JP5559532B2 - Gasification system and use thereof - Google Patents

Description

  The present invention relates to an improved gasification system for producing a mixture comprising carbon monoxide and hydrogen from a carbon-based stream using an oxygen-containing stream. This gasification system comprises a gasification reactor and a synthesis gas cooling vessel. The invention also relates to a method for producing a mixture comprising carbon monoxide and hydrogen in the system of the invention.

Syngas production methods are well known in the art. An example of a method for producing synthesis gas is described in EP-A-4000074. In general, a carbonaceous stream, such as coal, lignite, peat, wood, coke, firewood, or other gaseous, liquid or solid fuel or mixtures thereof, contains an oxygen-containing gas (eg, substantially pure oxygen or ( Partial combustion in a gasification reactor using air (optionally enriched in air, etc.), in particular to obtain synthesis gas (CO and H ₂ ), CO ₂ and slag. The slag formed during partial combustion falls and is discharged from an outlet located at or near the bottom of the reactor.

  The hot product gas in the reactor of EP-A-400740 flows upward. This hot product gas, ie raw synthesis gas, usually contains sticky particles, which lose their stickiness when cooled. These sticky particles in the raw syngas can cause problems downstream of the gasification reactor where the raw syngas is further processed. For example, unwanted deposits of sticky particles on heat exchange surfaces, walls, valves or outlets can adversely affect the process. Also, such deposits are difficult to remove.

  Accordingly, the raw synthesis gas is quenched in the quenching region. In this quenching region, quenching gas is injected into the synthesis gas in order to cool the raw synthesis gas moving upward.

  WO-A-2004 / 005438 describes a gasification system comprising a gasification reactor and a synthesis gas cooling vessel. This publication describes a gasification combustion chamber and a tubular section fluidly connected to the open upper end of the combustion chamber. Both the combustion chamber and the tubular portion are disposed in the pressure shell, forming an annular space between the pressure shell and the combustion chamber and between the pressure shell and the tubular portion, respectively. In the tubular portion, a quenching gas is injected into the hot synthesis gas. This publication also describes separate cooling vessels with three rows of heat exchange heat transfer surfaces arranged one above the other.

  US-A-5803937 describes a gasification reactor and a syngas cooler in one pressure vessel. In this reactor, the tubular part is fluidly connected to the open upper end of the combustion chamber. At the upper end of the tubular part, the gas is deflected 180 ° so that it flows downward through the annular space between the tubular part and the wall of the pressure shell. The annular space is provided with a heat exchange surface for cooling the hot gas.

  US-A-483146 describes a gasification system for solid particles comprising a gasification reactor and a syngas cooling vessel as described in WO-A-2004 / 005438. This publication describes a method and apparatus for controlling the wrapping of heat exchange surfaces present in separate cooling vessels. This wrapping is required to prevent deposits and deposition on the surface of the heat exchanger.

  The gasification reactor described above is common with respect to the gasification burner present in the reactor, in that the produced synthesis gas flows substantially upward and the slag flows substantially downward. All these reactors therefore have a slag outlet separate from the synthesis gas outlet. This is the type of gas, for example as described in EP-A-926441, where both slag and synthesis gas flow downwards and both slag and synthesis gas outlets are located at the lower end of the reactor. In contrast to the conversion reactor.

The present invention relates to an improved reactor of the type in which slag flows downward and is discharged at the lower end of the reactor, and synthesis gas flows upward and is discharged at the upper end of the reactor.
EP-A-400740 WO-A-2004 / 005438 US-A-5803937 US-A-483146 EP-A-926441 US-A-48887962 US-A-4523529 US-A-4510874

  The problem with the syngas coolers of WO-A-2004 / 005438 and US-A-483146 and the device of US-A-5803937 is that the configuration of the device becomes very complicated by the heat exchange surface. . Further, large-scale means such as lapping are required to prevent deposits and deposition on the surface of the heat exchanger. Another problem is that the heat exchange surface is more vulnerable to fouling, for example with feedstocks having a strong alkaline content. Thus, there is a desire not only to provide a simpler gasification system, but also to process strong alkaline feedstocks. These and other objectives are achieved by the following reactors.

SUMMARY OF THE INVENTION A gasification system comprising a gasification reactor and a syngas cooling vessel, the gasification reactor comprising:
-A pressure shell to maintain a pressure higher than atmospheric pressure;
-A slag tank located at the bottom of the pressure shell;
-A gasifier wall which is arranged inside the pressure shell and forms a gasification chamber;
During operation, synthesis gas can be generated in the gasification chamber, the open lower portion of the gasifier wall is in fluid communication with the slag tank, and the open upper end of the gasifier wall is cooled with the synthesis gas via a connecting conduit. In fluid communication with the container;
The gasification wherein the syngas cooling vessel comprises a hot syngas inlet, a cooled syngas outlet, and means for bringing liquid water into direct contact with the hot syngas produced in the gasification reactor in use system.

