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WO1993024704A1 - Procede de recuperation de produits chimiques et d'energie dans des liqueurs de cellulose epuisees - Google Patents

Procede de recuperation de produits chimiques et d'energie dans des liqueurs de cellulose epuisees Download PDF

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Publication number
WO1993024704A1
WO1993024704A1 PCT/SE1993/000212 SE9300212W WO9324704A1 WO 1993024704 A1 WO1993024704 A1 WO 1993024704A1 SE 9300212 W SE9300212 W SE 9300212W WO 9324704 A1 WO9324704 A1 WO 9324704A1
Authority
WO
WIPO (PCT)
Prior art keywords
gas
process according
compressed air
steam
gas turbine
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
Application number
PCT/SE1993/000212
Other languages
English (en)
Inventor
Lars Stigsson
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Chemrec AB
Original Assignee
Chemrec AB
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from CA002136817A external-priority patent/CA2136817A1/fr
Application filed by Chemrec AB filed Critical Chemrec AB
Priority to EP93909103A priority Critical patent/EP0642612A1/fr
Priority to FI945603A priority patent/FI945603A0/fi
Priority to BR9306444A priority patent/BR9306444A/pt
Publication of WO1993024704A1 publication Critical patent/WO1993024704A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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Classifications

    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/12—Combustion of pulp liquors
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/12—Combustion of pulp liquors
    • D21C11/125—Decomposition of the pulp liquors in reducing atmosphere or in the absence of oxidants, i.e. gasification or pyrolysis
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K21/00—Steam engine plants not otherwise provided for
    • F01K21/04—Steam engine plants not otherwise provided for using mixtures of steam and gas; Plants generating or heating steam by bringing water or steam into direct contact with hot gas
    • F01K21/047—Steam engine plants not otherwise provided for using mixtures of steam and gas; Plants generating or heating steam by bringing water or steam into direct contact with hot gas having at least one combustion gas turbine
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K23/00—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids
    • F01K23/02—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled
    • F01K23/06—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle
    • F01K23/067—Plants characterised by more than one engine delivering power external to the plant, the engines being driven by different fluids the engine cycles being thermally coupled combustion heat from one cycle heating the fluid in another cycle the combustion heat coming from a gasification or pyrolysis process, e.g. coal gasification
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C1/00—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid
    • F02C1/04—Gas-turbine plants characterised by the use of hot gases or unheated pressurised gases, as the working fluid the working fluid being heated indirectly
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C3/00—Gas-turbine plants characterised by the use of combustion products as the working fluid
    • F02C3/20—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products
    • F02C3/26—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension
    • F02C3/28—Gas-turbine plants characterised by the use of combustion products as the working fluid using a special fuel, oxidant, or dilution fluid to generate the combustion products the fuel or oxidant being solid or pulverulent, e.g. in slurry or suspension using a separate gas producer for gasifying the fuel before combustion
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/16—Combined cycle power plant [CCPP], or combined cycle gas turbine [CCGT]
    • Y02E20/18—Integrated gasification combined cycle [IGCC], e.g. combined with carbon capture and storage [CCS]
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P70/00—Climate change mitigation technologies in the production process for final industrial or consumer products
    • Y02P70/10—Greenhouse gas [GHG] capture, material saving, heat recovery or other energy efficient measures, e.g. motor control, characterised by manufacturing processes, e.g. for rolling metal or metal working

