EP2719747B1 - Procédé de gazéification de matières premières houillères, du coke et du charbon - Google Patents

Procédé de gazéification de matières premières houillères, du coke et du charbon Download PDF

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Publication number
EP2719747B1
EP2719747B1 EP13461551.7A EP13461551A EP2719747B1 EP 2719747 B1 EP2719747 B1 EP 2719747B1 EP 13461551 A EP13461551 A EP 13461551A EP 2719747 B1 EP2719747 B1 EP 2719747B1
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Prior art keywords
coal
homogeneous
oxygen
heterogeneous
gas
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EP13461551.7A
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German (de)
English (en)
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EP2719747A1 (fr
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Piotr Sarre
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/46—Gasification of granular or pulverulent flues in suspension
    • C10J3/48—Apparatus; Plants
    • C10J3/482—Gasifiers with stationary fluidised bed
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/721—Multistage gasification, e.g. plural parallel or serial gasification stages
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/80—Other features with arrangements for preheating the blast or the water vapour
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
    • C10J3/72—Other features
    • C10J3/82—Gas withdrawal means
    • C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2200/00—Details of gasification apparatus
    • C10J2200/09—Mechanical details of gasifiers not otherwise provided for, e.g. sealing means
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0913—Carbonaceous raw material
    • C10J2300/093—Coal
    • C10J2300/0936—Coal fines for producing producer gas
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
    • C10J2300/00—Details of gasification processes
    • C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
    • C10J2300/0953—Gasifying agents
    • C10J2300/0959—Oxygen

