WO2024088822A1 - Procédé de production de gaz de synthèse et réacteur - Google Patents

Procédé de production de gaz de synthèse et réacteur Download PDF

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Publication number
WO2024088822A1
WO2024088822A1 PCT/EP2023/078771 EP2023078771W WO2024088822A1 WO 2024088822 A1 WO2024088822 A1 WO 2024088822A1 EP 2023078771 W EP2023078771 W EP 2023078771W WO 2024088822 A1 WO2024088822 A1 WO 2024088822A1
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WO
WIPO (PCT)
Prior art keywords
wall
reactor
slag
steam
raw gas
Prior art date
Application number
PCT/EP2023/078771
Other languages
English (en)
Inventor
Eero Berg
Rauno Peippo
Original Assignee
Sumitomo SHI FW Energia Oy
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
Application filed by Sumitomo SHI FW Energia Oy filed Critical Sumitomo SHI FW Energia Oy
Publication of WO2024088822A1 publication Critical patent/WO2024088822A1/fr

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Classifications

    • 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
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/02—Dust removal
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
    • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
    • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/22—Non-catalytic cracking in the presence of hydrogen
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G47/00—Cracking of hydrocarbon oils, in the presence of hydrogen or hydrogen- generating compounds, to obtain lower boiling fractions
    • C10G47/36—Controlling or regulating
    • 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
    • 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
    • C10J3/52—Ash-removing devices
    • 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
    • C10J3/723—Controlling or regulating the gasification process
    • 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
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K1/00—Purifying combustible gases containing carbon monoxide
    • C10K1/04—Purifying combustible gases containing carbon monoxide by cooling to condense non-gaseous materials
    • C10K1/046—Reducing the tar content
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10K—PURIFYING OR MODIFYING THE CHEMICAL COMPOSITION OF COMBUSTIBLE GASES CONTAINING CARBON MONOXIDE
    • C10K3/00—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide
    • C10K3/001—Modifying the chemical composition of combustible gases containing carbon monoxide to produce an improved fuel, e.g. one of different calorific value, which may be free from carbon monoxide by thermal treatment
    • C10K3/003—Reducing the tar content

