous shale, peat deposits and sediments rich in organic matter through the management of the metabolism of microbial consortia.

System and Method for Processing Alternate Fuel Sources

An energy conserving wastewater treatment system capable of being fueled by alternate fuel sources comprises a synthesis gas generator that produces synthesis gas from a fuel and an organic waste digester that produces biogas. A combined synthesis gas and biogas storage reservoir that is in communication with both the synthesis gas generator and the organic waste digester. At least one boiler is in communication with the combined synthesis gas and biogas storage reservoir.

Methods and Systems for the Production of Hydrocarbon Products

Methods and systems for the production of hydrocarbon products, including providing a substrate comprising CO to a bioreactor containing a culture of one or more micro-organisms; and fermenting the culture in the bioreactor to produce one or more hydrocarbon products. The substrate comprising CO is derived from an industrial process selected from the group comprising steam reforming processes, refinery processes, steam cracking processes, and reverse water gas shift processes.

Generation of hydrogen from hydrocarbon bearing materials

Disclosed are strategies for the economical microbial generation of hydrogen, useful as an alternative energy source, from hydrocarbon-rich deposits such as coal, oil and/or gas formations, oil shale, bitumen, tar sands, carbonaceous shale, peat deposits and sediments rich in organic matter through the management of the metabolism of microbial consortia.

REACTOR AND PROCESS FOR GASIFYING AND/OR MELTING OF FEED MATERIALS

A reactor enables gasification or melting of waste and additional feed materials. The reactor includes a co-current section with a plenum section and a feed section with a sluice. Feed materials are introduced into the reactor. The reactor further includes a buffer section and a pre-treatment section, which adjoins a bottom of the buffer section to create a cross-sectional enlargement. An intermediate section adjoins the pre-treatment section. An upper oxidation section adjoins a bottom of the intermediate section and includes tuyeres in at least one level. An upper reduction section adjoins a bottom of the upper oxidation section. The reactor further includes a gas outlet section. The reactor further includes a countercurrent section having a conical lower reduction section and a conical lower oxidation section adjoining the conical lower reduction section having at least one tuyere and at least one tapping. 1100. Reactor () for gasifying and/or melting of feed materials , the reactor comprising{'b': '110', 'claim-text': [{'b': '111', 'claim-text': [{'b': 112', '100, 'a feed section with a sluice () through which the feed materials are introduced into the reactor () from above,'}, {'b': 113', '112, 'a buffer section () located below the feed section (),'}, {'b': 114', '113', '140, 'a pre-treatment section () that is located below the bottom of the buffer section () and which has a cross-sectional enlargement in the upper area and a narrowing cross-section in the bottom area so that a discharge cone () of the feed material can form,'}, {'b': 119', '114', '114, 'at least one gas supply means () which open in the pre-treatment section () in the region of the cross-sectional enlargement of the pre-treatment section () and through which hot gases can be fed to the discharge cone, and'}, {'b': 115', '114, 'an intermediate section () that is located below the bottom of the pre-treatment section (),'}], 'a plenum section () comprising'}, {'b': 116', '115', '116', '117', ' ...

Combined Hydrothermal Liquefaction and Catalytic Hydrothermal Gasification System and Process for Conversion of Biomass Feedstocks

A combined hydrothermal liquefaction (HTL) and catalytic hydrothermal gasification (CHG) system and process are described that convert various biomass-containing sources into separable bio-oils and aqueous effluents that contain residual organics. Bio-oils may be converted to useful bio-based fuels and other chemical feedstocks. Residual organics in HTL aqueous effluents may be gasified and converted into medium-BTU product gases and directly used for process heating or to provide energy. 119-. (canceled)20. A continuous biomass conversion process , comprising the steps of:providing a biomass conversion product comprising a bio oil fraction and an aqueous fraction, wherein each fraction is separable from the other fraction;without the aid of gravitational separation, continuously separating the bio oil fraction from the aqueous fraction; andconverting at least a portion of the aqueous fraction to a product gas containing a fuel gas.21. The process of claim 20 , wherein prior to continuously separating the bio oil fraction from the aqueous fraction claim 20 , further comprising removing solids from the biomass conversion product.22. The process of claim 20 , further comprising combusting the product gas to generate power.23. The process of claim 20 , wherein the product gas comprises one or more of methane claim 20 , hydrocarbons with a carbon number greater than that of methane claim 20 , and carbon dioxide claim 20 , wherein the product gas optionally comprises less than 5% hydrogen by weight.24. A continuous biomass conversion process claim 20 , comprising the steps of:providing a biomass conversion product comprising a bio oil fraction and an aqueous fraction, wherein each fraction is separable from the other fraction;using centrifugal force, continuously separating the bio oil fraction from the aqueous fraction; andconverting at least a portion of the aqueous fraction to a product gas containing a fuel gas.25. The process of claim 24 , wherein the separation is ...

Method for producing an organic substance

Provided is a method for producing an organic substance, in which an organic material (metabolite) derived from a microorganism is reduced while retaining a nutritive substance in an organic substance-containing solution discharged from a fermentation tank containing the microorganism, whereby various nutritional elements contained in the organic substance-containing solution can be reused with high efficiency. A method for producing an organic substance by the microbial fermentation of a synthetic gas containing at least carbon monoxide, the method comprising a synthetic gas supply step of supplying the synthetic gas into a fermentation tank containing a microorganism, a fermentation step of subjecting the synthetic gas to microbial fermentation in the fermentation tank, an aerobic fermentation treatment step of subjecting at least a portion of a liquid produced in the fermentation step to an aerobic fermentation treatment in a liquid waste treatment unit, and a recycling step of supplying a liquid produced in the aerobic fermentation treatment step to the fermentation tank, wherein the aerobic fermentation treatment step is carried out in the presence of a nitrifying bacterium inhibitor.

Solids circulation system and method for capture and conversion of reactive solids with fluidized bed temperature control

A solids circulation system receives a gas stream containing char or other reacting solids from a first reactor. The solids circulation system includes a cyclone configured to receive the gas stream from the first reactor, a dipleg from the cyclone to a second reactor, and a riser from the second reactor which merges with the gas stream received by the cyclone. The second reactor has a dense fluid bed and converts the received materials to gaseous products. A conveying fluid transports a portion of the bed media from the second reactor through the riser to mix with the gas stream prior to cyclone entry. The bed media helps manipulate the solids that is received by the cyclone to facilitate flow of solids down the dipleg into the second reactor. The second reactor provides additional residence time, mixing and gas-solid contact for efficient conversion of char or reacting solids.

PULVERIZED-FUEL SUPPLY UNIT AND METHOD, AND INTEGRATED GASIFICATION COMBINED CYCLE

A pulverized-fuel supply unit includes a hopper, first nozzles, second nozzles, a pressurizing-gas supply device, a fluidization-gas supply device, and a pulverized-fuel supply line. The hopper has a hollow to store therein pulverized fuel. The first nozzles are provided to the hopper. The second nozzles are provided to a vertically lower part of the hopper below the plurality of first nozzles. The pressurizing-gas supply device is configured to supply pressurizing gas to increase internal pressure of the hopper. The fluidization-gas supply device is configured to supply fluidization gas to fluidize the pulverized fuel in the hopper. The pulverized-fuel supply line is provided to a vertically lower part of the hopper. The pressurizing-gas supply device supplies pressurizing gas to the first nozzles and the second nozzles. The fluidization-gas supply device supplies fluidization gas to the second nozzles. 1. A pulverized-fuel supply unit comprising:a hopper having a hollow to store therein pulverized fuel;a plurality of first nozzles provided to the hopper;a plurality of second nozzles provided to a vertically lower part of the hopper below the plurality of first nozzles;a pressurizing-gas supply device configured to supply pressurizing gas to increase internal pressure of the hopper;a fluidization-gas supply device configured to supply fluidization gas to fluidize the pulverized fuel in the hopper; anda pulverized-fuel supply line provided to a vertically lower part of the hopper, whereinthe pressurizing-gas supply device supplies pressurizing gas to the plurality of first nozzles and the plurality of second nozzles, andthe fluidization-gas supply device supplies fluidization gas to the plurality of second nozzles.2. The pulverized-fuel supply unit according to claim 1 , wherein a flow rate of gas supplied by the fluidization-gas supply device is lower than a flow rate of gas supplied by the pressurizing-gas supply device.3. The pulverized-fuel supply unit according ...

Combined Hydrothermal Liquefaction and Catalytic Hydrothermal Gasification System and Process for Conversion of Biomass Feedstocks

A combined hydrothermal liquefaction (HTL) and catalytic hydrothermal gasification (CHG) system and process are described that convert various biomass-containing sources into separable bio-oils and aqueous effluents that contain residual organics. Bio-oils may be converted to useful bio-based fuels and other chemical feedstocks. Residual organics in HTL aqueous effluents may be gasified and converted into medium-BTU product gases and directly used for process heating or to provide energy. 115-. (canceled)16: A system for conversion of a biomass , the system comprising:a hydrothermal liquefaction (HTL) stage that hydrothermally liquefies the biomass in an aqueous medium at a temperature and pressure selected to form a conversion product comprising a separable bio-oil and an aqueous fraction containing residual organics therein; anda catalytic hydrothermal gasification (CHG) stage operatively coupled to the HTL stage configured to receive the aqueous fraction containing residual organics from the HTL stage at a selected temperature and pressure that forms a product gas containing at least one medium BTU product gas.17: The system of claim 16 , further including an upgrade stage configured to upgrade the bio-oil released from the HTL stage over a hydrogenation catalyst at a temperature up to about 450° C. and a hydrogen partial pressure up to about 150 atmospheres (1.52×104 kPa) that yields a green crude.18: The system of claim 16 , wherein the product gas when combusted generates sufficient energy such that the sum of the energy demands for conversion of the biomass feedstock to the product gas is a net positive.19: The system of claim 16 , further including one or more heat exchangers positioned to distribute heat to selected locations in the HTL stage and/or the CHG stage. This application claims priority from U.S. Provisional Patent Application No. 61/657,416 filed 8 Jun. 2012 entitled “Combined Hydrothermal Liquefaction and Catalytic Hydrothermal Gasification for ...

Integrated biorefinery for production of liquid fuels

A system including a mixing apparatus configured to produce a reformer feedstock and comprising one or more cylindrical vessel having a conical bottom section, an inlet for superheated steam within the conical bottom section and an inlet for at least one carbonaceous material at or near the top of the cylindrical vessel, wherein the one or more cylindrical vessel is a pressure vessel configured for operation at a pressure in the range of from about 5 psig (34.5 kPa) to about 50 psig (344.7 kPa); a reformer configured to produce, from the reformer feedstock, a reformer product comprising synthesis gas, and also producing a hot flue gas; a synthesis gas conversion apparatus configured to catalytically convert at least a portion of the synthesis gas in the reformer product into synthesis gas conversion product, and to separate, from the synthesis gas conversion product, a spent catalyst stream and a tailgas.

PROCESSING BIOMASS

Carbon-containing materials, such as biomass (e.g., plant biomass, animal biomass, and municipal waste biomass) or coal are processed to produce useful products, such as fuels, carboxylic acids and equivalents thereof (e.g., esters and salts). For example, systems are described that can use feedstock materials, such as cellulosic and/or lignocellulosic materials and/or starchy materials, to produce ethanol, butanol or organic acids (e.g., acetic or lactic acid), salts of organic acids or mixtures thereof. If desired, organic acids can be converted into alcohols, such as by first converting the acid, salt or mixtures of the acid and its salt to an ester, and then hydrogenating the formed ester. Acetogens or homoacetogens which are capable of utilizing a syngas from a thermochemical conversion of coal or biomass can be utilized to produce the desired product. 1. A method of processing biomass , the method comprising: treating biomass with radiation , thereby producing treated biomass; and converting a first portion of the treated biomass utilizing bacteria capable of metabolizing both sugar and syngas feedstocks , to produce the carboxylic acid ester , wherein during converting , syngas is delivered to the bacteria , wherein the syngas is produced by gasification of a second portion of the treated biomass.2. The method of wherein the radiation comprises gamma radiation claim 1 , microwave radiation claim 1 , infrared radiation claim 1 , electron beam radiation claim 1 , X-rays claim 1 , ultraviolet radiation claim 1 , ion particle beam radiation claim 1 , or a combination of any of the forgoing.3. The method of wherein the radiation comprises electron beam radiation.4. The method of wherein the electron beam radiation is delivered at a dose of at least 10 Mrad.5. The method of claim 1 , further comprising treating the biomass with shearing claim 1 , cutting claim 1 , grinding claim 1 , pulverizing claim 1 , chopping claim 1 , shredding claim 1 , sonication claim 1 , ...

Method Of Gasification Of Waste, In Particular Household Waste And The Apparatus For Performing Such A Method

A system and process for the gasification of waste, particularly household waste, in an apparatus comprising a gasification system for waste treatment and gasifier. 1. A process for the gasification of waste , particularly household waste , in an apparatus comprising a gasification system for waste treatment and gas generator , comprising the following successive steps:(a) start-up,(b) loading of waste into the waste processing,(c) processing waste, starting from step (c1) shredding the waste in a system for processing waste,(d) passing treated waste from the processing of waste to the gasifier,(e) producing synthesis gas in the gasifier,(f) producing electricity and/or heat from the synthesis gas,characterised in that (c2) drying the waste,', '(c3) granulation of the dried waste obtained from step (c2),', '(c4) compression of the granulate produced in step (c3)', 'wherein step (d) is passing compressed granules of step (c4) to step (e), the interval between steps (c1)-(c4) and step (e) may be any, and excess unused energy produced in step (f) is stored., 'step (c) comprises a sequence of steps'}2. Method according to claim 1 , characterised in that the waste disposed includes wood claim 1 , paper claim 1 , cardboard claim 1 , plastics claim 1 , organic matter claim 1 , in particular food.3. Method according to claim 1 , characterised in that after the execution of step (e) claim 1 , the transfer of the produced syngas for power generation plants and/or heat claim 1 , preferably a power generator and/or boiler.4. Method according to claim 1 , characterised in that after the performance of step (f) the device is switched off.5. Method according to claim 1 , characterised in that the residue from step (e) as a solid claim 1 , in particular ash claim 1 , and gaseous is discharged outside the system by a dedicated ventilation system.6. Method according to claim 1 , characterised in that the unused excess energy produced in step (f) is stored in at least one battery ...