Definitions

  • the kraft process is currently the dominant chemical pulping process. During pulping large quantities of recoverable energy in the form of black liquor are generated. Worldwide some 2.8 billion GJ (780 TWh) of black liquor was produced in 1990 at kraft pulp mills.
  • the kraft recovery system has two principal functions:
  • the chemical recovery process contributes significantly to the capital intensity of the kraft process. About 35% of the capital cost of a modern pulp mill is attri ⁇ butable to the recovery process.
  • the present invention relates to a major improvement in this area, using technology based on gasification and energy recovery in an externally fired gas turbine cycle (EFCC) .
  • EFCC externally fired gas turbine cycle
  • Gasification of black liquor can be performed at various temperatures and pressures, resulting in different forms of the recovered inorganic constituents and different calorific values of the combustible process gas.
  • the inorganics mainly alkali compounds, are withdrawn from the gasification system and solubilized to form an aqueous alkaline liquid, which liquor is used for cooking liquor preparation.
  • Kraft pulp mills are significant producers of biomass energy, and today most mills are designed to use the biomass fuel available at the kraft mill to meet on site steam and electricity needs via back pressure steam turbine cogeneration system. Electricity demand is often higher than internally generated, in particular for integrated mills, and often electricity is imported from the grit.
  • Process steam requirements for a modern kraft pulp mill is in the order of 10 GJ per ton of air dried pulp.
  • the internal electricity demand is around 600 kWh/ton of air dried pulp.
  • the biomass gasification gas turbine cogeneration system of the present invention will meet mill steam demand and has the potential to produce excess electricity for export.
  • the present invention can be practised using various types of gas generators and gasification principles, exemplified in prior art documents.
  • the combustible gas is used for generating steam or as a synthesis gas.
  • the steam turbine is of back pressure type, preferably selected to fit the needs of process steam for the mill.
  • WO 91/15665 In WO 91/15665 is described a method and apparatus for generation of electricity and steam from a pressurized black liquor gasification process. Energy is recovered in a gas turbine/back pressure steam turbine system. Excess steam generated in the mill is recirculated into the gas turbine or the combustor thereof for increasing the generation of electricity. This procedure is known to the industry as a steam injected gas turbine, herein ⁇ after referred to as STIG.
  • the objective of the present invention is to provide a safe, efficient and less capital intensive process for production of electric power and process steam from gasification of black liquor, based on energy recovery in an externally fired gas turbine cycle with indirect heating of the gas turbine motive fluid by counter- current heat exchange with hot gas generated during gasification.
  • a substantial portion of the alkali inorganics formed during the gasification are removed from the gas, which removed alkali is further processed to cooking liquors.
  • the relatively clean process gas from the gasifier is trans ⁇ ferred to an externally fired gas turbine system, in which gas turbine motive fluid steam or water is in ⁇ jected to increase motive fluid mass flow and provide better conditions for heat transfer in the heat ex ⁇ changer.
  • the principal use of the gas turbine exhaust in the present invention is as oxidant in the gasifier and/or for final oxidation of the process gas before entering into the heat exchanger.
  • Yet another method to exploit the heat content of turbine exhaust in the present invention is to raise superheated steam which is recirculated and injected in the compressed gas stream, thereby increasing motive fluid mass flow, see e.g US patent No 3,978,661.
  • Steam injection in biomass gasifier gas turbine cogeneration systems for forest product industry applications is for example described in PU/CEES Working Paper No 113 by Dr Eric Larson, Princeton, February 1990.
  • Indirect fired or externally fired gas turbine cycles are considerably less sensitive and can accept fuels of approximately the same quality as steam generators. Indirect cycles, currently under development for coal gasification applications, can accommodate a wide variety of conventional equipment. Advanced combustors and high temperature heat exchangers are commercially available or under development.
  • Stack gas recirculation to use all the cycle air for combustion can be attractive in indirect cycles, minimizing NO emissions and lowering capital cost.
  • a cellulose waste liquor containing hydrocarbonaceous material and inorganic alkali compounds is reacted with an oxygen containing gas in a free flow gas generator to produce a com ⁇ bustible gas.
  • the gas generator operates at a reaction zone temperature of between 600-1500 C and at a pressure of 1-100 bar.
  • molten inorganic particles compri ⁇ sing sodium and potassium compounds are formed, which molten particles are entrained in the gasflow as a combustion residue.
  • a large portion of the molten inorganics are separated from the hot gas stream in one ore more separate gas diversion and residue separation zones.
  • the first gas diversion and residue separation zone may be directly connected to the gas generator.
  • the hot raw gas stream comprising the molten inorganics undergoes a change in direction in the first separation zone, and is transferred to a second separation zone consisting of a staggered array of refractory tubes, acting as an impact separator.
  • the molten particles and slag pass through an outlet in the first gas diversion zone and drop by gravity into a pool, comprising an alkaline liquid.
  • a small stream of bleed gas of the hot gas stream from the reactor is passed through the outlet promoting the separation of slag from the diverted main gas stream.
  • the discharge of molten particles and slag in the first separation zone could preferably be arranged as a quench system including a cooled dip tube for directing the particle flow into the pool of alkaline liquid.
  • the second separation zone is located in the hot gas stream, acting as an impact separator for particles and slag entrained in the gas leaving the first separation zone.
  • Particle inertia tends to counteract the gas fluid drag forces which act to sweep the particles past separator tubes arranged in the gas stream.
  • Impact separators are quite effective for removing particles above a certain diameter, ranging from 5-50 microns.
  • the second separator thus acts as a slag screen.
  • the hot gas is directed to a slag collection zone before being decelerated to and passed through a ceramic filter.
  • Ceramic filters utilized for hot gas filtration of gas streams, will be exposed to a variety of conditions in addition to heat. Ceramic barrier filter devices currently under development and commercial use include candles, cross flow, tubes, bags and granual beds. Any of those alone or in combination may be used as final hot gas clean-up before entering the main heat exchanger, when practising the present invention.
  • the separated smelt particles and slag comprising alkali components are withdrawn from the separation zones and further processed to form cooking liquors.
  • the hot clean gas, leaving the last separation zone, is directed to a combustion zone, where the gas is com ⁇ busted in the presence of an oxygen containing gas, preferably part of the gas turbine exhaust.