Definitions

  • the present invention relates to a method for production of synthesis gas.
  • the present invention relates also to a reactor for processing of synthesis gas by partial oxidation from a raw gas containing carbon and sticky components.
  • High temperature gasification can be used to produce raw gas for power production and various chemical production plants. Many companies are developing high temperature gasification reactors to produce raw gas for further production of synthesis gas (syngas) and further liquid fuels, using feed stocks like pyrolysis oil, torrefied wood, peat and wood dust. The aim of these processes is thus to use carbon containing feed stock to produce purified gas to a given purpose. Ash, soot and tar are among the components that need to be purified away from the gas.
  • the syngas produced by primary gasification may contain significant amounts of unreacted higher molecular weight hydrocarbons which can be problematic for downstream equipment.
  • problematic hydrocarbons are those commonly denoted as “tars” that condense in downstream equipment potentially causing operational and efficiency issues.
  • These problematic hydrocarbons can be further processed by secondary gasification of the hy- drocarbon-containing syngas from a primary gasifier.
  • This configuration is similar to a primary gasifier except that the feedstock to the secondary gasifier includes, at least in part, the crude syngas from the primary gasifier.
  • a secondary gasifier may be used with feedstocks generated from hydrocarbon processing, such as refinery off gas (that is, crude syngas is not necessarily generated from a gasification process).
  • liquid alkali metal compounds Na and K as oxides, carbonates, hydroxides, chlorides, etc
  • ash will block the reactor.
  • tar removal is needed in fluidized bed gasification processes when aiming at very clean gas for various synthesis applications.
  • a prior art document US 7587995 B2 shows a synthesis gas cooler for extracting heat from synthesis gas produced by a gasification process.
  • the synthesis gas cooler comprises a shell having a synthesis gas inlet and a synthesis gas outlet; a fluid-cooled flue contained within the shell for receiving the synthesis gas: fluid-cooled radiant heat transfer surface is partially extending within the flue for cooling the synthesis gas; and means for conveying the synthesis gas from the outer flue to the outlet.
  • the main objective in the disclosure is to transfer heat from the synthesis gas so that the ash has a reduced tendency to stick to the cooling tubes and cause deposition and plugging.
  • the document explains that the heat transfer surface design should be based on achieving the required absorption without the use of soot blowers to clean the heat transfer surface of deposits which will accumulate during operation.
  • the document explains that based upon experience at current gasification units, an equilibrium fouling and absorption rate is achieved over time. It is noted that such equilibrium conditions are also attained in industrial and utility boilers firing similar fuels, and the performance of such boilers is quite manageable. Experiences indicates that due to slag buildup on sootblowers during service, penetration of corrosive gases, and breakdown of seal systems in-gas stream, removable sootblowers are unacceptable from a practical maintenance and availability standpoint.
  • the document discloses cooled hanging partition walls within a gas cooler enclosure to maintain desired cooling of gas without cleaning the partition walls by soot blowers.
  • Document WO2012085345 A1 discloses (paragraph [0040]; claims 1 , 9; figure 1) a method of gasifying solid fuel in a gasification reactor (12, 12'), where the product gas is partially oxidized and its temperature is increased, whereby thermal cracking of the components of the product gas is achieved.
  • Document discloses that when the gas is cooled down with a radiation heat exchange cooler (41), softened and/or melt fly ash sticks to a certain extent also to the walls of the lower portion of the gas treatment reactor (20) and solidifies to the surface thereof.
  • rapping hammer type soot blowers (44) are preferably provided in connection with the walls of the lower portion of the gas treatment reactor, by means of which material solidi9ed and accumulated on the walls can be removed.
  • Document US7037473 B1 discloses (abstract; column 3, lines 15-55; claim 1) a gasification reactor for the gasification of carbon- and ash-containing fuel, residual and waste materials using an oxygen-containing oxidizing agent.
  • a cooling gap (5) filled with water.
  • the cooling gap (5) is delimited by a cooling wall (4).
  • the liquid slag which forms in the reactionchamber (1) is cooled on the cold surface of the cooling wall (4).
  • Its protective layer so- lidifes and forms a refractory lining as a layer of slag which grows toward the reaction chamber 1 until the temperature has reached the melting point of the slag.
  • the further slag which is then ejected runs of as a film of slag and is discharged together with the hot crude gas via the opening (8).
  • Document US2010143216 A1 discloses (WPI abstract; paragraph [0034]) a reactor vessel for preparing syngas having a chamber linked to diptube via slap tap that has tubular part connected to opening of frusto-conical part of chamber, where half of vertical length of tubular part extends below discharge opening.
  • the frusto-conical part predicts blockage by the slag by measuring the temperature of the used cooling water or steam make in conduits of the frusto-conical part, and indicates decrease in temperature of the used cooling water or decrease in steam for a growing layer of the slag.
  • operating the reactor vessel closer the optimal gasi9cation temperature while simultaneously monitoring the slay layer thickness to minimize blocking risk by the slag is disclosed.
  • An object of the invention is to provide a method for production of synthesis gas in which the performance is considerably improved compared to the prior art solutions.
  • Another object of the invention is to provide a method wherein residual substances and particles can be removed from a raw gas easily and effectively.
  • An object of the invention is to provide a reactor for processing of synthesis gas by partial oxidation from a raw gas containing carbon and sticky components.
  • An embodiment of the present invention is a method for production of synthesis gas, the method comprising following steps:
  • the reactor comprises temperature-controlled inner wall and an outer wall, being arranged in a coaxial configuration in respect to each other and where the inner wall comprises a number of water tube panel walls on a suspended support and the outer walls being fixed wall,