INTEGRATED CHEMICAL LOOPING COMBUSTION SYSTEM AND METHOD FOR POWER GENERATION AND CARBON DIOXIDE CAPTURE

A chemical looping combustion (CLC) based power generation, particularly using liquid fuel, ensures substantially complete fuel combustion and provides electrical efficiency without exposing metal oxide based oxygen carrier to high temperature redox process. An integrated fuel gasification (reforming)-CLC-followed by power generation model is provided involving (i) a gasification island, (ii) CLC island, (iii) heat recovery unit, and (iv) power generation system. To improve electrical efficiency, a fraction of the gasified fuel may be directly fed, or bypass the CLC, to a combustor upstream of one or more gas turbines. This splitting approach ensures higher temperature (efficiency) in the gas turbine inlet. The inert mass ratio, air flow rate to the oxidation reactor, and pressure of the system may be tailored to affect the performance of the integrated CLC system and process. 1. An integrated system , comprising:a gasification subsystem comprising (a-i) a fuel heater suitable for heating a liquid fuel stream, (a-ii) a gasifier located downstream of, and fluidly connected to, the fuel heater, the gasifier being configured to gasify the liquid fuel stream with an oxygen-rich stream to form a syngas stream, and (a-iii) a gas splitter located downstream of, and fluidly connected to, the gasifier, the gas splitter being configured to split the syngas stream into a first syngas substream and a second syngas substream;{'sub': 2', '2, 'a chemical looping combustion (CLC) subsystem comprising (b-i) a reducer located downstream of, and fluidly connected to, the gas splitter, the reducer being configured to oxidize the first syngas substream in the presence of an oxygen carrier to form a CO/HO stream, the oxygen carrier being reduced to a reduced oxygen carrier, and (b-ii) an oxidizer located downstream of, and fluidly connected to, the first solid-gas separator, the oxidizer being configured to oxidize the reduced oxygen carrier in the presence of an oxygen-containing stream ...

Apparatus and method for syngas bio-methanation

A waste treatment, pyrolysis and gasification and concerns an apparatus for syngas bio-methanation include a unit for pyrolysis/gasification receiving organic material, the unit for pyrolysis/gasification generating syngas, comprising at least one membrane reactor inside a liquid bath comprising at least one bacteria population, the membrane reactor comprising at least one hollow fiber in contact with the liquid bath, around which a biofilm is formed and into which the syngas from the unit for pyrolysis/gasification flows, so as to convert the syngas into methane. A method for bio-methanation of syngas comprising a step of providing syngas from a unit for pyrolysis/gasification to a membrane reactor inside a liquid bath comprising at least one suitable bacteria population, the membrane reactor comprising at least one hollow fiber in contact with the liquid bath, around which a biofilm is formed and into which the output syngas of the unit for pyrolysis flows, so as to convert the syngas into methane.

CLOSED-LOOP SYSTEM FOR GROWTH OF AQUATIC BIOMASS AND GASIFICATION THEREOF

Processes, systems, and methods for producing combustible gas from wet biomass are provided. In one aspect, for example, a process for generating a combustible gas from a wet biomass in a closed system is provided. Such a process may include growing a wet biomass in a growth chamber, moving at least a portion of the wet biomass to a reactor, heating the portion of the wet biomass under high pressure in the reactor to gasify the wet biomass into a total gas component, separating the gasified component into a liquid component, a non-combustible gas component, and a combustible gas component, and introducing the liquid component and non-combustible gas component containing carbon dioxide into the growth chamber to stimulate new wet biomass growth. 1. A process for generating a combustible gas from a wet biomass in a closed system , comprising:growing a wet biomass in a growth chamber;moving at least a portion of the wet biomass to a reactor;heating the portion of the wet biomass under pressure with a catalyst in the reactor to gasify the wet biomass into a gasified component;separating the gasified component into a condensed liquid, a non-combustible gas component, and a combustible gas component; andintroducing the non-combustible gas component containing carbon dioxide and the liquid component into the growth chamber to stimulate wet biomass growth.2. The process of claim 1 , wherein the combustible gas component includes methane.3. The process of claim 1 , wherein the combustible gas component includes hydrogen.4. The process of claim 1 , wherein the gasified component is removed from the reactor prior to isolating the combustible gas component.5. The process of claim 1 , further comprising introducing a nutrient recaptured from the harvested biomass into the growth chamber to stimulate new biomass growth.6. The process of claim 5 , wherein the nutrient is recaptured from the gasified component.7. The process of claim 5 , wherein the nutrient is recaptured during a ...

Supercritical Water Gasification Process

The process described herein converts biomass directly into a combination of hydrogen, methane and carbon dioxide. A portion of the gases are collected at pressures above the thermodynamic critical pressure for water, which is 3200 psi (pounds per square inch). Typical operating pressure at the point where the first portion of gas collected can range from 3200 psi to 6000 psi. Upon cooling, most of the COcondenses to a liquid. At this density and pressure, the COcan be injected into a deep well aquifer to sequester the carbon dioxide. The overall process is superior to carbon neutral processes, can be carbon negative, and possesses the potential to reverse atmospheric COtrends if implemented on a global scale. 1. A process for converting a biomass stream into a product stream comprising hydrogen , methane , and carbon dioxide using a supercritical water gasification reactor , the process comprising:(i) exchanging heat, using a first heat exchanger, between a feedwater stream and the product stream, wherein the feedwater stream is heated by the product stream to a first temperature;(ii) feeding the feedwater stream exiting the first heat exchanger to a heater that is configured to heat the feedwater stream from the first temperature to a second temperature;(iii) exchanging heat, using a second heat exchanger, between the product stream and the feedwater stream exiting the heater, wherein the feedwater stream is heated by the product from the second temperature to a third temperature;(iv) feeding the feedwater stream exiting the second heat exchanger to the heater, wherein the heater is configured to heat the feedwater stream from the third temperature to a fourth temperature; and(v) reacting the feedwater stream provided by the heater with the biomass stream in the supercritical water gasification reactor to produce the product stream.2. The process of wherein step (i) further includes utilizing an additional heat exchanger to exchange heat between the product stream ...

METHOD AND SYSTEM FOR COGENERATING GAS-STEAM BASED ON GASIFICATION AND METHANATION OF BIOMASS

A system for cogenerating gas-steam based on gasification and methanation of biomass, the system including a gasification unit, a shift unit, a purification unit, a methanation unit, and a methane concentration unit. A waste heat boiler is provided in an upper part of a gasifier of the gasification unit. The methanation unit includes a first primary methanation reactor, a second primary methanation reactor, a first secondary methanation reactor, and a second secondary methanation reactor connected in series. An outlet of the second primary methanation reactor is provided with two bypasses, one of which is connected to an inlet of the first primary methanation reactor, the other of which is connected to the first secondary methanation reactor. The second secondary methanation reactor is connected to the methane concentration unit. 2. The system of claim 1 , whereinthe methanation unit comprises a primary methanation unit and a secondary methanation unit;the primary methanation unit comprises a first primary methanation reactor comprising a first outlet and an inlet and a second primary methanation reactor comprising a second outlet, and the first primary methanation reactor and the second primary methanation reactor are connected in series;the secondary methanation unit comprises a first secondary methanation reactor and a second secondary methanation reactor connected in series;the second outlet is provided with two bypasses: one of the two bypasses is connected to the inlet of the first primary methanation reactor to yield a first mixed gas; the other of the two bypasses is connected to the secondary methanation unit to yield a second mixed gas; andthe second secondary methanation reactor is connected to the methane concentration unit.3. The system of claim 2 , further comprising a first waste heat boiler claim 2 , a first steam superheater claim 2 , a second waste heat boiler claim 2 , and a second steam superheater claim 2 , whereinthe first waste heat boiler and ...

PROCESSING BIOMASS

Carbon-containing materials, such as biomass (e.g., plant biomass, animal biomass, and municipal waste biomass) or coal are processed to produce useful products, such as fuels, carboxylic acids and equivalents thereof (e.g., esters and salts). For example, systems are described that can use feedstock materials, such as cellulosic and/or lignocellulosic materials and/or starchy materials, to produce ethanol, butanol or organic acids (e.g., acetic or lactic acid), salts of organic acids or mixtures thereof. If desired, organic acids can be converted into alcohols, such as by first converting the acid, salt or mixtures of the acid and its salt to an ester, and then hydrogenating the formed ester. Acetogens or homoacetogens which are capable of utilizing a syngas from a thermochemical conversion of coal or biomass can be utilized to produce the desired product. 1. A method of processing lignocellulosic biomass to lignin and to a carboxylic acid ester , the method comprising:treating the lignocellulosic biomass to reduce its recalcitrance, producing treated biomass;hydrolyzing the treated biomass to produce sugars;capturing lignin liberated by saccharifying the treated biomass;contacting the sugars with a microorganism or a mixture of microorganisms to produce the carboxylic acid ester.2. The method of claim 1 , wherein treating the lignocellulosic biomass comprises shearing claim 1 , irradiation claim 1 , sonication claim 1 , pyrolysis claim 1 , oxidation claim 1 , steam explosion claim 1 , treating with ozone claim 1 , treating with Fenton's solution claim 1 , or a combination of any of these.3. The method of wherein treating the lignocellulosic biomass is by radiation.4. The method of wherein the radiation is by a beam of electrons.5. The method of wherein the beam of electrons delivers at least 10 Mrad of radiation.6. The method of wherein the lignocellulosic biomass comprises paper claim 1 , paper products claim 1 , wood claim 1 , wood-related materials claim 1 , ...

All-Steam Gasification for Supercritical CO2 Cycle System

A carbonaceous fuel gasification system for a supercritical COpower cycle system includes a micronized char preparation system comprising a devolatilizer that receives solid carbonaceous fuel, hydrogen, oxygen, and fluidizing steam and produces micronized char, steam, hydrogen, and volatiles. An indirect gasifier includes a vessel comprising a gasification chamber that receives the micronized char, a conveying gas, and steam where the gasification chamber provides syngas, ash, and steam. A combustion chamber receives syngas and an oxidant and burns the mixture of syngas with the oxidant to provide heat for gasification and for heating incoming flows, thereby generating steam and CO. The heat for gasification is transferred from the combustion chamber to the gasification chamber by circulating refractory sand. A syngas cooler cools the syngas and generates steam and provides to a supercritical COpower cycle system that performs a supercritical COpower cycle for generating power. 1. A carbonaceous fuel gasification system for a supercritical COpower cycle system comprising:a) a micronized char preparation system comprising a devolatilizer, the micronized char preparation system being configured to receive solid carbonaceous fuel, hydrogen, oxygen, and fluidizing steam and to produce micronized char, steam, hydrogen, and volatiles at one or more outlets; i) a vessel comprising a gasification chamber, the vessel being configured to receive the micronized char from the one or more outlets of the micronized char preparation system, a conveying gas, and steam, the gasification chamber providing syngas, ash, and steam at one or more outlets; and', {'sub': '2', 'ii) a combustion chamber being configured to receive syngas and an oxidant and to burn the mixture of syngas with the oxidant to provide heat for gasification and for heating incoming flows, thereby generating steam and CO, the combustion chamber being further configured to transfer heat for gasification from the ...

METHOD FOR CONVERTING BIOMASS TO METHANE

A method for enhancing the treatment of lignocellulose-containing materials by biotreatment wherein such lignocellulose-containing materials, normally resistant to biotreatment, are first subjected to a low-temperature, long-residence time pyrolysis at about 175° C. to about 325° C. for about 0.1 hour to about 2.0 hours, wherein a substantial portion of the incoming material is distilled into water-soluble compounds amenable to anaerobic biotreatment. Exemplary applications of the method include pyrolytic pre-treatment of wastewater sludges, cellulosic wastes, wood, peat, plant residues, low-grade coal, and the like to enhance methane gas production in anaerobic digestion and/or oxygen-limited or oxygen-starved fermentation to produce ethanol. 1. A system comprising ,a pyrolizer having an inlet and an outlet,a condenser having an inlet, a non-condensable gas outlet and a liquid outlet, andan anaerobic digester having one or more inlets,wherein the outlet of the pyrolizer is connected to the inlet of the condenser, and the non-condensable gas outlet or the condenser is connected to an inlet of the anaerobic digester.2. The system of further comprising a phase separator having an inlet claim 1 , an aqueous phase outlet and an organic phase outlet claim 1 , wherein the phase separator inlet is connected to the liquid outlet of the condenser and the aqueous phase outlet of the phase separator is connected to an inlet of the anaerobic digester.3. The system of wherein the pyrolizer comprises an internal screw.4. A process comprising the steps of claim 1 ,subjecting one or more biomaterials to pyrolysis to produce pyrolysis products including at least a pyrogas and char, andmixing the pyrogas into a sludge in an anaerobic digester.5. The process of wherein the one or more biomaterials comprise anaerobic digester sludge and undigested lignocellulosic material.6. The process of wherein the one or more biomaterials comprise municipal solid waste.7. The process of wherein the ...

SYSTEMS AND METHODS FOR PRODUCING SYNGAS FROM A SOLID CARBON-CONTAINING SUBSTANCE USING A REACTOR HAVING HOLLOW ENGINEERED PARTICLES

A solids circulation system receives a gas stream containing char or other reacting solids from a first reactor. The solids circulation system includes a cyclone configured to receive the gas stream from the first reactor, a dipleg from the cyclone to a second reactor, and a riser from the second reactor which merges with the gas stream received by the cyclone. The second reactor has a dense fluid bed and converts the received materials to gaseous products. A conveying fluid transports a portion of the bed media from the second reactor through the riser to mix with the gas stream prior to cyclone entry. The bed media helps manipulate the solids that is received by the cyclone to facilitate flow of solids down the dipleg into the second reactor. The second reactor provides additional residence time, mixing and gas-solid contact for efficient conversion of char or reacting solids. 1100. A reactor () for producing carbon monoxide , carbon dioxide , and hydrogen from a solid carbon-containing substance , comprising:(a) a fluidized bed comprising bed material in the form of hollow engineered particles selected from the group consisting of alumina, zirconia, sand, olivine sand, limestone, dolomite and metal catalyst;{'b': '160', '(b) a freeboard () located above a bed level of the fluidized bed;'}{'b': 700', '160', '100', '700, '(c) a cyclone () positioned within the freeboard () of the reactor (), the cyclone () configured to capture and recycle entrained bed material and char particles to the fluidized bed;'}{'b': 160', '160, 'sub': 2', '2, '(d) a plurality of fluid addition stages located in the freeboard (), the plurality of fluid addition stages configured to introduce a mixture of oxygen and superheated steam to the freeboard () to promote conversion of char into CO, CO, and H;'}{'b': 140', '130, '(e) a distributor () configured to accept and distribute a fluidization media () comprising oxygen and superheated steam into the bed material of the fluidized bed;'}{'b': ...