  • the heating value of the process gas leaving the gas generator is dependent on the type and amount of oxidant used in the gas generator.
  • the use of air as oxidant results in that a large portion of the product gas consists of nitrogen, thus resulting in a gas with a rather low calorific value.
  • An important feature of the present invention is that sulfur compounds, introduced into the gasifier by the cellulose waste liquor or other sulfur containing streams entering the gasifier, is reduced to sulfides and furthermore that a large portion of these sulfides are bound into alkali.
  • Binding of sulfur into the alkali smelt is promoted by high temperature in the gasifier and low gasification pressure.
  • Addition of various forms of metal oxides, such as titandioxide, mangandioxide or calcium com ⁇ ponents to the reaction zone, may be employed to minimize formation of alkali carbonates and hydrogen sulfide formation during gasification.
  • the oxidant to fuel ratio in the gasifier has further ⁇ more to be adjusted to minimize formation of sulfates and sulfur dioxide.
  • a preferred operating range of the gasifier is at temperatures above about 800°C and a reactor pressure between 1 and 5 bar.
  • the oxidant air supply to the reactor should be kept below 95% of the stochiometrical value for complete oxidation of the incoming streams to the reactor and is normally in the range of 30-80 %.
  • the oxidant is pre ⁇ ferably parts of or all of the gas turbine exhaust.
  • a distinguishing feature of the present invention is the use of a heat exchanger, which transfers a large portion of the gas combustor exhaust energy to preheat gas turbine motive fluid.
  • the efficiency of the indirect exhaust fired cycle is directly related to the size and performance of the heat exchanger.
  • the heat exchanger in the hot zone must operate at very high temperatures beyond the practical range for today's metal technology.
  • the range of operating conditions in the indirect gas turbine cycle of the present invention is not as limited as those for the typical steam generation systems of conventional combined cycle power plants.
  • energy available from the combustion system for evapora ⁇ tion and superheating can be used to circumvent pinch point restrictions normally encountered in the waste heat steam recovery systems of combined cycle power plants.
  • the mass flow through the turbine can be increased by injecting water or steam into the gaseous stream entering the gas turbine.
  • the compressed air stream used as motive fluid in the gas turbine is cooled after compression by adding water to the air stream in a humidification tower, in which all or part of the in ⁇ jected water evaporates.
  • the dewpoint decides maximum water addition.
  • the humid compressed air is heated by heat exchange with process gas combustor exhaust.
  • the evaporative regeneration can be performed in one or more steps with humidification towers before the heat exchanger. By injection of water in the compressed air stream in this way, at least two objectives are reached. The resulting increased mass flow through the gas turbine increases power output and heat transfer conditions in the heat exchanger are improved.
  • Another specific advantage of the process of the present invention is that it can utilize low level heat from the discharged flue gases, a compressor intercooler or from the gasification process, or utilize low level heat from elsewhere in the mill to preheat water used for evaporation cooling of the compressed air and/or fuel gas, and hence improve overall efficiency.
  • Yet another method to increase power output when practi ⁇ sing the present invention is to inject steam into the gaseous stream entering the gas turbine or injection of steam into the gas turbine before expansion.
  • a disadvantage with water or steam injected cycles is that water added to the system is lost, if no method to recapture the vapor from the exhaust gas is used.
  • the water consumption for humidifcation is in the order of 0.1-0.8 kg water per kWh power and about twice as much for power efficient steam injection systems. In both cases the water has to be processed to boiler feed water quality.
  • the gas turbine cycle in the present invention can be integrated with a facility for production of de- mineralized water to be used for injection.
  • a demineralization plant could be based on various prin ⁇ ciples known from the sea water desalination industry. Demineralization plants based on distillation processes are most preferred for use in the present invention, since they can use heat from the exhaust stream direct or use surplus steam or low level heat from elsewhere in the mill.
  • a kraft market pulp mill produces 1070 ton/day bleached pulp, generating a black liquor flow of 1662 ton/day as dry solids.
  • the mill's internal steam requirement amounts to 112 ton 5 bar steam and 36 ton 13 bar steam. This steam is supplied from bark an hog fuel firing
  • Electricity consumption in the mill is 600 kWh/ton of pulp or 642 MWh/day.
  • the black liquor is fed to a gasification system inte ⁇ grated with an externally fired gas turbine plant.
  • the black liquor has the following data at the gasifier entrance:
  • the gasifier is operated at a pressure of 1,3 bar and a reaction zone temperature of 900°C. Air is extracted from the gas turbine exhaust stream and used as oxidant in the gasifier.
  • the smelt formed in the gasifier is separated from the hot process gas in a separation zone arranged in the bottom of the gasifier. Additional slag and particles are removed from the hot gas stream in a slag screen arranged at the gasifier exit.
  • the smelt from the gasifier have the following composi ⁇ tion (potassium calculated as sodium) :
  • the smelt comprising the alkali sulfides are withdrawn from the gasifier and used for preparation of cooking liquors.
  • the hot process gas is oxidized in a gas combustor in the presence of gas turbine exhaust gas.
  • the oxidized hot gas stream is directed to the shell side of a heat exchanger, exchanging heat to a compressed air stream used as motive fluid in the gas turbine.
  • Clean filtered air enters the compressor, where it is pressurized to approximately 1.2 MPa and a temperature of 361°C.
  • This air stream is humidified by injection of steam and directed to the tube side of the ceramic heat exchanger, where temperature is raised to 882 C.
  • This high temperature, pressurized air stream enters the gas turbine, where it expands and generates power.
  • the cooled shell side gas stream and excess turbine exhaust stream is directed to a waste heat steam genera ⁇ tor generating steam powering a condensing steam turbine plant.
  • the gas turbine have the following main design criteria:
  • the modern kraft mill often has hog and/or bark fired boilers or gasifiers integrated.
  • Other mills have natural gas available for various purposes, such as lime kiln fuel.
  • the present invention can be practised in combination with combustion or gasification of other gaseous and liquid hydrocarbon fuels available at the mill.
  • additional natural gas or biogas can be fired in a preburner in the compressed air stream increasing gas turbine inlet temperature and power output.
  • the same objective can be reached by blending the combustible gas from the gasifier with another hydrocarbonaceous fuel in the combustor ahead of the heat exchangers.
  • Yet another method to increase power output in the present invention is to inject high pressure steam in various locations in the gas turbine motive fluid and/or into the gas turbine.