  • the slag/dust layer is being continuously and/or intermittently determined and maintained such that when the slag/dust layer thickness has accumulated to a predetermined value, the slag/dust layer is dropped to the bottom of the reactor by rapping at least one of the inner panel walls at a time.
  • Another embodiment of the invention is a reactor for processing of synthesis gas by partial oxidation from a raw gas containing carbon and sticky components, the reactor comprising:
  • At least one second intake passage for controllably feeding steam and oxygen such that oxygen and steam are capable of reacting with portion of said raw gas to rise the temperature to enable melt of ash and crack of hydrocarbon compounds of the sticky components, and reactions occurring free of catalyst for cracking of sticky components are capable of being driven by hydrogen of the steam to crack complex hydrocarbons into lighter volatile hydrocarbon fractions,
  • an inner wall assembly configured on suspended support inside the outer wall and the inner wall being formed of a number of temperature-controlled water tube panel walls
  • At least one rapping device is arranged at an upper part of the inner wall for removal of a slag/dust layer on the inner wall.
  • the reactor utilizes the method to treat raw gas that contains carbon compounds and sticky components for processing of the raw gas by partial oxidation wherein oxygen and steam is added to the raw gas stream.
  • oxygen and steam reacts with portion of said raw gas to rise the temperature to enable melt of ash and crack of hydrocarbon compounds of the sticky components.
  • the temperature should be in a range of 1100 to 1400 °C to melt ash and crack tar.
  • a gasifier upstream of the reactor may be operated at a regular lower temperature to avoid issues with alkali and other corrosive components.
  • the raw gas produced in the gasifier and entering the reactor contain sticky components such as tar.
  • the aim of the present process is to maintain a controlled accumulation of residuals forming a protective slag/dust layer on the reactor walls, in the temperature range where the tars of the raw gas will be decomposed. Too thick slag/dust layer causes plugging of the temperature-controlled walls and thus preventing controllability of the process. Plugging of the reactor is prevented by rapping the inner walls that captures the slag/dust. However, formation of the slag/dust layer is essential to the process, otherwise raw gas purification does not happen and gas separation following the reactor will deteriorate.
  • the accumulation is targeted especially on the inner wall assembly configured on suspended support inside the outer wall and the inner wall being formed of a number of temperature-controlled water tube panel walls, here such a single hanging sector, section or panel of the inner wall is called as an inner panel wall.
  • the temperature of surfaces where slag/dust is to be accumulated during operation should be the following:
  • Temperature in the reactor may advantageously controlled so that the reactor has a low corrosion rate below 1 millimeter per annum when exposed to any liquid alkali metal, sulphur or chlorine compounds, while the crack of hydrocarbon compounds of the sticky components is still the primary factor for process temperature within the reactor.
  • the first ash will deposit onto the inner wall as solid, and as the deposit will grow its surface will be increasingly softer as its temperature will be closer to the gas temperature.
  • the deposit growth will be interrupted by rapping the inner panel walls in certain time interval, requiring collect of the deposit from the bottom of the reactor.
  • the thickness of the protective slag/dust layer is being continuously and/or intermittently determined and maintained such that when the slag/dust layer thickness has accumulated to a predetermined value, the slag/dust layer is dropped to the bottom of the reactor by rapping at least one of the inner panel walls at a time.
  • the cleaning action of the hammer rely on the fact that the slag/ash in direct contact with the panel surface (200 - 350 °C) will be solid. It can be rapped off and down to the bottom of the reactor I hopper only at the boundary layer between deposit and inner wall when the boundary layer temperature is cooled enough. Rapping breaks the bond and drops the deposits in lumps/sheets which are bulky enough not to have time to melt again while falling down to the hopper. Immediately after the rapping, a new slag/dust layer starts to accumulate on the surfaces of the inner wall.
  • the rapping device is a spring hammer.
  • the spring hammer based technology has found to be the most efficient one in this solution.
  • the inner wall comprising a number of inner panel walls are of hanging type and cleaned by spring hammers. This is very efficient also in operation, if needed, the changing of hanging inner walls is easy and not very time consuming.
  • the most time-consuming part is a cooling down procedure of the reactor so that the reactor or possibly its enclosure, heat shield, pressure shell or like can be safely opened.
  • One objective of the present invention is to produce synthesis gas that fits easily to various following processes. If the gasification temperature in the reactor is under melting temperature of the ash, but over 1100 °C, the ash will become soft or become to hemispherical state. If the chemical composition of ash is on the area of more alkaline, the ash won't totally melt in the reactor when the gasification temperature is under 1400 °C. According to the experiments on the invention, the gasification temperature range of 1100°C - 1300°C is suitable for producing low tar containing gas. That brings one desired property, the produced synthesis gas by the method can be cooled down to +5°C - +20°C without problems.
  • Rectisol-process This physical wash will remove CO2 and sour gases from synthesis gas quite well. It is commonly known that Rectisol-process is a physical wash that may handle many hydrocarbons (ex. methane) and i.e. a small amount of tars in the gas are no problem in the Rectisol-process.
  • the thickness of the protecting layer of the slag/dust on inner walls of the reactor is controlled by rapping the inner walls in sequence so that the temperature of the water/steam inside the inner walls is maintained within desired range.
  • the thickness of slag/dust layer is determined by calculation based on temperature difference between ingoing and outcoming water/steam of the inner panel walls.
  • the slag/dust layer is dropped to the bottom of the reactor by rapping each one of the inner panel walls at a predetermined time interval.
  • the intention for this action is that when the slag/dust layer is dropped to the bottom of the reactor by rapping only one or part of the inner panel walls at a predetermined time interval, the accumulation in other inner panel walls is still in another phase of the cycle.