Solids Circulation System and Method For Capture and Conversion of Reactive Solids

A solids circulation system receives a gas stream containing char or other reacting solids from a first reactor. The solids circulation system includes a cyclone configured to receive the gas stream from the first reactor, a dipleg from the cyclone to a second reactor, and a riser from the second reactor which merges with the gas stream received by the cyclone. The second reactor has a dense fluid bed and converts the received materials to gaseous products. A conveying fluid transports a portion of the bed media from the second reactor through the riser to mix with the gas stream prior to cyclone entry. The bed media helps manipulate the solids that is received by the cyclone to facilitate flow of solids down the dipleg into the second reactor. The second reactor provides additional residence time, mixing and gas-solid contact for efficient conversion of char or reacting solids.

RENEWABLE ELECTRICITY CONVERSION OF LIQUID FUELS FROM HYDROCARBON FEEDSTOCKS

The present invention includes a method for converting renewable energy source electricity and a hydrocarbon feedstock into a liquid fuel by providing a source of renewable electrical energy in communication with a synthesis gas generation unit and an air separation unit. Oxygen from the air separation unit and a hydrocarbon feedstock is provided to the synthesis gas generation unit, thereby causing partial oxidation reactions in the synthesis gas generation unit in a process that converts the hydrocarbon feedstock into synthesis gas. The synthesis gas is then converted into a liquid fuel. 120.-. (canceled)21. A method for producing a liquid fuel , the method comprising:generating oxygen and hydrogen using an electrolysis unit wherein at least some of electricity for the electrolysis unit is provided by from a renewable energy source;supplying at least some of the oxygen generated by the electrolysis unit to a synthesis gas generation unit that converts a hydrocarbon feedstock to synthesis gas wherein the oxygen is either directly supplied to the synthesis gas generation unit or is supplied to a storage unit that stores the oxygen and later supplies the oxygen to the synthesis gas generation unit;producing a hydrogen and carbon monoxide mixture in the synthesis gas generation unit using at least one of steam reformation or partial oxidation of a hydrocarbon feedstock;supplying at least some of the hydrogen generated by the electrolysis unit so as to provide additional hydrogen in the hydrogen and carbon monoxide mixture; andconverting the hydrogen and carbon monoxide mixture into a liquid fuel.22. The method of wherein the hydrogen from electrolysis is used to increase a hydrogen to carbon monoxide ratio of the hydrogen and carbon monoxide mixture for liquid fuel production to a selected ratio.23. The method of where the selected ratio is two.24. The method of wherein the hydrogen that is produced by the electrolysis unit is reacted with COthat is produced in the ...

BIOMASS GASIFICATION POWER GENERATION SYSTEM AND POWER GENERATION METHOD

A biomass gasification power generation system including: a gas generation device that generates a combustible gas from a biomass and a gasification agent; an internal combustion engine that generates motive power from a fuel gas containing the combustible gas generated by the gas generation device; and a generator that generates electric power from the motive power generated by the internal combustion engine. The power generation system is additionally provided with a water electrolysis device that generates oxygen and hydrogen through the electrolysis of water. The gasification agent contains oxygen generated by the water electrolysis device, and the fuel gas contains hydrogen generated by the water electrolysis device. The oxygen concentration in the gasification agent is from 22 vol. % to 40 vol. %. 1. A biomass gasification power generation system comprising: a gas generation device that generates a combustible gas from a biomass and a gasification agent; an internal combustion engine that generates motive power from a fuel gas containing the combustible gas generated by the gas generation device; and a generator that generates electric power from the motive power generated by the internal combustion engine , whereinthe power generation system further comprises a water electrolysis device that generates oxygen and hydrogen through the electrolysis of water, the gasification agent comprises oxygen produced by the water electrolysis device, and the fuel gas comprises hydrogen produced by the water electrolysis device; andan oxygen concentration in the gasification agent is from 22 vol. % to 40 vol. %.2. The biomass gasification power generation system according to claim 1 , further comprising: an oxygen supply device that supplies oxygen generated by the water electrolysis device to the gas generation device; and a hydrogen supply device that supplies hydrogen generated by the water electrolysis device to the internal combustion engine.3. The biomass gasification ...

All-Steam Gasification for Supercritical CO2 Power Cycle System

A carbonaceous fuel gasification system for a supercritical COpower cycle system includes a micronized char preparation system comprising a devolatilizer that receives solid carbonaceous fuel, hydrogen, oxygen, and fluidizing steam and produces micronized char, steam, hydrogen, and volatiles. An indirect gasifier includes a vessel comprising a gasification chamber that receives the micronized char, a conveying gas, and steam where the gasification chamber provides syngas, ash, and steam. A combustion chamber receives syngas and an oxidant and burns the mixture of syngas with the oxidant to provide heat for gasification and for heating incoming flows, thereby generating steam and CO. The heat for gasification is transferred from the combustion chamber to the gasification chamber by circulating refractory sand. A syngas cooler cools the syngas and generates steam and provides to a supercritical COpower cycle system that performs a supercritical COpower cycle for generating power. 1. A carbonaceous fuel gasification system for a supercritical COpower cycle system comprising:a) a micronized char preparation system comprising a devolatilizer, the micronized char preparation system being configured to receive solid carbonaceous fuel, hydrogen, oxygen, and fluidizing steam and to produce micronized char, steam, hydrogen, and volatiles at one or more outlets; i. a vessel comprising a gasification chamber, the vessel being configured to receive the micronized char from the one or more outlets of the micronized char preparation system, a conveying gas, and steam, the gasification chamber providing syngas, ash, and steam at one or more outlets; and', {'sub': '2', 'ii. a combustion chamber being configured to receive syngas and an oxidant and to burn the mixture of syngas with the oxidant to provide heat for gasification and for heating incoming flows, thereby generating steam and CO, the combustion chamber being further configured to transfer heat for gasification from the ...

SYSTEM AND METHOD FOR PRODUCING LOW NOx AIR EMISSIONS FROM GASIFICATION POWER PLANTS

An apparatus is provided that receives waste and generates electrical power or thermal energy with minimal NOx emissions. A gasifier is provided that receives the waste and air to produce fuel gas for delivery to a fluidly coupled reformer. The reformer receives the fuel gas, recycled flue gas, and air to auto-thermally produce a reformed fuel gas and destroy fuel gas pollutants at a first temperature without a catalyst. A burner is fluidly coupled to the reformer and receives recycled flue gas and air to oxidize the reformed fuel gas at a second temperature that prevents nitrogen oxide formation, the second temperature being lower than the first temperature. A quench chamber is fluidly coupled to the burner and receives flue gas from the burner for quenching with recycled flue gas. A heat recovery system is fluidly coupled to the reformer, burner, and quench chamber to extract usable energy. 1. An apparatus that receives waste and generates energy by producing steam from the waste , the apparatus minimizing air pollutants by thermally processing the waste to produce a carbon free residual mineral , the apparatus comprising:a gasifier that receives the waste and air to produce a fuel gas;a reformer fluidly coupled to the gasifier, the reformer receives the fuel gas, a first stream of recycled flue gas, and a first stream of air to auto-thermally produce a reformed fuel gas and destroy pollutants in the fuel gas at a first temperature;a burner fluidly coupled to the reformer, the burner receives a second stream of recycled flue gas and a second stream of air to oxidize the reformed fuel gas at a second temperature that prevents formation of nitrogen oxide, the second temperature being lower than the first temperature;a quench chamber fluidly coupled to the burner, the quench chamber receives flue gas from the burner that is quenched with a third stream of recycled flue gas; anda heat recovery system fluidly coupled to the reformer, the burner, and the quench chamber ...

Environmentally-friendly integrated installation for producing chemical and petrochemical products

An environmentally-friendly integrated installation includes a combined air separation and carbon dioxide capture installation and an electrolysis unit. In certain embodiments, the integrated installation additionally includes a unit for producing renewable energy. A control unit and a computer program product are provided for the integrated installation. A method for producing chemical products in the integrated installation, and the use of the integrated installation to produce chemical products are disclosed and use as a chemical store for fluctuating renewable energies is disclosed.

ENTRAINED FLOW GASIFIER HAVING AN INTEGRATED INTERMEDIATE TEMPERATURE PLASMA

A process for gasifying solid or liquid gasification materials, in particular biomass, at pressures in the range from atmospheric pressure to 10 MPa and at gasification temperatures in the range from 800° C. to 1500° C. to form a highly calorific synthesis gas. An endothermic steam gasification process proceeds in a gasification space of an entrained flow gasifier, and a plasma of intermediate temperature (typically <3500° C., preferably <2000° C.) introduces heat of reaction into the gasification space in such a quantity that the gasification temperature is kept below the ash softening temperature of 1500° C. Endothermic reactions, in particular reactions having a high activation energy, proceed at high rates at far lower gas temperatures than in the case of a thermal process. The gasification process, which does not require an oxygen plant, gives a crude gas which is free of hydrocarbons. 1. A process for gasifying solid or liquid gasification materials at pressures in the range from atmospheric pressure to 10 MPa and at gasification temperatures in the range from 800° C. to 1500° C. to form a synthesis gas , comprising:performing an endothermic steam gasification process according to an entrained flow principle using a plasma of intermediate temperature, <3500° C.; andintroducing required heat of reaction at least partly by means of the plasma.2. The process as claimed in claim 1 , further comprising all of the introducing of the required heat of reaction is by means of the plasma.3. The process as claimed in claim 1 , further comprising generating the plasma of intermediate temperature by means of a DC discharge.4. The process as claimed in claim 1 , further comprising generating the plasma of intermediate temperature by means of a low-frequency AC discharge.5. The process as claimed in claim 1 , further comprising generating the plasma of intermediate temperature by means of electromagnetic waves.6. The process as claimed in claim 1 , further comprising: ...

DEVICE AND METHOD FOR PRODUCING SUBSTITUTE NATURAL GAS AND NETWORK COMPRISING SAME

A device includes a gasifier to produce a gaseous compound from a biomass. The gasifier includes inlets for the biomass and for an oxidizing agent and an outlet for the gaseous compound including carbon monoxide. A first methanation unit to methanate the carbon monoxide to produce a substitute natural gas exiting the gasifier. The first methanation unit includes at least one inlet for water and an inlet for the gaseous compound coming from the gasifier. A second methanation unit to methanate the carbon dioxide to produce the substitute natural gas. The second methanation unit includes at least one inlet for water and one inlet for the carbon dioxide from the first methanation unit. A dihydrogen producing unit to produce dihydrogen from water and electric current. The dihydrogen producing unit includes an electrical power supply, an inlet for water and an outlet for dihydrogen supplying the second methanation unit. 123-. (canceled)24. Integrated device for producing a substitute natural gas , comprising: an inlet for the biomass;', 'an inlet for an oxidizing agent; and', 'an outlet for the gaseous compound comprising carbon monoxide;, 'a gasifier configured to produce a gaseous compound from a biomass, comprisinga carbon monoxide methanation unit to methanate the carbon monoxide to produce substitute natural gas from the gaseous compound output from the gasifier, the first methanation unit comprises at least one inlet for water and an inlet for the gaseous compound coming from the gasifier;a carbon dioxide methanation unit to produce substitute natural gas comprising at least one inlet for the water and an inlet for the carbon dioxide coming from the carbon monoxide methanation unit; an electrical power supply;', 'an inlet for the water; and', 'an outlet for dihydrogen supplying the carbon dioxide methanation unit., 'an electrolysis unit to produce from the water and an electric current, comprising25. The Integrated device according to claim 24 , further comprising a ...

FUEL PRODUCTION SYSTEM

A fuel production system includes a gasification unit including a gasification furnace that gasifies biomass feedstock to produce a syngas; a liquid fuel production unit that produces a liquid fuel from the syngas produced by the gasification unit; an electrolysis unit that produces hydrogen from water using electric power generated using renewable energy; a hydrogen tank that stores the hydrogen produced by the electrolysis unit; a remaining hydrogen amount determining section that determines the amount of hydrogen remaining in the hydrogen tank; a hydrogen supply unit that supplies the hydrogen from the hydrogen tank to the gasification unit; and a control unit that performs a hydrogen consumption increasing control to reduce the H/CO ratio of the syngas produced by reaction in the gasification furnace and to increase the amount of hydrogen supplied by the hydrogen supply unit, when the remaining amount of hydrogen is more than a predetermined amount. 1. A fuel production system for producing a liquid fuel from biomass feedstock , comprising:a gasification unit comprising a gasification furnace that gasifies biomass feedstock to produce a syngas comprising hydrogen and carbon monoxide;a liquid fuel production unit that produces a liquid fuel from the syngas produced by the gasification unit;an electrolysis unit that produces hydrogen from water using electric power generated using renewable energy;a hydrogen tank that stores the hydrogen produced by the electrolysis unit;a remaining hydrogen amount determining section that determines an amount of hydrogen remaining in the hydrogen tank;a hydrogen supply unit that supplies the hydrogen from the hydrogen tank to the gasification unit; and{'sub': '2', 'a control unit that performs a hydrogen consumption increasing control to reduce a H/CO ratio of the syngas produced by reaction in the gasification furnace and to increase an amount of hydrogen supplied by the hydrogen supply unit, when the remaining amount of ...