Definitions

  • the object of the invention is the gasification method of coal-bearing raw materials, char and coal, as well as the arrangement of the equipment conducting for this process for industrial synthesis gas (syngas) production.
  • Polish Patent No. 205483 where the method involves waste gasification at a temperature of 150-350°C, with air inflow to the reactor at flow rate of 200-400 m 3 /hr and an increase of air flow to 400-680 m 3 /hr at the end of gasification process to incinerate the gasification residue at a temperature of 550-850°C, and the injection of steam into the reactor at a pressure of 0.1-0.2 MPa to produce generator gas.
  • Patent application No. PL.381200 presents the method of energy production through waste gasification in which the waste, for instance, municipal solid waste is dumped into a shaft melting gasifier, dried counter-currently, gasified with the simultaneous melting of solid waste, after which liquid waste is removed and dust-laden crude gas is discharged from above, the water is cleaned and cooled and finally taken through the separation and electrostatic distribution zone. Then, the resulting gas is fed into a burner, or generally taken to generate energy.
  • the method is distinguished by the fact that hot raw gases discharged from the melting gasifier are taken to the hot gas and steam generator in which hot gas is mixed with steam and this mixture passes through a dual-rotor turbine driving the electrical generator, whereby the initial reaction takes place at the same time.
  • the pre-cleaned mixture of hot gas and steam is fed into the precipitation device in which, using water supplemented with the reactive agent suspension and repeatedly using expansion and compression combined with foaming, this mixture is cooled and pre-cleaned whilst the fluid is collected.
  • the pre-cleaned gas is taken to the gas filter in which the gas foams with the reactive agent, the foam is removed and, finally, the cleaned gases are brought to further energetic use, for example, for combustion in an engine.
  • the invention also encompasses a device for the production of energy from waste gasification.
  • Invention No. PL.161778 deals with the method and device for the gasification of solid fuels, especially fine-grained or dusty fuels, with the gasifying reactor equipped with gasifying burners, a device for separating volatile dust from crude gas, a volatile dust tank and a device for returning volatile dust to the gasifying reactor.
  • the gasifying burners are equipped with a primary oxygen supply channel, which is coaxial with respect to the burner axis and which surrounds the annular fuel supply channel and an annular secondary oxygen supply channel which surrounds this channel.
  • Volatile dust separated from raw gas is introduced into the axis of at least one stream of fuel/reactive medium, positioned with its assistance, in the primary reaction zone of the gasifying reactor and is melted in it.
  • the ratio of the mass of primary to secondary oxygen ranges between 1:1 and 1:4, favourably between 1:1 and 1:3.
  • the method of gasification of carbon-based materials known from the description of patent PL.164016 is characterized by the fact that carbon-based material, in a form of a stationary bed filling the corona reactor is subjected to the action of non-equilibrium plasma at atmospheric pressure and room temperature, whereby plasma is generated by a pulsed corona discharge, while CO 2 flows through the carbon-based material cocurrently or counter-currently with respect to flowing electrolyte solution in the cooler.
  • the device has a corona reactor filled with carbon-based material, containing an axially located corona electrode, while the outer part of the cooler is an external cylindrical electrode.
  • the corona electrode is connected to a device supplying power.
  • the method of continuous gasification of liquid hydrocarbons from the low temperature carbonization process in the carbonization gas stream before their condensation, using the mixture of oxygen and steam which is known from the description of patent No. PL.167505 , is characterized by the fact that the gasification process is conducted outside the low temperature carbonization device in the carbonization gas stream in a laminar flow occurring in the intergranular spaces of the packing in the counter-current shaft reactor.
  • the volatile liquid hydrocarbons contained in this stream are subjected to the pyrolysis process and then these pyrolysis products are gasified in the hydrothermic gasification reaction zone situated upstream, under which a gasifying agent is introduced.
  • the invention also includes the gasification reactor for liquid hydrocarbons.
  • the method of pyrolysis and gasification of waste materials is known from the description of patent No. PL.191219 .
  • These stages include the following processes: processed material is gasified at a temperature of between 1300 and 1500°C in a period of between 3 and 15 seconds and melts in a period of between 5 and 30 minutes, in the total absence of air, yielding a mixture of combustible, non-combustible and inert gases in at least two, sequentially conducted stages of gasification.
  • a constant temperature is maintained by applying at least one thermal lance in each of the gasification stages.
  • the mixture of combustible and non-combustible gases obtained in such a way is cleaned and undergoes energy recovery treatment. Then, the inert gases or a part of the inorganic and mineral substances are obtained in a vitrified state.
  • the reactor is divided into two sections:
  • the primary gasification chamber consists of a vertical cylinder with an opening or outlet in the middle of the said cylinder cover for charging with waste.
  • a place for introducing the thermal lance is always located in the upper part of the cylinder, but with a tangential clutch.
  • the lower part of the cylinder is tapered like a truncated cone, so as to connect the cylinder with the pipe connecting it to the secondary gasification and melting chamber.
  • the volume and length of the cylinder and pipeline specify the length of time in which waste remains in contact with the hot gases produced by the thermal lance and the surface of the fireproof coating which is kept at the anticipated operating temperature (1300-1500°C).
  • the gas flow produced in the primary gasification chamber creates a descending flow, which tangentially enters the secondary gasification and melting chamber, together with waste introduced for gasification and melting.
  • the secondary gasification and melting chamber consists of a vertical cylinder situated at a lower level with respect to the primary chamber.
  • the lower part of this cylinder constitutes a base or basin for melting the mineral waste residue.