  • the accumulation time for fully grown slag/dust layer is one hour and there are six separate inner panel walls, it gives a theoretical interval of ten minutes to rapp one inner panel wall while the other inner panel walls are at different state of accumulation. This makes the process much more stable when not all the inner panel walls are rapped at the same time.
  • the cracking of sticky components in the reactor is being kept in balance. Also part of possible alkali metal, sulphur and/or chlorine components are being removed from the process as attached to the slag/dust.
  • the accumulation of the slag/dust layer is not necessarily linear but it can as well be logarithmic or exponential depending on the process parameters. Therefore, it is advisable to have different tools to decide on the time interval for rapping the inner walls.
  • the controlling of the insulating thickness or value or mass is one of those possible tools.
  • the outer wall is in a fixed configuration defining an internal space.
  • the outer wall being formed of a number of temperature-controlled water tube panel walls.
  • the outer wall is being formed of 6, 7, 8, 9, or more water tube panel walls having substantially planar cross section and joined together to form a continuous array of panels.
  • the outer wall is gas tight.
  • the inner wall assembly is configured on suspended support inside the outer wall and the inner wall being formed of a number of temperature-controlled water tube panel walls, here referred as inner panel walls.
  • inner panel walls Preferably the inner wall is being formed of 6, 7, 8, 9, or more inner panel walls having substantially planar cross section.
  • Each inner panel wall is hanging on its own suspended support and thus forming an array of inner panel walls.
  • the inner wall is having the same number of inner panel walls as the outer wall.
  • the inner wall and the outer wall are temperature controllable by means of fluid temperature inside the inner and outer walls.
  • Water and steam are among the most suitable fluids for controlling the temperature of the inner walls and outer walls.
  • Those water I steam -based control systems are well-known in the industry so there is less effort needed to adapt an existing control system for this purpose.
  • the reactor is inside an enclosure that is formed as a pressure shell.
  • the outer wall as such may be sufficient to form the closed space inside the reactor.
  • the outer wall inside the enclosure is in a fixed configuration defining an internal space and the outer wall being formed of a number of temperature-controlled water tube panel walls, the enclosure surrounds outside the outer wall.
  • the inner wall forms the innermost array of panels
  • the outer wall is in the middle and the enclosure forms the outermost layer.
  • the coaxial configuration is such that a normal of the inner wall is substantially perpendicular to the imaginary vertical axis of the reactor.
  • the reactor should be heat insulated in a way or another so that it would be feasible to have those operational temperatures inside the reactor without significant heat losses.
  • the inner wall is shorter than the outer tube panel wall. This has the effect that the inner panels are easy to rap and there are enough room below the inner wall for the slag/dust layer to be dropped.
  • FIG. 1 illustrates a reactor according to an embodiment of the invention
  • FIG. 1a, 2b and 2c illustrates some details of the reactor according to another embodiment of the invention
  • FIG. 3 illustrates an application of the present invention in a larger context of synthesis gas production.
  • Figure 1 depicts schematically a reactor 1 for processing of synthesis gas by partial oxidation from a raw gas containing carbon and sticky components, the reactor comprising:
  • At least one rapping device 8 is arranged at an upper part of the inner wall 3 for removal of a slag/dust layer on the inner wall 3,
  • the hopper 71 has an inclined surface that leads the condensed and/or solidified material to the proximity of the second exhaust passage 7.
  • the second exhaust passage 7 has a gas-tight dual hatch arrangement (not shown in figures) that enables collecting the condensed and/or solidified material during continuous operation of the reactor 1. In that kind of dual hatch arrangement one of the hatches is always closed, meaning that both hatches are not open simultaneously during operation, so there is no direct connection from inside the reactor 1 to the atmosphere.
  • Figure 2a depicts schematical side view of a reactor 1 for processing of synthesis gas by partial oxidation from a raw gas containing carbon and sticky components.
  • Figure 2b depicts a cross-section of the reactor of Fig. 1 at A - A and
  • Fig. 2c depicts an enlarged view of encircled detail of Fig. 2b.
  • the reactor 1 comprises:
  • the enclosure 10 may formed as a pressure shell or as a thermal insulation
  • the panels may preferably be arranged as a continuous array as depicted in Fig. 2b and Fig. 2c,
  • the suspended support 32 enables the inner panel walls 31 to vibrate or swing when rapped,
  • At least one rapping device 8 is arranged at an upper part of the inner wall 3 for removal of a slag/dust layer on the inner wall 3.
  • the interior of the reactor is made of water/steam-cooled tube wall panels according to the exemplar embodiments shown on Figs. 2a, 2b and 2c.
  • the inner wall and outer wall may comprise e.g. 12 separate sections of wall panels, here called as outer panel wall 21 and inner panel wall, 31.
  • the width of each panel section may be for example 0.6 m and height 5 m.
  • Each panel section will be separately cleanable by spring hammer rapping.
  • the inner panel walls 31 forming the inner wall 3 are fast and easily replaceable as these can be formed as modular spare parts.
  • the construction is made of water tubes 310, 210 having a welded fin in between each water tube 310 to 310 or 210 to 210.
  • the inner wall 3 may be formed of 6, 7, 8, 9, or more inner panel walls 31 having substantially planar cross section.
  • the outer wall 2 is being formed of 6, 7, 8, 9, or more outer panel walls 21 having substantially planar cross section.
  • the inner wall 3 is having the same number of panels 31 as the outer wall 2 so that the spacing between the inner wall and the outer wall remains about the same or equal around the circumference of the inner wall 3/ outer wall 2.
  • the reactor 1 may be dimensioned according to following example.
  • Cooling water/steam temperature is 250 °C
  • the total temperature controlled wall area is 40 m 2
  • the area of one water tube panel wall section is 5,5 m 2 .
  • FIG. 3 it is presented an exemplary embodiment of the present reactor 1 and method as claimed herein as a part of a larger production chain of synthesis gas.
  • gasifier Upstream of the reactor there are gasifier delivering the raw gas, then there are sources for oxygen and steam. These are combined in the reactor as explained here earlier.