RENEWABLE ELECTRICITY CONVERSION OF LIQUID FUELS FROM HYDROCARBON FEEDSTOCKS

The present invention includes a method for converting renewable energy source electricity and a hydrocarbon feedstock into a liquid fuel by providing a source of renewable electrical energy in communication with a synthesis gas generation unit and an air separation unit. Oxygen from the air separation unit and a hydrocarbon feedstock is provided to the synthesis gas generation unit, thereby causing partial oxidation reactions in the synthesis gas generation unit in a process that converts the hydrocarbon feedstock into synthesis gas. The synthesis gas is then converted into a liquid fuel. 1generating oxygen in an oxygen separation unit utilizing electricity from wind or solar power;supplying the oxygen from the oxygen separation unit to a synthesis gas generation unit;supplying steam to the synthesis gas generation unit;producing synthesis gas in the synthesis gas generation unit using a combination of steam reformation and partial oxidation of a hydrocarbon feedstock in the synthesis gas generation unit; andconverting the synthesis gas into a fuel.. A method, comprising: This application is a continuation of U.S. patent application Ser. No. 15/267,021 filed Sep. 15, 2016, which is a continuation of U.S. patent application Ser. No. 14/077,094 filed Nov. 11, 2013, issued as U.S. Pat. No. 9,469,533 on Oct. 18, 2016 which is a continuation of U.S. patent application Ser. No. 12/575,305, filed on Oct. 7, 2009, issued as U.S. Pat. No. 8,614,364 on Dec. 24, 2013 which is a continuation-in-part of U.S. patent application Ser. No. 11/177,152, filed Jul. 6, 2005, now abandoned, which further claims priority to U.S. Provisional Application No. 61/103,397, filed Oct. 7, 2008, and U.S. Provisional Application No. 61/107,563, filed Oct. 22, 2008. These patents and applications are incorporated herein by this reference in their entirety and for any purpose.This invention relates to a system for optimal use of variable electricity from a renewable energy source, such as from wind ...

APPARATUS FOR ENDOTHERMIC REACTIONS

A carbonaceous feed pyrolysis apparatus is provided including two or more hot particle fluidised beds, one of which contains a combustion zone, and one or more positive displacement apparatus for the transfer of hot particles beds. Also provided is a bio-oil production process including two or more fluidised beds, a first combustion zone carried out in one or more combustion fluidised beds in which a particulate material is fluidised and heated, and a second pyrolysis zone carried out in one or more pyrolysis fluidised beds in which hot particles heated in the combustion zone are used for pyrolysis of bio-mass, the combustion zone being operated at or about atmospheric pressure at a temperature of from 400° C. to 1100° C., and the pyrolysis zone being operated at a pressure of from atmospheric to 100 Barg at a temperature of from 400° C. to 900° C. 120-. (canceled)30. An endothermic reaction process , comprising: two or more fluidized bed zones comprising a first fluidized bed zone and a second fluidized bed zone;', 'a second fluidized bed zone gas feed comprising a closed gas loop configured such that, in use, a portion of a gas produced in the second fluidized bed zone is recycled in the closed gas loop to the first fluidized bed zone, such that the recycled gas is used as a gaseous fuel for the first fluidized bed zone, either fully or in part;', 'an apertured divider having one or more apertures therethrough connecting at least two of the fluidized bed zones;', 'a mass transfer device for transferring particulate matter from at least one fluidized bed zone to an other fluidized bed zone;', 'a gas loop purge configured such that, in use, a part of the recycled gas stream from the second fluidized bed zone is purged from the closed gas loop; and', 'a flow rate regulator configured to, in use, regulate a flow rate to a predeterminable rate;, 'providing an endothermic reaction apparatus, comprisingcombusting a carbonaceous material in a presence of oxygen in a hot ...

ECOLOGICAL SEQUESTRATION OF CARBON DIOXIDE/INCREASE OF BIO-ENERGY OBTAINABLE THROUGH BIOMASS

According to known methods, biomass is broken down under the action of water vapour via a carbon monoxide-hydrogen mixture (called synthesis gas) as an intermediate stage into hydrogen and carbon dioxide instead of being combusted directly to generate energy. Carbon dioxide is stored/sequestered and the hydrogen is used to generate energy. The transfer of bio-activity can also be effected within the same process by breaking down a mixture of biomass and fossil fuel (e.g. wood and coal) into carbon dioxide and hydrogen. The hydrogen is then reacted with half of the formed carbon dioxide to form methane and the remaining carbon dioxide is stored. The stored carbon dioxide and generated methane respectively comprise one half each of biological and fossil carbon. If the bio-activity of the stored biocarbon dioxide is transferred to the fossil carbon in methane, a corresponding mixture of wood and coal produces 100% biomethane. Here, too, up to 100% biomethane can be obtained from coal-wood mixtures. By adding the hydrogen obtained from excess electrical energy to the biocarbon, the bio-energy based on the biomass used is even quadrupled. For a traceable eco-balance with such mixtures, it is important to quantify the bio-proportion in the two “end products” stored carbon dioxide and generated methane. For this purpose, use is made e.g. of the radiocarbon (C14) method. 1. A process for transporting and steadying or storing renewable energy , the process comprising:converting biomass to bio carbon dioxide and bio hydrogen;reacting the bio hydrogen with synthesis gas obtained from biomass to form bio methane;supplying the bio methane into a network of natural gas; andtransporting or storing and consuming the bio methane together with the natural gas.2. The process according to claim 1 , wherein the bio carbon dioxide is stored and reacted with hydrogen claim 1 , made from electric power by water-electrolysis claim 1 , to form methane claim 1 , and the methane is supplied to ...

Method and apparatus for gasification

A gasification system includes a gasifier configured to gasify a feedstock and an oxidant to generate a producer gas, a steam generator configured to supply steam to the gasifier, and a combustion system configured to supply an exhaust gas to the steam generator to produce the steam. The system also includes an exhaust gas injection system located upstream of the gasifier and fluidly coupled to the gasifier. The exhaust gas injection system is configured to supply a portion of the exhaust gas from the combustion system to the gasifier.

WTE-PROCESSES AND RENEWABLE ENERGY OPTIMIZATION SYSTEM

The present disclosure encompasses systems, machinery, and processes for handling municipal, solid waste mixtures through which this material is recycled into renewable energy. The system comprises three processes: a waste handling process, a recycling and transforming process that converts the waste into fuel, and an energy renewal process. The waste handling process includes collection, sorting, an sizing of the mixed waste; the recycling and transforming process converts collected material into RDF (refuse derived fuel) pellets, and the energy renewal process comprises decomposition of mixture rich in organic matter using biogas/anaerobic technology to collect methane gas and biogas residues, and gasification of the solid RDF pellets, converting them into renewable energy and synthetic carbon. 1. A system for processing waste mixtures comprising:(a) a waste handling process;(b) a recycling and transforming waste-into-fuels process to transform waste into fuel; and(c) an energy renewal process;wherein stages (a), (b), and (c) are carried out in a continuously flowing process;whereby at least a portion of the waste mixture is recycled and at least a portion of the waste mixture is transformed into renewable energy; andwherein said mixtures are homogeneous or heterogeneous unclassified waste mixtures.2. The process of claim 1 , wherein the waste handling process (step (a)) comprises:(a) waste collection;(b) preliminary cut large size of waste into appropriate size for further processing;(c) cut-tear-and-beating the preliminary cut waste of step (b) into smaller pieces, and spreading the small pieces evenly on a conveyor;(d) removal of metal materials from waste;(e) removal of inorganic, nonflammable materials from the waste;(f) cutting waste a second time with a two-axis cutting device; and(g) collecting small and evenly desired size of waste.3. The process of claim 2 , wherein In the cut-tear-beat process (step (c)) comprises cutting claim 2 , tearing and breaking ...

Device for Processing Scrap Rubber

A device for processing scrap rubber has a reactor with a screw conveyor disposed inside a heating chamber, a thermal decomposition unit, burners, a condenser, a cyclone filter, and devices for discharging solid residue and removing a gas-vapor mixture. The reactor has two sections connected in parallel. The thermal decomposition unit has screw conveyors in each section, the conveyors have axial heating pipes with a coil. Along the length of the conveyors plates are arranged at the corners of an equilateral triangle in contact with and perpendicular to the side surface of the heating tube. A cylinder furnace with an evaporator and a burner is connected to the ends of the pipes. An outlet of the condenser is connected to a liquid fraction separator, inlets of the coils are connected to an outlet of the evaporator, and an inlet of the evaporator is connected to an outlet from the separator.

PROCESS

A process for the manufacture of one or more useful products comprises: gasifying a carbonaceous feedstock comprising waste materials and/or biomass in a gasification zone to generate a raw synthesis gas; supplying at least a portion of the raw synthesis gas to a clean-up zone to remove contaminants and provide a clean synthesis gas; supplying the clean synthesis gas to a first further reaction train to generate at least one first useful product and a tailgas; and diverting selectively on demand a portion of at least one of the carbonaceous feedstock, the clean synthesis gas, the tailgas and the light gas fraction to heat or power generation within the process, in response to external factors to control the carbon intensity of the overall process and enable GHG emission savings. 1. A process for the manufacture of one or more useful products comprising:a. gasifying a carbonaceous feedstock comprising waste materials and/or biomass in a gasification zone to generate a raw synthesis gas;b. supplying at least a portion of the raw synthesis gas to a clean-up zone to remove contaminants and provide a clean synthesis gas;c. importing natural gas and/or power into the process;d. supplying the clean synthesis gas to a first further reaction train to generate at least one first useful product and a tailgas; ande. diverting selectively on demand a portion of at least one of the carbonaceous feedstock, the clean synthesis gas, the tailgas and (if present) a light gas fraction to heat or power generation within the process to control the carbon intensity of the process.2. The process according to wherein means within the process are provided selectively on demand to divert one or more of:i. a portion of the carbonaceous feedstock to a combustor to generate energy for the production of steam for use on plant or for power generation; and/orii. a portion of the clean synthesis gas as fuel gas for use on plant and/or or for the generation of steam for use on plant and/or for power ...

SYSTEM AND METHOD FOR REDUCING NOx EMISSIONS FROM GASIFICATION POWER PLANTS

A method is provided for thermally processing waste to produce steam and generate energy while minimizing air pollutants in a staged thermal reactor. The method includes gasifying the waste to convert the waste to a fuel gas and a substantially carbon free, inert, granulated, sintered mineral ash and reforming the fuel gas auto-thermally to minimize creation of nitrogen oxide when the fuel gas is combusted. The method further includes burning the reformed fuel gas to minimize creation of nitrogen oxide in a flame region of a fuel gas burner and recirculating cooled flue gas to control oxygen content and temperature during the reforming operation and the burning operation. In one example, reforming the fuel gas converts non-molecular nitrogen species into molecular nitrogen in an auto-thermal non-catalytic reformer unit by decomposition reactions promoted by a prevailing reducing gas atmosphere.

Method and Apparatus for Reducing CO2 in a Stream by Conversion to a Syngas for Production of Energy

A system and method for producing Syngas from the COin a gaseous stream, such as an exhaust stream, from a power plant or industrial plant, like a cement kiln, is disclosed. A preferred embodiment includes providing the gaseous stream to pyrolysis reactor along with a carbon source such as coke. The COand carbon are heated to about 1330° C. and at about one atmosphere with reactants such as steam such that a reaction takes place that produces Syngas, carbon dioxide (CO) and hydrogen (H). The Syngas is then cleaned and provided to a Fischer-Tropsch synthesis reactor to produce Ethanol or Bio-catalytic synthesis reactor. 1. An apparatus for producing syngas that reduces an amount of carbon dioxide in a gaseous stream , the apparatus comprising:{'sub': 2', '2, 'a reaction chamber, said reaction chamber selected to be one of a pyrolysis reactor, a conventional gasifier or a plasma arc gasifier and wherein said reaction chamber includes a input line for receiving a gaseous stream provided by a source separate from said reaction chamber, and said reaction chamber capable of operating at a preferred temperature of about 1330° C. and up to about 2000° C. and a pressure of about one bar or greater and capable of supporting a reaction in said reaction chamber to form syngas comprising carbon monoxide (CO) and hydrogen (H), and carbon dioxide (CO);'}a source of carbonaceous material provided as a feed to said reaction chamber;{'sub': '2', 'a source of HO provided as a feed to said reaction chamber;'}{'sub': '2', 'a selected one of a power plant or an industrial plant capable of providing said gaseous stream from said separate source as a feed to said reaction chamber at said input line, said gaseous stream being a gaseous exhaust containing between about 30% to about 45% carbon dioxide (CO);'}{'sub': 2', '2', '2', '2, 'said reaction chamber further capable of supporting a reaction that consists essentially of said carbonaceous material, said HO and said carbon dioxide (CO) in ...

Waste Processing

This invention provides a system () for generating energy from waste material. The system comprises a first batch processing oven () for generating syngas and a second batch processing oven () for generating syngas. At least one thermal treatment chamber () heats the syngas after it is produced, and an energy converter () converts energy from the syngas to electrical energy. 1. A system for generating energy from waste material comprising:a first batch processing oven for generating syngas;a second batch processing oven for generating syngas;at least one thermal treatment chamber for heating said syngas;and an energy converter for converting energy from the syngas to electrical energy.2. A system according to wherein the thermal treatment chamber includes one or more burners for burning said syngas and the energy convertor includes a heat recovery means for recovering heat from the burning gases.3. A system according to wherein the thermal treatment chamber includes one or more burners for heating said syngas without combusting it claim 1 , and the energy converter comprises a syngas engine.4. A system as claimed in further comprising a third or third and fourth batch processing oven for generating syngas.5. A system as claimed in further comprising control means for controlling the supply of syngas from said first and subsequent batch processing ovens to the or each said thermal treatment chamber in dependence on at least one operating parameter of said apparatus claim 1 , thereby to ensure a substantially constant supply of syngas to said thermal treatment chamber.6. A system as claimed in wherein said operating parameter is the content of carbon monoxide in said syngas.7. A system as claimed in wherein the control means is operable to control the supply of syngas from one batch processing oven to the thermal treatment chamber while another batch processing oven is being emptied and refilled.8. A system as claimed in wherein the control means is configured to ...