  • the fireproof coating of the said base is oriented so as to obtain an inclination or slope of between 5 and 30%, with the best slope being 20%, between the highest point (gas inlet region from the previous chamber) and the lowest, diametrically opposite point (melted ash discharge region).
  • the length and slope of this track set the duration and melting of the gasification residue, respectively.
  • a second thermal lance is located on the cylinder wall of the secondary gasification and melting chamber, always near the base, having the task of maintaining the operating temperature in accordance with the set condition (1300-1500°C). Therefore, in addition to melting, gasification is conducted to the end and, since this happens in two successive stages, it features very high efficiency levels.
  • WO 2012/055012 A1 shows a reforming zone which is mostly homogeneous and a heterogeneous fluidized bed reaction zone.
  • hydrocarbons CH4, "residual gas”
  • the stream does also contain gaseous tar and small amounts of char and is therefore not 100% homogeneous but nevertheless the characteristics of this stream are more in line with a homogeneous stream than that of a heterogeneous stream, as it presents a gaseous fuel / oxygen mixture with small particles entrained in the flow that do not alter the reactivity of said stream.
  • a number of other inventions regarding the gasification process which are conducted using air, oxygen, steam or their mixtures, are also known.
  • the most common processes are those conducted in counter-current shaft reactors or fluidized bed reactors, as well as using air gasifying burners.
  • a fundamental issue of gasification is the minimization of the tar content in the final gas, the most complete possible carbon conversion and the least possible concentration of inert components in the gas.
  • the existing methods either have a high concentration of tar in the gas or a high level of inert components in the gas produced.
  • the method of achieving the gasification of coal-bearing raw materials, char and coal involves conducting it in the co-current system using a favourably turbulent gas flow.
  • the method according to the invention is implemented in a series of alternating homogeneous and heterogeneous reaction zones with a mixture of steam, hydrocarbon vapours and/or combustible gases, with the oxygen or oxygen with steam injection into the homogeneous reaction zone, which increases the temperature of the homogeneous zone to no higher than 1000°C, whereby fine-grained coal and coal-bearing raw material being the feed, best below 2 mm, is mechanically distributed throughout the heterogeneous reaction zone to ensure the continuous development of the contact surface dissipated in a form of solid-phase curtains with carbon dioxide and steam.
  • the gas temperature between successive heterogeneous reaction zones is raised to no higher than 1000°C via an oxygen or oxygen with steam injection and adjusted for each homogeneous reaction zone.
  • An amount of hydrocarbon and/or combustible gas vapours is added to the steam and oxygen mixture supplied to the first homogeneous reactor, which enables the temperature of all gases in this reactor to be raised to over at least 700°C, preferably up to 1000°C.
  • the gas obtains a favourably progressive rotational motion.
  • the solid-phase is dumped continuously from the shelves of the heterogeneous reactors, so that the dumping takes place from at least one shelf, but preferably from three shelves simultaneously.
  • the layout of the devices containing co-current homogeneous and heterogeneous reactors is set up in a number of pairs of homogeneous and heterogeneous reactors starting with the homogeneous reactor, whereby the solid phase and gases are moved between heterogeneous reactors along separate paths.
  • Such handling of the process enables the receipt of virtually tar-free synthesis gas, the expected conversion of carbon contained in the feed and the use of lower gasification temperatures, which decidedly restricts the carbon reduction of sulphates to sulphur dioxide and reduces the vapour pressure of any possible heavy metals.
  • the external energy needed to cover the energy deficiency of the reaction between carbon and carbon dioxide, and steam with carbon is supplied in doses by the physical heat of the gas emitted in the reaction of oxygen with the combustible components of the gas in volumes preceding gas contact with the solid phase containing elemental carbon.
  • Such action is more effective than shell heating of steam.
  • the array of devices in which gasification is conducted according to the invention starts with the chamber which is the homogeneous reactor, in which gases for the gasification process are autothermally heated.
  • fig. 1 shows the schematic diagram of the gasification system
  • fig. 2 presents an example of the horizontal projection of the layout of the shelves for the gasification reactor section with four rows of shelves situated every 90°
  • fig. 3 shows the axonometric view of the arrangement of the shelves in the heterogeneous reactor
  • fig. 4 presents coal with 40% ash content, taken from a municipal waste carbonization installation of an average granulation of 1.1 mm.
  • the heterogeneous system reaction chamber represents a rotational pipe device 3, favourably inclined in the direction of the movement of the solid phase and the gas, in which the intensity of contact of the phases is increased by the curtain-spreading of the fragmented solid phase in the system of shelves 4 attached helically to the reactor walls ( figs. 2 and 3 ). It is important for the dumping of the solid phase from the shelves to be continuous and that it takes place from at least one shelf, preferably from three shelves simultaneously.
  • Reactions take place in the heterogeneous co-current reactor between carbon and carbon dioxide producing carbon monoxide and between steam with carbon producing carbon monoxide and hydrogen. These reactions run because of the physical heat taken from the gas, the temperature of which declines in the direction of the movement of the phases.
  • the solid and the gas phases are separated at the end of the heterogeneous reactor.
  • the gas is fed to the next chamber of the homogeneous reactor, where it is heated to the technologically set temperature via the injection of a subsequent portion of oxygen and it again receives an advantageously rotational progressive motion.
  • the heated gas is fed to the next heterogeneous reactor, to which the solid phase from the previous heterogeneous reactor is added by different path to that of the gas, without coming into contact with oxygen.
  • the number of devices and their individual lengths are calculated as a function of the average temperature of the process that is planned for technological reasons and the required degree of carbon conversion of over 95%.