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)
  • Treatment Of Water By Oxidation Or Reduction (AREA)

Abstract

L'invention se rapporte à un procédé de récupération de produits chimiques et d'énergie dans des liqueurs de cellulose épuisées par oxydation partielle de ladite liqueur de cellulose épuisée dans un générateur de gaz fonctionnant dans une plage de température de 600 à 1500 °C et à une pression de l'ordre de 1 à 100 bar. Ledit générateur génère un gaz combustible et des composés alcalins fondus, qui sont extraits du gaz combustible et utilisés pour la préparation de liqueurs de lessivage, dans laquelle une turbine à alimentation en gaz indirecte est utilisée.
PCT/SE1993/000212 1992-05-29 1993-03-11 Procede de recuperation de produits chimiques et d'energie dans des liqueurs de cellulose epuisees Ceased WO1993024704A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
EP93909103A EP0642612A1 (fr) 1992-05-29 1993-03-11 Procede de recuperation de produits chimiques et d'energie dans des liqueurs de cellulose epuisees
FI945603A FI945603A0 (fi) 1992-05-29 1993-03-11 Menetelmä kemikaalien ja energian saamiseksi talteen selluloosajäteliemestä
BR9306444A BR9306444A (pt) 1992-05-29 1993-03-11 Um processo para a recuperaçáo de compostos químicos e energia do licor residual da celulose

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
SEPCT/SE92/00363 1992-05-29
PCT/SE1992/000363 WO1993024703A1 (fr) 1992-05-29 1992-05-29 Procede de recuperation d'energie dans un gaz combustible
BR9207135A BR9207135A (pt) 1992-05-29 1992-05-29 Um processo para recuperar energia de um gas combustivel
CA002136817A CA2136817A1 (fr) 1992-05-29 1992-05-29 Procede de recuperation de l'energie dans un gaz combustible

Publications (1)

Publication Number Publication Date
WO1993024704A1 true WO1993024704A1 (fr) 1993-12-09

Family

ID=27160064

Family Applications (2)

Application Number Title Priority Date Filing Date
PCT/SE1992/000363 Ceased WO1993024703A1 (fr) 1992-05-29 1992-05-29 Procede de recuperation d'energie dans un gaz combustible
PCT/SE1993/000212 Ceased WO1993024704A1 (fr) 1992-05-29 1993-03-11 Procede de recuperation de produits chimiques et d'energie dans des liqueurs de cellulose epuisees