PRODUCTION OF PRODUCTS WITH FAVOURABLE GHG EMISSION REDUCTIONS FROM CELLULOSIC FEEDSTOCKS

The present invention provides a process for producing one or more products for use as a transportation or heating fuel. In various embodiments the process comprises treating a cellulosic feedstock in one or more processing steps that release extractives from the feedstock. A solids-liquid separation is subsequently conducted on the process stream comprising the extractives and solids. An aqueous stream comprising one or more of the extractives may be fed to an anaerobic digester to produce crude biogas from which one or more impurities may optionally be removed. In various embodiments the process further comprises providing a solids stream to a thermal process. A product produced or derived from the thermal process may displace a product made from fossil fuel. One or more products obtained or derived from at least one of the foregoing process steps are provided for use as a transportation or heating fuel. In various embodiments the process enables advantaged fuel credit generation. 130-. (canceled)31. A process for producing a transportation or heating fuel comprising the steps of:(i) treating a cellulosic feedstock in one or more processing steps that release extractives from the feedstock, said extractives comprising acetic acid, acetate, or a combination thereof;(ii) conducting a solids-liquid separation on a process stream comprising the extractives and solids comprising insoluble components, thereby producing an aqueous stream comprising the extractives and a solids stream comprising insoluble components;(iii) feeding an aqueous stream comprising one or more of the extractives or a portion of said aqueous stream to an anaerobic digester to produce crude biogas and optionally removing at least a portion of one or more impurities from the crude biogas;(iv) carrying out or causing one or more parties to carry out a process comprising (a) gasifying a solids stream comprising the insoluble components to produce syngas, and (b) reacting the syngas to produce a fuel ...

Processes for Making Synthesis Gas and Syngas-Derived Products

The present invention provides processes for making synthesis gas and processes for making syngas-derived products. For example, one aspect of the present invention provides a process for making a synthesis gas stream comprising hydrogen and carbon monoxide, the process comprising (a) providing a carbonaceous feedstock; (b) reacting the carbonaceous feedstock in a gasification reactor in the presence of steam and a gasification catalyst under suitable temperature and pressure to form a raw product gas stream comprising a plurality of gases comprising methane, hydrogen and carbon monoxide; (c) removing steam from and sweetening the raw product gas stream to form a sweetened gas stream; (d) separating and adding steam to the sweetened gas stream to form a first reformer input gas stream having a first steam/methane ratio; and a second reformer input stream having a second steam/methane ratio, in which the first steam/methane ratio is smaller than the second steam/methane ratio; (e) reforming the second reformer input stream to form a recycle gas stream comprising steam, carbon monoxide and hydrogen; (f) introducing the recycle gas stream to the gasification reactor; and (g) reforming the first reformer input stream to form the synthesis gas stream.

Continuous Process for Converting Carbonaceous Feedstock into Gaseous Products

Continuous processes for converting a carbonaceous feedstock into a plurality of gaseous products are described. The continuous processes include, among other steps, recovering a substantial portion of alkali metal from the solid char that results from the gasification of a carbonaceous feedstock. The alkali metal is recovered as an alkali metal carbonate. A gasification catalyst for a subsequent gasification step may comprise the recovered alkali metal carbonate and a makeup amount of alkali metal hydroxide.

Sour Shift Process for the Removal of Carbon Monoxide from a Gas Stream

Processes for the catalytic conversion of a carbonaceous composition into a gas stream comprising methane are provided, where a sour shift reaction is used to remove carbon monoxide gas stream produced by the gasification process. The incorporation of the sour shift reaction provides an efficient and cost-effective means of eliminating carbon monoxide from the gas stream. In addition, the sour shift reaction also generates additional hydrogen, thus increasing the amount of hydrogen produced from the gasification process.

Two-Train Catalytic Gasification Systems

Systems for converting a carbonaceous feedstock into a plurality of gaseous products are described. The systems include, among other units, two separate gasification reactors to convert a carbonaceous feedstock in the presence of an alkali metal catalyst into the plurality of gaseous products including at least methane. Each of the gasification reactors may be supplied with the feedstock from a single or separate catalyst loading and/or feedstock preparation unit operations. Similarly, the hot gas streams from each gasification reactor may be purified via their combination at a heat exchanger, acid gas removal, or methane removal unit operations. Product purification may comprise trace contaminant removal units, ammonia removal and recovery units, and sour shift units.

Three-Train Catalytic Gasification Systems

Systems to convert a carbonaceous feedstock into a plurality of gaseous products are described. The systems include, among other units, three separate gasification reactors for the gasification of a carbonaceous feedstock in the presence of an alkali metal catalyst into the plurality of gaseous products including at least methane. Each of the gasification reactors may be supplied with the feedstock from a single or separate catalyst loading and/or feedstock preparation unit operations. Similarly, the hot gas streams from each gasification reactor may be purified via their combination at a heat exchanger, acid gas removal or methane removal unit operations. Product purification may comprise trace contaminant removal units, ammonia removal and recovery units, and sour shift units.

Four-Train Catalytic Gasification Systems

Systems to convert a carbonaceous feedstock into a plurality of gaseous products are described. The systems include, among other units, four separate gasification reactors for the gasification of a carbonaceous feedstock in the presence of an alkali metal catalyst into the plurality of gaseous products including at least methane. Each of the gasification reactors may be supplied with the feedstock from a single or separate catalyst loading and/or feedstock preparation unit operations. Similarly, the hot gas streams from each gasification reactor may be purified via their combination at a heat exchanger, acid gas removal, or methane removal unit operations. Product purification may comprise trace contaminant removal units, ammonia removal and recovery units, and sour shift units.

Four-Train Catalytic Gasification Systems

Systems to convert a carbonaceous feedstock into a plurality of gaseous products are described. The systems include, among other units, four separate gasification reactors for the gasification of a carbonaceous feedstock in the presence of an alkali metal catalyst into the plurality of gaseous products including at least methane. Each of the gasification reactors may be supplied with the feedstock from a single or separate catalyst loading and/or feedstock preparation unit operations. Similarly, the hot gas streams from each gasification reactor may be purified via their combination at a heat exchanger, acid gas removal, or methane removal unit operations. Product purification may comprise trace contaminant removal units, ammonia removal and recovery units, and sour shift units.

Four-Train Catalytic Gasification Systems

Systems to convert a carbonaceous feedstock into a plurality of gaseous products are described. The systems include, among other units, four separate gasification reactors for the gasification of a carbonaceous feedstock in the presence of an alkali metal catalyst into the plurality of gaseous products including at least methane. Each of the gasification reactors may be supplied with the feedstock from a single or separate catalyst loading and/or feedstock preparation unit operations. Similarly, the hot gas streams from each gasification reactor may be purified via their combination at a heat exchanger, acid gas removal, or methane removal unit operations. Product purification may comprise trace contaminant removal units, ammonia removal and recovery units, and sour shift units.

Processes for Gasification of a Carbonaceous Feedstock

The present invention relates to processes and continuous processes for preparing gaseous products, and in particular, methane via the catalytic gasification of carbonaceous feedstocks in the presence of steam. In one aspect of the invention, the processes comprise at least partially combusting a first carbonaceous feedstock with an oxygen-rich gas stream in an oxygen-blown gasifier, under suitable temperature and pressure, to generate a first gas stream comprising hydrogen, carbon monoxide and superheated steam; and reacting a second carbonaceous feedstock and the first gas stream in a catalytic gasifier in the presence of a gasification catalyst under suitable temperature and pressure to form a second gas stream comprising a plurality of gaseous products comprising methane, carbon dioxide, hydrogen, carbon monoxide and hydrogen sulfide. The processes can comprise using at least one catalytic methanator to convert carbon monoxide and hydrogen in the gaseous products to methane and in certain embodiments do not recycle carbon monoxide or hydrogen to the gasifier.

Processes for Gasification of a Carbonaceous Feedstock

The present invention relates to processes for preparing gaseous products, and in particular, methane via the catalytic gasification of carbonaceous feedstocks in the presence of steam. The processes comprise using at least one methanation step to convert carbon monoxide and hydrogen in the gaseous products to methane and do not recycle carbon monoxide or hydrogen to the catalytic gasifier.

Char Methanation Catalyst and its Use in Gasification Processes

The invention provides processes for generating a methane-enriched gas from a gas mixture comprising carbon monoxide and hydrogen such as gas streams generated by gasification of an alkali metal catalyst-loaded carbonaceous feedstock, and a char methanation catalyst useful in such processes.

Processes for Hydromethanation of a Carbonaceous Feedstock

The present invention relates to processes for preparing gaseous products, and in particular methane, via the hydromethanation of a carbonaceous feedstock in the presence of steam, syngas, a hydromethanation catalyst and an oxygen-rich gas stream.

Processes for Hydromethanation of a Carbonaceous Feedstock

The present invention relates to processes for preparing gaseous products, and in particular methane, via the hydromethanation of carbonaceous feedstocks in the presence of steam, carbon monoxide, hydrogen and a hydromethanation catalyst.

Processes For Hydromethanation Of A Carbonaceous Feedstock

The present invention relates to processes for preparing gaseous products, and in particular methane, via the catalytic hydromethanation of a carbonaceous feedstock in the presence of steam, syngas and an oxygen-rich gas stream.

Processes for Gasification of a Carbonaceous Feedstock

The present invention relates to processes for preparing gaseous products, and in particular, methane via the catalytic gasification of carbonaceous feedstocks in the presence of steam and an oxygen-rich gas stream. The processes comprise using at least one catalytic methanator to convert carbon monoxide and hydrogen in the gaseous products to methane and do not recycle carbon monoxide or hydrogen to the catalytic gasifier.

Integrated biorefinery for production of liquid fuels

A method and system for reforming a carbonaceous feedstock comprising the steps, reforming the feedstock produce a first synthesis gas, subjecting a portion of the first synthesis gas to catalytic conversion, separating from the synthesis gas conversion product at least one byproduct, and utilizing at least a portion of the at least one byproduct during reforming of additional carbonaceous material. In certain instances, the method and system may be used to produce a liquid fuel.

Biomass high efficiency hydrothermal reformer

A system for the production of synthesis gas, the system including a mixing apparatus configured for combining steam with at least one carbonaceous material to produce a reformer feedstock; and a reformer comprising a cylindrical vessel containing a plurality of coiled tubes, wherein each of the plurality of coiled tubes has a vertical height in the range of from about 40 feet 12.2 m) to about 100 feet (30.5 m) and a coil length that is at least four times the vertical height; at least one burner configured to combust a fuel and provide heat to maintain the reformer at a reformer temperature; at least one outlet for reformer product comprising synthesis gas; and at least one outlet for flue gas produced via combustion of fuel in the burners. A suitable mixing apparatus is also provided.

Biomass high efficiency hydrothermal reformer

A method of producing synthesis gas by mixing a carbonaceous feed comprising at least one carbonaceous material with superheated steam to produce a reformer feedstock and reforming the reformer feedstock to produce a first synthesis gas comprising hydrogen and carbon monoxide by introducing the reformer feedstock into a plurality of coiled tubes within a reformer at a reformer temperature and a reformer pressure at which at least a portion of the reformer feedstock is converted to synthesis gas.

Integrated biorefinery for production of liquid fuels

A method and system for reforming a carbonaceous feedstock comprising the steps, reforming the feedstock produce a first synthesis gas, subjecting a portion of the first synthesis gas to catalytic conversion, separating from the synthesis gas conversion product at least one byproduct, and utilizing at least a portion of the at least one byproduct during reforming of additional carbonaceous material. In certain instances, the method and system may be used to produce a liquid fuel.

Integrated biorefinery for production of liquid fuels

A system for the production of conversion products from synthesis gas, the system including a mixing apparatus configured for mixing steam with at least one carbonaceous material to produce a reformer feedstock; a reformer configured to produce, from the reformer feedstock, a reformer product comprising synthesis gas comprising hydrogen and carbon monoxide from the reformer feedstock; a synthesis gas conversion apparatus configured to catalytically convert at least a portion of the synthesis gas in the reformer product into synthesis gas conversion product and to separate from the synthesis gas conversion product a tailgas comprising at least one gas selected from the group consisting of carbon monoxide, carbon dioxide, hydrogen and methane; and one or more recycle lines fluidly connecting the synthesis gas conversion apparatus with the mixing apparatus, the reformer, or both.

Integrated biorefinery for production of liquid fuels

A system including a mixing apparatus configured to produce a reformer feedstock and comprising one or more cylindrical vessel having a conical bottom section, an inlet for superheated steam within the conical bottom section and an inlet for at least one carbonaceous material at or near the top of the cylindrical vessel, wherein the one or more cylindrical vessel is a pressure vessel configured for operation at a pressure in the range of from about 5 psig (34.5 kPa) to about 50 psig (344.7 kPa); a reformer configured to produce, from the reformer feedstock, a reformer product comprising synthesis gas, and also producing a hot flue gas; a synthesis gas conversion apparatus configured to catalytically convert at least a portion of the synthesis gas in the reformer product into synthesis gas conversion product, and to separate, from the synthesis gas conversion product, a spent catalyst stream and a tailgas.

Biomass high efficiency hydrothermal reformer

A mixing apparatus for producing a feedstock for a reformer, the mixing apparatus including at least one mixing vessel comprising a cylindrical vessel with a conical bottom; a steam inlet configured for introducing steam into the conical bottom; a carbonaceous material inlet configured for introducing a carbonaceous feed into the cylindrical vessel; and an outlet for a reformer feedstock comprising at least 0.3 pounds of steam per pound of carbonaceous material, with the at least one mixing vessel configured for operation at a pressure of greater than about 10 psig.

Biomass high efficiency hydrothermal reformer

A mixing apparatus for producing a feedstock for a reformer, the mixing apparatus including at least one mixing vessel comprising a cylindrical vessel with a conical bottom; a steam inlet configured for introducing steam into the conical bottom; a carbonaceous material inlet configured for introducing a carbonaceous feed into the cylindrical vessel; and an outlet for a reformer feedstock comprising at least 0.3 pounds of steam per pound of carbonaceous material, with the at least one mixing vessel configured for operation at a pressure of greater than about 10 psig.