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  • Chemical & Material Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Organic Chemistry (AREA)
  • Processing Of Solid Wastes (AREA)
  • Solid Fuels And Fuel-Associated Substances (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)

Claims (4)

  1. Méthode de gazéification des matières carbonifères, biochars et charbons, à co-courant, le flux de gaz favorablement turbulent, caractérisée par la réalisation dans la suite des réactions dans des zones homogènes (1) et hétérogènes (2) alternativement, à l'aide d'un mélange de la vapeur d'eau, des vapeurs d'hydrocarbures et/ou des gaz combustibles, avec l'injection d'oxygène ou de mélange oxygène-vapeur d'eau dans des zones homogènes en quantité qui assure l'augmentation de la température dans la zone homogène jusqu'à moins que 1000°C pendant que la charge constituée par le charbon ou une matière carbonifère de dimension de préférence au dessous de 2 mm est distribuée mécaniquement dans la zone hétérogène de réaction assurant le développement continu de la surface de contact de la phase solide diffusée sous forme d'un rideau avec le dioxyde de carbone et la vapeur d'eau; la température du gaz entre des zones de réactions hétérogènes voisines est augmentée à moins que 1000°C par l'injection de l'oxygène ou du mélange oxygène-vapeur d'eau contrôlée pour chaque zone de réactions homogènes.
  2. Méthode, suite à la revendication 1, caractérisée par ce qu'au mélange vapeur d'eau-oxygène fourni dans le premier réacteur homogène est ajouté une quantité des vapeurs d'hydrocarbures et/ou gaz combustibles permettant atteindre la température de la totalité des gaz au dessus de 700°C et favorablement 1000°C dans ce réacteur.
  3. Méthode, suite à la revendication 1, caractérisée par ce qu'au gaz qui passe de la zone homogène à hétérogène on impose le mouvement rotatif et de translation qui est favorable.
  4. Méthode, suite à la revendication 1, caractérisée par ce que la descente de la phase solide des plateaux des réacteurs hétérogènes se fait d'une façon continue et que la descente se passe d'au moins un et profitablement de trois en même temps.
EP13461551.7A 2012-10-12 2013-10-07 Procédé de gazéification de matières premières houillères, du coke et du charbon Active EP2719747B1 (fr)

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PL401192A PL224212B1 (pl) 2012-10-12 2012-10-12 Sposób zgazowania surowców węglonośnych, karbonizatów i węgli oraz układ urządzeń do prowadzenia tego procesu

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EP2719747A1 EP2719747A1 (fr) 2014-04-16
EP2719747B1 true EP2719747B1 (fr) 2018-11-28

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Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4303415A (en) * 1980-09-29 1981-12-01 Lubille Energy Development Co., Ltd. Gasification of coal

Family Cites Families (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
PL111437B1 (en) 1976-12-17 1980-08-30 Przedsieb Wdrazania Upowszech Swine fattening method
CA1102131A (fr) * 1977-02-28 1981-06-02 Lionel S. Galstaun Traduction non-disponible
PL205483A1 (pl) 1978-03-20 1979-11-19 Poludniowe Zaklady Przemyslu E Tulejka chwytajaca urzadzenia do usuwania koncowki materialu pretowego w automatach tokarskich wzdluznych
DE3837587C1 (fr) 1988-11-05 1990-05-23 Krupp Koppers Gmbh, 4300 Essen, De
PL164016B1 (pl) 1990-10-23 1994-06-30 Univ Warszawski Sposób zgazowania materiałów węglopochodnych oraz urządzenie do stosowania tego sposobu
PL167505B1 (pl) 1992-05-11 1995-09-30 Inst Mineralnych Materialow Bu Sposób ciągłego zgazowania węglowodorów ciekłych z procesu wytlewania węgla i reaktor do stosowania tego sposobu
IT1313272B1 (it) 1999-07-29 2002-07-17 Rgr Ambiente Reattori Gassific Procedimento e dispositivo per la pirolisi e gassificazione di rifiuti
JP2009545636A (ja) * 2006-06-05 2009-12-24 プラスコエナジー アイピー ホールディングス、エス．エル．、ビルバオ、シャフハウゼン ブランチ 垂直な連続処理領域を含むガス化装置
DE102006056480B4 (de) 2006-11-28 2008-09-04 Berthold, Hermann Verfahren und Anlage zur Nutzenergiegewinnung durch Müllvergasung
US20090014689A1 (en) * 2007-07-09 2009-01-15 Range Fuels, Inc. Methods and apparatus for producing syngas and alcohols
US8636923B2 (en) * 2010-10-29 2014-01-28 Enerkem, Inc. Production of synthesis gas by heating oxidized biomass with a hot gas obtained from oxidation of residual products

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4303415A (en) * 1980-09-29 1981-12-01 Lubille Energy Development Co., Ltd. Gasification of coal

Also Published As

Publication number Publication date
PL224212B1 (pl) 2016-11-30
PL401192A1 (pl) 2014-04-14
EP2719747A1 (fr) 2014-04-16

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