Abstract

L'Invention concerne un procédé de production de gaz de synthèse qui comprend les étapes suivantes consistant à : fournir un gaz brut qui contient des composés de carbone et des composants visqueux à un réacteur (1) pour le traitement du gaz brut par oxydation partielle, de l'oxygène et de la vapeur étant ajoutés au flux de gaz brut ; mettre en réaction de l'oxygène et de la vapeur avec une partie dudit gaz brut afin d'augmenter la température pour permettre la fusion de cendres et le craquage des composés hydrocarbonés des composants collants ; et déterminer et maintenir l'épaisseur de la couche de laitier/poussière de protection par intermittence de telle sorte que lorsque l'épaisseur de ladite couche de laitier/poussière s'est accumulée à une valeur prédéterminée, la couche de laitier/poussière est lâchée vers le fond du réacteur (1) par frappage d'au moins l'une des parois de panneau interne (31) à la fois. L'invention concerne également un réacteur correspondant (1).
PCT/EP2023/078771 2022-10-25 2023-10-17 Procédé de production de gaz de synthèse et réacteur WO2024088822A1 (fr)

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FI20225958 2022-10-25
FI20225958A FI20225958A1 (fi) 2022-10-25 2022-10-25 Menetelmä synteesikaasun valmistamiseksi ja reaktori

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WO2024088822A1 true WO2024088822A1 (fr) 2024-05-02

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WO2012085345A1 (fr) 2010-12-20 2012-06-28 Foster Wheeler Energia Oy Dispositif et procédé de gazéification de combustible solide
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EP4026886A1 (fr) * 2021-01-06 2022-07-13 GIDARA Energy B.V. Procédé et appareil de production de gaz de synthèse par la conversion thermochimique de biomasse et de déchets de matériaux

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB2106931A (en) * 1981-09-22 1983-04-20 Steinmueller Gmbh L & C Cooling and purifying gases
US4841917A (en) * 1987-07-31 1989-06-27 L. & C. Steinmuller Gmbh Radiation cooling unit for cooling dust-laden gases
US5980858A (en) * 1996-04-23 1999-11-09 Ebara Corporation Method for treating wastes by gasification
US7037473B1 (en) 1998-07-01 2006-05-02 Future Energy Gmbh Device for gasifying combustible materials, residues and waste materials containing carbon
US7587995B2 (en) 2005-11-03 2009-09-15 Babcock & Wilcox Power Generation Group, Inc. Radiant syngas cooler
US20100263278A1 (en) * 2007-09-18 2010-10-21 Uhde Gmbh Gasification reactor and process for entrained-flow gasification
US20100143216A1 (en) 2008-12-04 2010-06-10 Ten Bosch Benedict Ignatius Maria Reactor for preparing syngas
WO2012085345A1 (fr) 2010-12-20 2012-06-28 Foster Wheeler Energia Oy Dispositif et procédé de gazéification de combustible solide
CN108410510A (zh) * 2018-06-11 2018-08-17 宁夏神耀科技有限责任公司 一种废锅除灰一体式煤气化炉
EP4026886A1 (fr) * 2021-01-06 2022-07-13 GIDARA Energy B.V. Procédé et appareil de production de gaz de synthèse par la conversion thermochimique de biomasse et de déchets de matériaux

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