Combined Hydrothermal Liquefaction and Catalytic Hydrothermal Gasification System and Process for Conversion of Biomass Feedstocks

A combined hydrothermal liquefaction (HTL) and catalytic hydrothermal gasification (CHG) system and process are described that convert various biomass-containing sources into separable bio-oils and aqueous effluents that contain residual organics. Bio-oils may be converted to useful bio-based fuels and other chemical feedstocks. Residual organics in HTL aqueous effluents may be gasified and converted into medium-BTU product gases and directly used for process heating or to provide energy. 119-. (canceled)20. A system for conversion of a biomass , the system comprising:a hydrothermal liquefaction (HTL) stage apparatus that hydrothermally liquefies the biomass in an aqueous medium at a temperature and pressure selected to form a crude conversion product comprising a bio-oil component and an aqueous component; anda catalytic hydrothermal gasification (CHG) stage apparatus operatively coupled to the hydrothermal liquefaction (HTL) stage apparatus and configured to receive at least a portion of the crude conversion product having both the bio-oil component and the aqueous component, and form, at a selected temperature and pressure, a gas product containing at least one medium BTU product gas.21. The system of further including an upgrade stage apparatus configured to upgrade the bio-oil component released from the hydrothermal liquefaction (HTL) stage apparatus over a hydrogenation catalyst at a temperature up to about 450° C. and a hydrogen partial pressure up to about 150 atmospheres (1.52×104 kPa) that yields a green crude.22. The system of further comprising at least one heat exchanger operatively coupled to the upgrade stage apparatus.23. The system of further comprising another heat exchanger operatively coupled to the hydrothermal liquefaction (HTL) stage apparatus.24. The system of wherein the heat exchangers are operably engaged to exchange thermal transfer fluid.25. The system of wherein the gas product when combusted generates sufficient energy such that the ...

Fuel production system

Fuel production system includes: synthesis gas generation unit configured to generate synthesis gas containing hydrogen and carbon monoxide from carbon-containing raw material; fuel production unit configured to produce fuel from synthesis gas generated; water electrolyzer configured to electrolyze water to generate water-electrolyzed hydrogen; hydrogen supply unit configured to supply water-electrolyzed hydrogen generated to synthesis gas generation unit; and controller. The controller is configured to perform: calculating input energy based on first energy possessed by raw material, second energy consumed by water electrolyzer, third energy consumed by synthesis gas generation unit, and fourth energy consumed by fuel production unit; calculating recovered energy based on fifth energy possessed by fuel produced; and controlling water electrolyzer based on input energy and recovered energy calculated.

Устройство и способ для термохимической гармонизации и газификации влажной биомассы

1. Устройство для термохимической карбонизации и газификации влажной, в особенности водосодержащей и/или сухой, биомассы для изготовления энергоносителя и/или сырьевого носителя посредством реактора (1) карбонизации с подогревом, имеющего закрывающееся входное отверстие (13), в котором биомасса преобразовывается в твердый, наливной или газообразный энергоноситель и/или сырьевой носитель и выводится через закрывающееся выходное отверстие (14) в охлаждаемый резервуар (9), соединенный с реактором (1) карбонизации для временного хранения энергоносителя и/или сырьевого носителя, который соединен с нижестоящим реактором (16) газификации, в котором газ и отходы, такие как зола, отделяются от биомассы, отличающееся следующими признаками:a) внешняя тепловая энергия (60) подается в реактор (1) карбонизации, который функционально соединен с нагревательным элементом (4), в частности окружен нагревательной рубашкой, и далее тепловая энергия подается, по меньшей мере, от одной установки, в особенности от реактора (16) газификации,b) энергия охлаждения от второго резервуара или охлаждающего резервуара (9) подается в реактор газификации,c) влага, в особенности вода, подается во второй резервуар или охлаждающий резервуар (9), чтобы обеспечить почти непрерывный процесс,d) из реактора (1) карбонизации и/или второго резервуара или охлаждающего резервуара (9), реакционный газ подается в емкость (21) для хранения газа, где реакционный газ повторно подается в реактор (16) газификации.2. Устройство по п.1, отличающееся тем, что влагосодержащая биомасса, принимаемая в реакторе (1) карбонизации, выпаривается под давлением от 5 до 30 бар, предпочтительно под РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК C10J 3/26 (11) (13) 2012 151 909 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2012151909/10, 14.02.2011 (71) Заявитель(и): ЦББ ГМБХ (DE) Приоритет(ы): (22) Дата подачи заявки: 14.02.2011 (43) Дата публикации заявки: 10.01.2015 Бюл. № 1 ( ...

Система, вырабатывающая электрическую энергию с помощью газификации горючих веществ

Изобретение относится к области электротехники, в частности к технологии преобразования химической энергии горючих веществ в электрическую энергию с высокой эффективностью, где горючие вещества газифицируются для получения газа и полученный газ используется в топливном элементе для выработки электрической энергии. Техническим результатом изобретения является повышение эффективности преобразования химической энергии горючих веществ в электрическую. Предложенная низкотемпературная газификационная печь для газификации горючих веществ, таких как горючие отходы или уголь, работает при температуре, например, 400-1000°С, а полученный газ затем подается в топливный элемент для выработки электрической энергии. Низкотемпературная газификационная печь предпочтительно представляет собой газификационную печь с псевдоожиженным слоем. 3 н. и 8 з.п. ф-лы, 25 ил. ÐÎÑÑÈÉÑÊÀß ÔÅÄÅÐÀÖÈß RU (19) (11) 2 270 849 (13) C2 (51) ÌÏÊ C10J 3/00 (2006.01) H01M 8/06 (2006.01) ÔÅÄÅÐÀËÜÍÀß ÑËÓÆÁÀ ÏÎ ÈÍÒÅËËÅÊÒÓÀËÜÍÎÉ ÑÎÁÑÒÂÅÍÍÎÑÒÈ, ÏÀÒÅÍÒÀÌ È ÒÎÂÀÐÍÛÌ ÇÍÀÊÀÌ (12) ÎÏÈÑÀÍÈÅ ÈÇÎÁÐÅÒÅÍÈß Ê ÏÀÒÅÍÒÓ (21), (22) Çà âêà: 2001115091/09, 05.11.1999 (24) Äàòà íà÷àëà îòñ÷åòà ñðîêà äåéñòâè ïàòåíòà: 05.11.1999 (30) Ïðèîðèòåò: 05.11.1998 JP 10/330161 (73) Ïàòåíòîîáëàäàòåëü(è): ÈÁÀÐÀ ÊÎÐÏÎÐÅÉØÍ (JP) (45) Îïóáëèêîâàíî: 27.02.2006 Áþë. ¹ 6 2 2 7 0 8 4 9 (56) Ñïèñîê äîêóìåíòîâ, öèòèðîâàííûõ â îò÷åòå î ïîèñêå: RU 2107359 C1, 20.03.1973. RU 2073064 C1, 10.02.1997. RU 2121197 C1, 27.10.1998. SU 1114342 A3, 15.09.1984. RU 2014346 C1, 15.06.1994. ÅÐ 0170277 À, 05.02.1986. US 5509264 À, 23.04.1996. (85) Äàòà ïåðåâîäà çà âêè PCT íà íàöèîíàëüíóþ ôàçó: 05.06.2001 2 2 7 0 8 4 9 R U (87) Ïóáëèêàöè PCT: WO 00/27951 (18.05.2000) C 2 C 2 (86) Çà âêà PCT: JP 99/06185 (05.11.1999) Àäðåñ äë ïåðåïèñêè: 129010, Ìîñêâà, óë. Á.Ñïàññêà , 25, ñòð.3, ÎÎÎ "Þðèäè÷åñêà ôèðìà Ãîðîäèññêèé è Ïàðòíåðû", ïàò.ïîâ. Å.È.Åìåëü íîâó (54) ÑÈÑÒÅÌÀ, ÂÛÐÀÁÀÒÛÂÀÞÙÀß ÝËÅÊÒÐÈ×ÅÑÊÓÞ ÝÍÅÐÃÈÞ Ñ ÏÎÌÎÙÜÞ ÃÀÇÈÔÈÊÀÖÈÈ ÃÎÐÞ×ÈÕ ÂÅÙÅÑÒ (57) Ðåôåðàò: Èçîáðåòåíèå îòíîñèòñ ...

Реактор газификации

Реактор газификации может быть использован для производства энергоносителей в виде горячей воды, пара и горючего синтез-газа для производства электроэнергии. Реактор газификации содержит котел 23 с крышкой 2, с двумя концентрично расположенными один в другом внутренними и внешними кожухами, выполненными в виде кольцевых теплообменных рубашек, газоход 35 между ними, лопастной ворошитель сырья 5, усеченный конус 11, зону первичной газификации 9 и регенерации газов 10, горелку 12. Реактор дополнительно снабжен системой нижнего ворошения 13, с лопастным ворошителем 14, расположенным в усеченном конусе 11, закрепленном в корпусе герметично, теплосъемными водяными стержнями 24, расположенными в газоходе 35, зоной синтеза метана 17, расположенной на входе в газоход 35. Сопло горелки 12 расположено в герметичной полости между стенками конуса 11 и его корпуса 32. Реактор снаружи покрыт теплоизоляционными материалами 33, а внутренняя поверхность зоны первичной газификации футерована термоизоляционными материалами. Изобретение позволяет повысить теплотворную способность вырабатываемого синтез-газа без увеличения габаритов установки. 1 з.п. ф-лы, 1 ил. РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2 482 164 (13) C1 (51) МПК C10J 3/20 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ (21)(22) Заявка: 2011146926/05, 21.11.2011 (24) Дата начала отсчета срока действия патента: 21.11.2011 Приоритет(ы): (22) Дата подачи заявки: 21.11.2011 (72) Автор(ы): Силантьева Лариса Яковлевна (RU) (73) Патентообладатель(и): Силантьева Лариса Яковлевна (RU) R U (45) Опубликовано: 20.05.2013 Бюл. № 14 C 1 2 4 8 2 1 6 4 R U C 1 Адрес для переписки: 443083, г.Самара, ул. Победы, 5, кв.25, Л.Я.Силантьевой (54) РЕАКТОР ГАЗИФИКАЦИИ (57) Реферат: Реактор газификации может быть использован для производства энергоносителей в виде горячей воды, пара и горючего синтез-газа для производства электроэнергии. Реактор газификации содержит котел 23 с крышкой 2, с двумя ...

Fuel feed system for a gasifier and method of gasification system start-up

A method of startup for a gasification system includes assembling a fuel mixture for use by a gasifier at a fuel mixture assembly point, wherein the fuel mixture includes a quantity of particulate solid fuel and a quantity of non-ventable carrier gas. The method includes channeling the fuel mixture through a first conduit to a fuel mixture disassembly system including a non-ventable carrier gas removal apparatus, establishing a substantially steady flow of the fuel mixture within the first conduit, and redirecting the fuel mixture through a second conduit to the gasifier to facilitate gasifier startup.

エネルギー生成のために生物燃料又は屑材料を利用する方法と装置

(57)【要約】 エネルギー生成のために生物燃料若しくは屑材料又はその両者を利用する方法と装置。生物燃料又は屑材料は流動床ガス化器（１０）、好ましくは循環式流動床ガス化器の中でガス化される。ガス化器中で生成したガスは化石燃料バーナー（２８、２８’、２８”）、典型的には微粉炭バーナーを備えるボイラー（１２）に導入される。ガスはバーナーより上のレベルの所に導入される。ガス化器の床を形成するためにボイラーからの灰を用いることができる。ＮＯｘを制御するために、ガスをボイラーの上部で、８００〜１０５０℃（１４７２〜１９２２°Ｆ）、好ましくは８５０〜９００℃（１５６２〜１６５２°Ｆ）の低温度レベルにおいて、約５〜１０％の小含有空気過剰分で燃焼させる。第二の態様では、原料ガスを浄化して有害な又は有毒な成分を除き、そして、所望によっては、ガス化器とボイラーとの間において、石炭の灰の床を有する追加の循環式流動床反応器（１５２）の中で冷却することができる。

Method of conversion of solar energy into electrical energy by photosynthesis

FIELD: conversion of solar energy accumulated by photosynthesis into electrical energy. SUBSTANCE: proposed method employs closed-cycle electric station provided with water basin for growing microalgae and combustion chamber with fluidized layer; partially dried algae contain at least 60 mass-% of water; combustion is performed in artificial atmosphere of oxygen and carbon dioxide. EFFECT: enhanced efficiency. 17 cl, 3 dwg 9516$ сс ПЧ сэ (19) РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (51) МПК? 13) ВИ "” 2 239 754 ^^ С2 Е 244 2/42, Е ОЛК 25/14 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 2001126058/06, 14.03.2000 (24) Дата начала действия патента: 14.03.2000 (30) Приоритет: 22.03.1999 Ш 129,101 (43) Дата публикации заявки: 21.05.2003 (45) Дата публикации: 10.11.2004 (56) Ссылки: СВ 22548358 А, 21.10.1992. МО 95/24548 А, 14.09.1995. УР 03154616 А, 02.07.1991. 4$ 4334026 А, 22.07.1997. ($ 5375410 А, 27.12.1994. ЗЧ 1460362 А, 23.02.1989. 5Ц 1021884 А, 07.06.1983. (85) Дата перевода заявки РСТ на национальную фазу: 22.10.2001 (86) Заявка РСТ: || 00/00154 (14.03.2000) (87) Публикация РСТ: М/О 00/57105 (28.09.2000) (98) Адрес для переписки: 103009, Москва, а/я 184, ППФ "ЮС", пат.пов. С.В.Ловцову (72) Изобретатель: ЯНТОВСКИЙ Евгений (ОЕ) (73) Патентообладатель: СОЛМЕКС (ИЗРАИЛЬ) ЛТД. (11) (74) Патентный поверенный: Ловцов Сергей Викторович (54) СПОСОБ ПРЕОБРАЗОВАНИЯ СОЛНЕЧНОЙ ЭНЕРГИИ, НАКОПЛЕННОЙ ПУТЁМ ФОТОСИНТЕЗА, В ЭЛЕКТРИЧЕСКУЮ ЭНЕРГИЮ (57) Изобретение относится к способу преобразования солнечной энергии, накопленной путем фотосинтеза, В электрическую энергию. Способ осуществляется путем использования электростанции замкнутого цикла, содержащей массив воды для выращивания помещенных в него макроводорослей, и камеру сгорания с псевдоожиженным слоем для сжигания, по меньшей мере, части частично высушенных макроводорослей, содержащих до 60% мас./воды; сжигание производится в искусственно созданной атмосфере кислорода и углекислого газа ...