Family Applications Before (1)

Application Number Title Priority Date Filing Date
PCT/SE1992/000363 Ceased WO1993024703A1 (fr) 1992-05-29 1992-05-29 Procede de recuperation d'energie dans un gaz combustible

Country Status (6)

Country Link
EP (1) EP0642612A1 (fr)
AU (1) AU2321092A (fr)
BR (1) BR9207135A (fr)
CA (1) CA2136829A1 (fr)
FI (1) FI945603A0 (fr)
WO (2) WO1993024703A1 (fr)

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2946088A1 (fr) * 2009-05-26 2010-12-03 Inst Francais Du Petrole Systeme de production d'energie, notamment electrique, avec une turbine a gaz utilisant un combustible provenant d'un gazeifieur
WO2011020767A1 (fr) * 2009-08-21 2011-02-24 Krones Ag Procédé et dispositif de valorisation de la biomasse
US8561412B2 (en) 2009-08-21 2013-10-22 Krones Ag Method and device for converting thermal energy from biomass into mechanical work
US9334518B2 (en) 2013-03-08 2016-05-10 Xyleco, Inc. Array for processing materials
CN116164316A (zh) * 2022-12-30 2023-05-26 杭州老板电器股份有限公司 一种集成灶及其自清洗控制方法

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Publication number Priority date Publication date Assignee Title
EP0821135A1 (fr) * 1996-07-22 1998-01-28 N.V. Kema Production d'énergie au moyen d'un cycle combiné à gaz et au charbon
ES2154572B1 (es) * 1998-11-05 2001-10-01 Dalering Desarrollos Energetic Sistema con ciclo abierto de turbina de gas de combustion externa.
FI20002153L (fi) * 2000-09-29 2002-03-30 Kvaerner Pulping Oy Menetelmä ja sovitelma liotussäiliössä
EP1609958A1 (fr) * 2004-06-22 2005-12-28 Siemens Aktiengesellschaft Turbine à gaz avec compresseur et récupérateur
SE535117C2 (sv) * 2010-03-30 2012-04-17 Chemrec Ab Förgasning av sulfittjocklut
CN110219724A (zh) * 2019-06-10 2019-09-10 宁波大学 一种船舶尾气净化及余热回收系统和方法

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US4492085A (en) * 1982-08-09 1985-01-08 General Electric Company Gas turbine power plant
US4682985A (en) * 1983-04-21 1987-07-28 Rockwell International Corporation Gasification of black liquor
WO1991015665A1 (fr) * 1990-04-03 1991-10-17 A. Ahlstrom Corporation Procede et appareil servant a produire de la chaleur et de l'electricite dans un malaxeur de pate au sulfate

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Publication number Priority date Publication date Assignee Title
US4753068A (en) * 1987-01-15 1988-06-28 El Masri Maher A Gas turbine cycle incorporating simultaneous, parallel, dual-mode heat recovery

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4492085A (en) * 1982-08-09 1985-01-08 General Electric Company Gas turbine power plant
US4682985A (en) * 1983-04-21 1987-07-28 Rockwell International Corporation Gasification of black liquor
WO1991015665A1 (fr) * 1990-04-03 1991-10-17 A. Ahlstrom Corporation Procede et appareil servant a produire de la chaleur et de l'electricite dans un malaxeur de pate au sulfate

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2946088A1 (fr) * 2009-05-26 2010-12-03 Inst Francais Du Petrole Systeme de production d'energie, notamment electrique, avec une turbine a gaz utilisant un combustible provenant d'un gazeifieur
WO2011020767A1 (fr) * 2009-08-21 2011-02-24 Krones Ag Procédé et dispositif de valorisation de la biomasse
JP2013502526A (ja) * 2009-08-21 2013-01-24 クロネス アーゲー バイオマスを使用する方法および装置
US8561412B2 (en) 2009-08-21 2013-10-22 Krones Ag Method and device for converting thermal energy from biomass into mechanical work
US8621872B2 (en) 2009-08-21 2014-01-07 Krones Ag Method and device for utilising biomass
US9334518B2 (en) 2013-03-08 2016-05-10 Xyleco, Inc. Array for processing materials
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BR9207135A (pt) 1996-11-19
EP0642612A1 (fr) 1995-03-15
AU2321092A (en) 1993-12-30
WO1993024703A1 (fr) 1993-12-09
CA2136829A1 (fr) 1993-11-30
FI945603A7 (fi) 1994-11-28
FI945603L (fi) 1994-11-28
FI945603A0 (fi) 1994-11-28

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