  Applicants have found that by using the reactor of the present invention, the use of complex heat exchange surfaces can be avoided. Another advantage is that it can more easily process strong alkaline feedstocks. Other advantages and preferred embodiments are described below.

  The present invention also relates to a method for producing a mixture containing carbon monoxide and hydrogen by partial oxidation of a solid carbon-based raw material in the gasification system of the present invention. In the gasification chamber, the solid carbon-based raw material is partially oxidized with an oxygen-containing gas to form a gas mixture in which the temperature is 1200 to 1800 ° C., preferably 1400 to 1800 ° C., and the pressure moves upward 20 to 100 bar. Alternatively, the gas mixture in the connecting conduit is cooled to a temperature of 500-900 ° C. by injecting a liquid cooling medium, and then the gas in the synthesis gas cooling vessel is further brought to below 500 ° C. by contacting with water. Cooling.

  It has been found that the raw synthesis gas is cooled very efficiently, which reduces the risk of sticky particle deposits downstream of the gasification reactor.

DETAILED DESCRIPTION OF THE INVENTION The gasification reactor of the present invention or the system of the present invention uses the gasification reactor of the present invention to produce a mixture containing carbon monoxide and hydrogen by partial oxidation of a solid carbon-based raw material. It is suitable to do. In such a process, a solid carbon-based raw material is partially oxidized using an oxygen-containing gas in a gasification chamber to form a gas mixture that moves upward at a temperature of 1200 to 1800 ° C, preferably 1400 to 1800 ° C. Preferably, the mixture is cooled in the cooling step. In a separate cooling vessel, the gas is preferably further cooled to below 500 ° C.

  A solid carbon material is partially oxidized with an oxygen-containing gas. Preferred carbonaceous feedstocks are solid, high carbon content feedstocks, more preferably comprising substantially (ie> 90% by weight) natural or synthetic (petroleum) coke, most preferably coal. Suitable coals include lignite, bituminous coal, subbituminous coal, anthracite and lignite.

  In general, this so-called gasification is performed by partially burning a carbon-based raw material using a limited volume of oxygen at a high temperature in the absence of a catalyst. In order to achieve faster and complete gasification, initial pulverization of coal is preferable to fine coal particles. The term fine particles refers to at least comminuted particles having a particle size distribution such that about 90% by weight or more of the substance is less than 90 μm and the water content is generally 2 to 8% by weight, preferably less than about 5% by weight. It means to include.

  Preferably, the gasification is carried out in the presence of oxygen and optionally some water vapor, preferably the purity of oxygen is at least 90% by volume and nitrogen, carbon dioxide and argon are acceptable as impurities. Substantially pure oxygen, such as that separated by an air separation unit (ASU), is preferred. Oxygen may contain some water vapor. Water vapor functions as a moderator gas in the gasification reaction. Preferably, the ratio of oxygen to water vapor is 0 to 0.3 parts by volume of water vapor per 1 part by volume of oxygen. Preferably, the oxygen used is preferably heated to a temperature of about 200-500 ° C. prior to contact with the coal.

  If the water content of the carbonaceous feedstock is too high as can occur when coal is used, it is preferable to dry the feedstock before use.

  Preferably, the partial oxidation reaction is carried out by burning a dry mixture of carbon-based fine particles and carrier gas with oxygen in a suitable burner provided in the gasification chamber of the reactor of the present invention. Examples of suitable burners are described in US-A-48887962, US-A-4523529 and US-A-4510874. Preferably, the gasification chamber includes one or more pairs of partial oxidation burners, and the burners include a solid carbon-based raw material supply means and an oxygen supply means. Here, a pair of burners means two burners arranged in a diametrical direction horizontally in the gasification chamber. This results in a pair of two burners in substantially opposite directions at the same horizontal position. The reactor may comprise 1 to 5 pairs of burners thus paired. The upper limit of the logarithm will depend on the reactor size. The combustion direction of the burner may be shifted slightly in the tangential direction as described in EP-A-4000074, for example.

  Examples of suitable carrier gases for transporting the dried solid feed to the burner are water vapor, nitrogen, synthesis gas and carbon dioxide. Nitrogen is preferably used especially when synthesis gas is used as a feedstock for producing ammonia for power generation. Carbon dioxide is preferably used when the shift reaction is carried out downstream with respect to the synthesis gas. The shifted synthesis gas can be used, for example, to produce hydrogen methanol and / or dimethyl ether or as a feed gas for Fischer-Tropsch synthesis.