Реактор для газификации

1. Реактор (1) для газификации, содержащий:- камеру (2) реактора;- теплообменные блоки (3, 15, 16), генерирующие пар;- по меньшей мере один барабан (20) парового котла;- линии рециркуляции для циркуляции воды и пара между одним или более теплообменными блоками (3, 15, 16) и барабаном (20) парового котла;в котором барабан парового котла содержит линию (28) подачи пара через теплообменный блок (15) и линию (30) подачи перегретого пара к паросборнику (32) перегретого пара, при этом линия (30) подачи перегретого пара разделяется на обратную линию (33), ведущую к теплообменной линии (35), проходящей через барабан (20) парового котла, и линию (34) питания паросборника, причем реактор содержит один или более клапанов (37, 38, 39) для выборочного открывания или закрывания обратной линии (33) или линии (34) питания паросборника, теплообменная линия (35), проходящая через барабан (20) парового котла, соединяется с вторичной линией (36) подачи перегретого пара, ведущей к паросборнику (32) перегретого пара, и вторичная линия (36) подачи перегретого пара присоединяется к линии (34) питания паросборника перед ее открыванием в паросборник перегретого пара.2. Реактор для газификации по п. 1, в котором линия (30) подачи перегретого пара выше по ходу потока от обратной линии (33), снабжена одним или более температурными датчиками, и в котором один или более блоков управления клапанами выполнены с возможностью открывания или закрывания обратной линии и линии питания паросборника, соответственно, в ответ на измеренную температуру.3. Реактор для газификации по п. 1 или 2, в котором теплообменная линия (35), проходящая через барабан (20) парового котла, соединяется с линией, идущей к теплообменнику РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК F01K 13/02 (13) 2014 115 773 A (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2014115773/06, 19.09.2012 (71) Заявитель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) Приоритет(ы): (30) ...

使用炭甲烷化催化剂的气化方法

本发明提供用于由包含一氧化碳和氢气的气体混合物产生富甲烷气体的方法，所述气体混合物诸如为通过使负载碱金属催化剂的碳质原料气化产生的气流；以及可用于这类方法的炭甲烷化催化剂。

Method and system to produce energy source under thermodynamic cycle by co2 conversion from feed stock containing carbon

FIELD: power industry. SUBSTANCE: invention can be used to generate electric power from feed stock containing carbon, specifically from coal and/or dry biomass. Method of power generating from feed stock containing carbon includes stage of dry feed stock gasification in the gasification reactor by gas flow mainly containing CO 2 , at high temperature with generation of the first gas flow mainly containing molecules of carbon monoxide; oxidation in oxidating reactor by oxygen carriers in oxidized condition (MeO) at high temperature with generation of the second gas flow containing CO 2 and oxygen carriers in restored condition (Me); activation in activation reactor of the oxygen carriers in restored condition by the activation gas flow containing oxygen components, and with creation of the oxygen lean activation gas flow; and conversion of thermal energy part of the activation flow in the electric power. EFFECT: invention generates electric power from biomass containing carbon, and creation of the valuable product of common energy to supply the electric power generating system, such as turbine alternator. 15 cl, 2 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (51) МПК C10J 3/00 C01B 3/32 B01J 12/00 B01J 23/00 C10J 3/46 (13) 2 553 289 C2 (2006.01) (2006.01) (2006.01) (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2012137275/05, 08.10.2010 (24) Дата начала отсчета срока действия патента: 08.10.2010 (72) Автор(ы): ГИОМАРК Раймон Франсуа (FR), БЕНСАКРИА Аммар (FR) 01.02.2010 FR 10/00377 (43) Дата публикации заявки: 10.03.2014 Бюл. № 7 R U (73) Патентообладатель(и): СЕЕ-СОЛУСОЙНШ, ЭНЕРЖИЯ Э МЕЙУ АМБИЕНТЕ ЛТДА. (BR) Приоритет(ы): (30) Конвенционный приоритет: (45) Опубликовано: 10.06.2015 Бюл. № 16 2 5 5 3 2 8 9 (56) Список документов, цитированных в отчете о поиске: US 2008078122 A1, 03.04.2008. US 2008134579 A1, 12.06.2008. RU 2175075 C2, 20.10.2001. RU 2287010 C2, 10.11.2006. RU 2373259 C1, 20.11. ...

可燃物气化发电系统

本发明提供了一种在预定温度如400～1000℃下气化可燃物，如可燃性废弃物或煤的低温气化炉(2)，再将所生成的气体供给燃料电池(6)进行发电。低温气化炉优选包括流化床气化炉。

Structural scheme and environmentally safe method of processing wastes and biomass to increase efficiency of generating electric power and heat

FIELD: ecology; waste processing and recycling. SUBSTANCE: invention relates to a method and structural scheme of environmentally safe processing of wastes and biomass to increase efficiency of electric power and heat generation. According to structural scheme of invention solid household and industrial wastes and biomass are loaded and crushed, then subjected to pyrolysis and gasification. Obtained pyrolysis gas is cooled, purified and carbon dioxide is extracted therefrom, then purified pyrolysis gas is compressed and stored along with synthesis gas, which are used to generate electric power and heat, and generated electric power and heat are supplied to external consumers. Heat formed when cooling pyrolysis gas is then used to generate additional electric power. During pyrolysis and gasification there is melting and formation of basalt-like slag, which is processed and used to produce heat-insulating materials or granulated slag. Carbon dioxide, extracted from exhaust gases formed during production of electric power and heat, is compressed, stored together with carbon dioxide extracted from pyrolysis gas, and after distribution and dispensing, on one side, is supplied as plasma-forming gas into plasmatrons, on other side, is used for production of commercial products from carbon dioxide for external consumers, on third side is used as a feed medium for growth of algae. Seed material is loaded and algae is grown using sources of light and heat and carbon dioxide. Produced biodiesel is cleaned, stored and simultaneously with purified pyrolysis gas is used to produce electric power and heat, and biomass squeeze is returned to beginning of process. Biomass and oil from algae obtained when producing liquid biofuel, as commercial positions, are supplied to external consumers. Furthermore, in order to expand range of processed wastes simultaneously with beginning of process, coal dust is loaded, then synthesis gas is generated using heat, followed by compression of ...

气化反应器

用于含碳原料的方法和反应器。所述反应器包括：反应室(2)；产生蒸汽的换热单元(3,15,16)；至少一个蒸汽罐(20)；和在一个或多个换热单元(3,15,16)与蒸汽罐(20)之间循环水和蒸汽的循环管线。所述蒸汽罐还包括用于输送蒸汽通过换热单元(15)的蒸汽进料管线(28)和至过热蒸汽总管(32)的过热蒸汽管线(30)。所述过热蒸汽管线分为通到经过蒸汽罐的换热管线(35)的返回管线(33)和总管进料管线(34)。

Processes for gasification of a carbonaceous feedstock

본 발명은, 스팀 및 산소-풍부 기체 스트림의 존재 하에서의 탄소질 공급원료의 촉매적 기체화를 통한 기체상 생성물, 및 특히 메탄의 제조 방법에 관한 것이다. 본 발명의 방법은, 하나 이상의 촉매적 메탄화기를 사용하여 기체상 생성물 중의 일산화탄소 및 수소를 메탄으로 전환시키는 것을 포함하며, 일산화탄소 또는 수소를 촉매적 기체화기로 재순환시키지 않는다. The present invention relates to a gaseous product via catalytic gasification of a carbonaceous feedstock in the presence of steam and oxygen-rich gas streams, and in particular to a process for producing methane. The process of the present invention involves the conversion of carbon monoxide and hydrogen in the gaseous product to methane using one or more catalytic methanators and does not recycle carbon monoxide or hydrogen to the catalytic gasifier.

高效低耗高氢煤气发生系统

本发明创造涉及高效低耗高氢煤气发生系统。储煤罐与煤气发生装置连接。煤气发生装置由反应段、供气段、排灰段、汽化剂加热段、冷却段和储灰缸构成；设在反应段上端的排气管Ⅰ与旋风除尘器连接，旋风除尘器底部与反应段内腔连通；反应段与供气段之间装炉篦；供气段上设环形供气孔；汽化剂管道装在汽化剂加热段内；冷却段经出灰阀Ⅰ与储灰缸连接。旋风式炉体下端经出灰阀Ⅱ与储灰缸Ⅱ连接，沿炉体内壁和排气通道外壁制有储水箱；排气管Ⅱ一端与旋风除尘器连接，另一端与炉体连通。水蒸汽管路一端与水蒸汽出口连接，另一端与混合气室连接，富氧空气管路与混合气室连接。本发明创造种原料利用率高，煤气热值高，含氢量高，热值利用率高。

一种流化床煤气化用余热锅炉

本发明涉及一种流化床煤气化用余热锅炉，包括高温蒸发器、过热器、蒸发器、省煤器。过热器、蒸发器和省煤器设置水管式锅炉，半焦粉尘对此段金属的磨损很小。高温蒸发器采用斜火管结构，有效避免了直型火管锅炉的脱盐水中产生的空气和水蒸气浮起于火管顶部引发局部过热；并将高温蒸发器、过热器、蒸发器、省煤器四段同放于一个钢制容器中，形成组合式结构，此种结构紧凑，管理方便。省煤器用合金钢，可以避免室温水引起钢管外表面结露腐蚀。

使用炭甲烷化催化剂的气化方法

本发明提供用于由包含一氧化碳和氢气的气体混合物产生富甲烷气体的方法，所述气体混合物诸如为通过使负载碱金属催化剂的碳质原料气化产生的气流；以及可用于这类方法的炭甲烷化催化剂。

Profitable method for carbon capture and storage

The present invention generally relates to a method for sequestering carbon dioxide. Biomass is converted into paraffinic hydrocarbons. The paraffinic hydrocarbons are steam cracked into olefins. The olefins are polymerized into non-biodegradable polyolefins.

Profitable method for carbon capture and storage

The present invention generally relates to a method for sequestering carbon dioxide. Biomass is converted into paraffinic hydrocarbons. The paraffinic hydrocarbons are steam cracked into olefins. The olefins are polymerized into non-biodegradable polyolefins.

Profitable method for carbon capture and storage

The present invention generally relates to a method for sequestering carbon dioxide. Biomass is converted into paraffinic hydrocarbons. The paraffinic hydrocarbons are steam cracked into olefins. The olefins are polymerized into non-biodegradable polyolefins.

碳质原料的气化方法

本发明涉及在蒸汽和富氧气流的存在下通过碳质原料的催化气化来制备气体产物（尤其甲烷）的方法。该方法包括使用至少一个催化甲烷转化器将气体产物中的一氧化碳和氢气转化成甲烷并且没有将一氧化碳或氢气循环到催化气化器中。

Waste treatment method and gasification and melting and combustion equipment

Gasification reactor

FIELD: energy. SUBSTANCE: invention relates to power engineering. Reactor for carbon-containing fuel gasification comprises reactor chamber 2, heat exchanging units, generating steam, at least one steam boiler drum 20 and recirculation lines for circulation of water and steam between one or more heat exchanging units and steam boiler drum. At that, steam boiler drum additionally contains steam supply line 28 through heat exchanging unit 15 and superheated steam supply line 30 to steam collector 32 of superheated steam. Superheated steam supply line is divided into return line 33, leading to heat exchanging line 35, passing through steam boiler drum, and steam collector supply line 34. Also disclosed is method of lowering temperature of superheated steam flow to steam collector of superheated steam in gasification reactor. EFFECT: invention allows to increase process economic efficiency and reduce damage as a result of heat loads. 15 cl, 2 dwg РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 610 634 C2 (51) МПК F01K 13/02 (2006.01) F22G 5/16 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ФОРМУЛА (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ 2014115773, 19.09.2012 (24) Дата начала отсчета срока действия патента: 19.09.2012 (72) Автор(ы): КАР Ибрагим (DE), ШМИТЦ-ГЁБ Манфред (DE) 14.02.2017 Приоритет(ы): (30) Конвенционный приоритет: (56) Список документов, цитированных в отчете о поиске: US 4288979 A1, 15.09.1981. US 20.09.2011 EP 11181992.6 4247302 A1, 27.01.1981. US 3818869 A1, 25.06.1974. RU 2405025 C1, 27.11.2010. RU 2340651 C1, 10.12.2008. (45) Опубликовано: 14.02.2017 Бюл. № 5 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 21.04.2014 (86) Заявка PCT: EP 2012/068385 (19.09.2012) (87) Публикация заявки PCT: 2 6 1 0 6 3 4 (43) Дата публикации заявки: 27.10.2015 Бюл. № 30 R U (73) Патентообладатель(и): ШЕЛЛ ИНТЕРНЭШНЛ РИСЕРЧ МААТСХАППИЙ Б.В. (NL) Дата регистрации: 2 6 1 0 6 3 4 R U C 2 C 2 WO 2013/041543 (28.03.2013) Адрес ...

在源于非化石资源的氢气存在下由直接液化和间接液化结合的杂化途径转化碳基材料的方法

借助于直接沸腾(ebullent)床液化和通过气化随后Fischer-Tropsch合成的间接液化相结合的杂化途径将碳基材料转化为燃料基质的方法，包括制造源于非化石资源的氢气的步骤和反向水煤气反应步骤。该方法能够限制温室气体排放。

METHODS FOR CARBON DIOXIDE RECIRCULATION INTO A GASIFICATION SYSTEM

1. Способ рециркуляции диоксида углерода из первой смеси синтез-газа системы газификации, включающий: ! удаление обогащенного диоксидом углерода газа из первой смеси синтез-газа в устройстве для разделения; ! сжатие обогащенного диоксидом углерода газа; и ! подачу по меньшей мере первой части сжатого обогащенного диоксидом углерода газа в газификатор. ! 2. Способ по п.1, в котором при газификации получают вторую смесь синтез-газа, причем указанный способ дополнительно включает охлаждение второй смеси синтез-газа в излучательном охладителе синтез-газа. ! 3. Способ по п.2, дополнительно включающий подачу охлажденной второй смеси синтез-газа в скруббер для синтез-газа. ! 4. Способ по п.3, дополнительно включающий: ! охлаждение обработанной в скруббере смеси синтез-газа, выгруженной из скруббера для синтез-газа; и ! направление охлажденной, обработанной в скруббере смеси синтез-газа в устройство для разделения. ! 5. Способ по п.2, дополнительно включающий приведение второй смеси синтез-газа в контакт со второй частью сжатого обогащенного диоксидом углерода газа в излучательном охладителе синтез-газа для облегчения охлаждения второй смеси синтез-газа. ! 6. Способ по п.5, дополнительно включающий: ! приведение охлажденной второй смеси синтез-газа в контакт с третьей частью сжатого обогащенного диоксидом углерода газа с образованием смеси; и ! направление этой смеси в конвекционный охладитель синтез-газа. ! 7. Способ по п.1, дополнительно включающий нагревание сжатого обогащенного диоксидом углерода газа перед подачей первой части сжатого обогащенного диоксидом углерода газа в газификатор. ! 8. Способ по п.1, в котором ука� РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2010 124 202 (13) A (51) МПК C10J 3/66 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (71) Заявитель(и): Дженерал Электрик Компани (US) (21)(22) Заявка: 2010124202/05, 16.06.2010 Приоритет(ы): (30) Конвенционный приоритет: 17.06.2009 US 12/486,228 A 2 0 1 0 1 2 4 2 0 2 R U ...

Method and device for gasification of combustion material in fluidized-bed furnace

FIELD: gasification of combustible materials, such as wastes, coal, etc. for production of combustible gas containing large amount of combustible materials sufficient for melting ash under action of their own heat. SUBSTANCE: fluidized-bed furnace 2 has form of approximately round horizontal cross section. Movable bed 9 where fluidized medium settles and gets sprayed is formed in central zone of furnace and fluidized bed 10 where fluidized medium is intensively fluidized is formed in peripheral zone of furnace. Fluidized medium turns in upper portion of movable bed 9 form upper portion of fluidized bed 10, circulating in both beds. Combustible material 11 is molten in upper portion of movable bed 9 and is gasified forming combustible gas during circulation together with fluidized medium. Amount of oxygen fed to fluidized-bed furnace 2 corresponds to amount of oxygen contained in air which is no more than 30% of theoretical amount of air required for combustion. Temperature of fluidized bed 10 is set between 450 and 650 C owing to which combustible gas contains considerable amount of combustible materials. Combustible gas and small particles formed in fluidized-bed furnace 2 are fed to furnace for burning the molten mass where they are burnt at high temperature at which ash gets molten. EFFECT: forming combustible gas at high efficiency. 22 cl, 14 dwg Оз гс ПЧ ГЭ РОССИЙСКОЕ АГЕНТСТВО ПО ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (19) (51) МПК ВИ” 2138 730. 13) Сл Е 23 С 11/02 12) ОПИСАНИЕ ИЗОБРЕТЕНИЯ К ПАТЕНТУ РОССИЙСКОЙ ФЕДЕРАЦИИ (21), (22) Заявка: 95103554/06, 09.03.1995 (24) Дата начала действия патента: 09.03.1995 (30) Приоритет: 10.03.1994 /Р 65439/1994 15.04.1994 УР 101541/1994 09.02.1995 УР 22000/1995 (46) Дата публикации: 27.09.1999 (56) Ссылки: УР 2-147692 А, 06.06.90. ЗЦ 1686259 АЛ, 23.10.91. $Ц 1451456 АЛ, 15.01.89. $4 1343182 АД, 07.10.87. 5Ц 1258334 АЗ, 15.09.86. ОЕ 3115236 А, 30.04.83. (98) Адрес для переписки: 121087, Москва, а/я 33, Патентному поверенному Курышеву В. ...

A kind of system and method being generated electricity using mud

本发明公开了一种利用污泥进行发电的系统及方法。该系统包括：干化装置，具有污泥入口、干化污泥出口、干燥水出口、蒸汽入口、冷却水出口；蓄热式旋转床，具有原料入口、热解水出口、热解油气出口、热解炭出口，原料入口与干化污泥出口相连；气化熔融反应室，具有热解油气入口、热解炭入口、热态合成气出口、熔渣出口，热解油气入口与热解油气出口相连，热解炭入口与热解炭出口相连；换热装置，具有热态合成气入口、冷态合成气出口、废水出口、冷却水入口和蒸汽出口，热态合成气入口与热态合成气出口相连；发电装置，具有蒸汽入口、乏汽出口和电量输出端，蒸汽入口与蒸汽出口相连。本发明实现了污泥的“无害化、减量化、资源化”。

Device for thermochemical harmonisation and gasification of wet biomass and its application

FIELD: process engineering. SUBSTANCE: invention relates to production of power carrier and/or stock carrier from water-containing and/or dry biomass. Invention covers the device for thermochemical carbonation and gasification of wet biomass and its application. This device comprises carbonation heated reactor wherein biomass is converted into solid, liquid or gaseous power carrier and/or stock carrier. Converted biomass is directed via closing outlet into cooling tank for temporary store of power carrier and/or stock carrier, said tank being connected with carbonation reactor. Cooling tank is connected with gasification heated reactor wherein gas and wastes like ash are separated from power carrier. Carbonation reactor is enclosed in heating jacket for feed of heat power and extra heat power from gasification reactor. Energy of cooling from cooling tank is fed to gasification reactor cooling jacket. Water is fed to cooling reactor to allow a continuous working cycle. Reaction gas is fed from carbonation reactor and/or cooling tank into gas store vessel. EFFECT: production of all carbon from biomass gases, ruled out critical reaction products as gases and evaporation via combustion in gasification reaction. 12 cl, 4 dwg, 2 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (51) МПК C10J 3/26 C10J 3/66 (11) (13) 2 562 112 C2 (2006.01) (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2012151909/10, 14.02.2011 (24) Дата начала отсчета срока действия патента: 14.02.2011 (72) Автор(ы): ДЕМИР Эльхан (DE) (73) Патентообладатель(и): ЦББ ГМБХ (DE) (43) Дата публикации заявки: 10.01.2015 Бюл. № 1 R U Приоритет(ы): (22) Дата подачи заявки: 14.02.2011 (45) Опубликовано: 10.09.2015 Бюл. № 25 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 05.07.2013 (86) Заявка PCT: DE 2011/075023 (14.02.2011) 2 5 6 2 1 1 2 (56) Список документов, цитированных в отчете о поиске: DE 10 2008047201 A1, 15.04.2010. WO2010063206 A1, 10. ...

Step modular entrained flow bed gas preparation system

本发明提供一种梯级模块化气流床煤气制备系统，包括：依序连通的给煤单元、气化单元、收集单元、热处理单元，收集单元包括第一煤气出口；热处理单元包括依序连通的蒸汽过热器、蒸发器和省煤器；收集单元通过第一煤气出口与蒸汽过热器的煤气入口连通；还包括第一汽包，省煤器的出水口与第一汽包的入水口连通，第一汽包的出水口与蒸发器的入水口连通，蒸发器的出汽口与第一汽包的入汽口连通，第一汽包的出汽口与蒸汽过热器的入汽口连通。本发明适用于中低压气流床煤气制备系统，由于换热结构采用管壳式换热结构，既不会使冷却水受到污染，还能够对余热进行梯级回收利用。

Four-train catalytic gasification systems for sng production

탄소질 공급물을 다수의 기체 생성물로 전환시키기 위한 시스템이 기재되어 있다. 시스템은, 다른 장치들 중에서, 탄소질 공급물을 알칼리 금속 촉매의 존재 하에 적어도 메탄을 포함한 다수의 기체 생성물로 전환시키기 위한 2개의 별도의 기체화 반응기를 포함한다. 단일 또는 별개의 촉매 부하로부터의 공급물 및/또는 공급물 제조 장치 작업을 각각의 기체화 반응기에 공급할 수 있다. 유사하게, 각각의 기체화 반응기로부터의 고온 기체 흐름을 열 교환기, 산 기체 제거 또는 메탄 제거 장치 작업에서의 조합을 통해 정제할 수도 있다. 생성물 정제는 미량 오염물 제거 장치, 암모니아 제거 및 회수 장치 및 사워 시프트 장치를 포함할 수도 있다. A system for converting a carbonaceous feed to a plurality of gaseous products is described. The system includes, among other apparatuses, two separate gasification reactors for converting the carbonaceous feed into a plurality of gas products including at least methane in the presence of an alkali metal catalyst. Feeds from a single or separate catalyst load and / or feed manufacturing apparatus operations may be fed to each gasification reactor. Similarly, the hot gas flow from each gasification reactor may be purified through a combination in a heat exchanger, acid gas removal or methane removal apparatus operation. Product purification may include trace contaminant removal devices, ammonia removal and recovery devices, and sour shift devices.

METHOD AND INSTALLATION FOR PRODUCING ENERGY BY GASIFICATION OF GARBAGE

1. Способ получения полезной энергии путем газификации мусора, при котором отходы, такие, как городской мусор, направляют в шахтный плавильный газогенератор (15), высушивают в противотоке, дегазируют и газифицируют с расплавлением твердых остатков, расплавленные остатки выпускают, а газ, содержащий пыль, отводят сверху, горячий сырой газ очищают и охлаждают, пропускают через зону разделения и подвергают электростатическому отделению, после чего полученный газ направляют дальше в горелку или, в общем случае, для получения (18) полезной энергии, отличающийся тем, что отводимые с плавильного газогенератора (15) горячие сырые газы подают на генератор (18) пара и горячих газов, в котором к горячему газу подмешивается водяной пар, и эта смесь горячего газа с паром через сдвоенный ротор (18.13) турбины подается на турбину (18.3), приводящую во вращение генератор (18.4) тока, причем одновременно происходит предварительная реакция, ! затем предварительно очищенная смесь горячего газа с паром подается в устройство (38) с падающим потоком, в котором с использованием подаваемой через насадки воды с примешанным реактивом путем многократного расширения и сжатия с пенообразованием смесь охлаждается и предварительно очищается, причем предварительно очищенный газ отводится, а жидкость собирается, ! предварительно очищенный газ направляется на газоочистку (40), где газ с реактивом вспенивается с последующим пеногашением, ! очищенные газы в заключение подвергаются дальнейшей переработке в энергетических целях, например сжиганию в двигателе (41). ! 2. Способ по п.1, отличающийся тем, что направляющий цилиндр (15.9) с радиальными крытыми отверстия РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) 2009 124 480 (13) A (51) МПК F23G 5/02 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ, ПАТЕНТАМ И ТОВАРНЫМ ЗНАКАМ (12) ЗАЯВКА НА ИЗОБРЕТЕНИЕ (21)(22) Заявка: 2009124480/03, 28.11.2007 (71) Заявитель(и): БЕРТОЛЬД Херманн (DE) Приоритет(ы): (30) Конвенционный приоритет: 28.11.2006 DE 102006056480 ...

Methods for gasification of carbon-containing materials

FIELD: oil and gas industry. SUBSTANCE: this invention is referred to the method for gasification of carbon-containing materials with production of synthetic gas. The method for gasification of carbon-containing materials in gas generator includes loading of carbon-containing materials to gas generator, delivery of gas containing molecular oxygen, delivery of gaseous carbon dioxide and water optionally; at that total quantity of supplied oxygen varies from 0.75 up to 3.0 pounds per pound of total quantity of carbon loaded to gas generator; thereat in gas generator carbon-containing ash is received, and the above ash contains less than 10% of carbon; and gas containing carbon monoxide, hydrogen and tar is generated; further the above gas is treated at temperature of 954-1927°C in presence of molecular oxygen with generation of raw synthetic gas containing carbon monoxide, hydrogen and carbon in synthetic gas. The produced raw synthetic gas contains less than 8 g of carbon in synthetic gas per standard cubic meter of the produced raw synthetic gas. EFFECT: invention allows development of method for synthetic gas manufacturing with maximum generation of energy or chemical products at maintained low quantity of unreacted carbon and carbon black in crude synthetic gas and carbon in ash. 8 cl, 10 dwg, 2 tbl РОССИЙСКАЯ ФЕДЕРАЦИЯ (19) RU (11) (13) 2 570 879 C2 (51) МПК C10J 3/16 (2006.01) C10J 3/00 (2006.01) C10J 3/72 (2006.01) C12P 7/06 (2006.01) ФЕДЕРАЛЬНАЯ СЛУЖБА ПО ИНТЕЛЛЕКТУАЛЬНОЙ СОБСТВЕННОСТИ (12) ОПИСАНИЕ (21)(22) Заявка: ИЗОБРЕТЕНИЯ К ПАТЕНТУ 2012147911/05, 11.04.2011 (24) Дата начала отсчета срока действия патента: 11.04.2011 (72) Автор(ы): СУТРАДХАР Бхагиа Чандра (US), КО Чин-Ван (US) (73) Патентообладатель(и): ИНЕОС ЮЭсЭй ЭлЭлСи (US) Приоритет(ы): (30) Конвенционный приоритет: (43) Дата публикации заявки: 20.05.2014 Бюл. № 14 R U 13.04.2010 US 12/798,871 (45) Опубликовано: 10.12.2015 Бюл. № 34 (85) Дата начала рассмотрения заявки PCT на национальной фазе: 13.11. ...

Carbonaceous fuel, particularly gasification of coal

在外加热的沸腾层反应器中，煤的气化所产生 的合成煤气经除尘脱硫后，一部分被燃烧，作为热源 通过间接热交换加热反应器，也可产生为气化所必 需的蒸汽。从反应器热交换器中出来的废气可用作 减压涡轮机的工作能。剩余的合成煤气作为有用煤 气应用于例如还原铁矿石、燃烧或者应用于气体涡 轮机中作为发电用的工作能。这种方法既有利于环 境保护，同时比直接燃烧煤或自热的煤气化法有更 高的效率，也不象已知的外热煤气化法那样需要核 能之类的外界能量。