Synthesis gas discharged from the gasification reactor comprises at least _H 2, CO, and CO _2. In particular, the suitability of the synthesis gas composition for the methanol production reaction is represented by the stoichiometric number SN of the synthesis gas, and thus using the molar content [H ₂ ], [CO], and [CO ₂ ], SN = ([H ₂ ]-[CO ₂ ]) / ([CO] + [CO ₂ ]). It has been found that the stoichiometric number of synthesis gas produced by gasification of the carbon-based raw material is smaller than about 2.05, which is a desirable ratio in the case of producing methanol in the methanol production reaction. By performing a water shift reaction and separating a part of carbon dioxide, the SN number can be improved. Preferably, SN separated from methanol synthesis off-gas can be added to the synthesis gas to increase the SN.

  In one embodiment of the invention, the hot synthesis gas is first cooled to a temperature of 500-900 ° C. in a first cooling step before the hot synthesis gas enters a separate cooling vessel. Preferably, in this first cooling step, a gas temperature lower than the solidification temperature of the non-gas component present in the high-temperature synthesis gas is realized. The solidification temperature of the non-gas component in the high-temperature synthesis gas depends on the carbon-based feedstock, and is usually 600 to 1200 ° C, particularly 500 to 1000 ° C in the case of coal-based feedstock. Preferably, the first cooling step is performed in a connecting conduit that fluidly connects the gasification chamber and the cooling vessel. Cooling may be performed by injecting a quenching gas. Cooling with quenching gas is well known and is described, for example, in EP-A-416242, EP-A-661506 and WO-A-2004 / 005438. Examples of suitable quenching gases are recycled synthesis gas and water vapor.

  More preferably, this first cooling and / or cooling performed in the cooling vessel is performed by injecting a mist of droplets into the gas stream, as will be explained in detail later. The use of liquid mist compared to quenching gas is advantageous because of the greater cooling capacity of the mist.

  This liquid can be any liquid having a viscosity suitable for nebulization. Examples of liquids to be injected include, but are not limited to, liquefied hydrocarbons, waste streams, and the like. Preferably, the liquid contains 50% or more water. Most preferably, the liquid contains substantially (ie> 95% by volume) water. In a preferred embodiment, waste water (also referred to as black water) obtained in a downstream synthesis gas scrubber that is supposed to be installed is used as this liquid. More preferably, any downstream water shift reactor process condensate is used as this liquid.

The term hot synthesis gas means a gas mixture as obtained directly in the gasification chamber.
The term “mist” means that the liquid is injected in the form of small droplets. When water is used as the liquid, preferably more than 80% water, more preferably more than 90% water is in the liquid state.

  Preferably, the temperature of the injected mist is at most 50 ° C. below the bubble point, in particular at most 15 ° C., more preferably at most 10 ° C. below the bubble point, at the general pressure conditions at the point of injection. For this reason, when the injected liquid is water, the temperature is usually higher than 90 ° C, preferably higher than 150 ° C, more preferably 200 ° C to 230 ° C. This temperature obviously depends on the operating pressure of the gasification reactor, i.e. on the pressure of the raw synthesis which will be described in detail later. This makes it possible to quickly vaporize the injected mist while preventing cold spots. As a result, there is less risk of ammonium chloride depositing or ash being attracted locally in the gasification reactor.

Furthermore, it is preferable that the mist consists of droplets having a diameter of 50 to 200 μm, preferably 100 to 150 μm. Preferably, at least 80% by volume of the injected liquid is in the form of droplets having the above size.
In order to promote rapid cooling of the high-temperature synthesis gas, it is preferable to inject mist at a speed of 30 to 90 m / s, preferably 40 to 60 m / s.

Also, it is at least 10 bar higher than the raw syngas pressure present in the gasification reactor, preferably 20-60 bar higher than the raw syngas pressure, more preferably about 40 bar higher than the raw syngas pressure. The mist is preferably injected at a high injection pressure. If the mist is injected at an injection pressure that is less than 10 bar above the pressure of the raw syngas, the mist droplets may become too large. In the latter case, the atomizing gas may be used to at least partially offset, and as this atomizing gas, for example, N ₂ , CO ₂ , water vapor or synthesis gas may be mentioned, and water vapor or synthesis gas is more preferable. A further advantage of using an atomizing gas is that the difference between the injection pressure and the raw syngas pressure can be reduced to a pressure difference of 5-20 bar.

  Furthermore, it has been found to be particularly suitable when the mist is injected away from the gasification reactor or when the mist is injected in the raw syngas flow direction, more preferably at a constant angle. . This eliminates or reduces dead space that can cause local deposits on the walls of the connecting conduit. Preferably, from the wall of the connecting conduit or from the wall of the cooling vessel in the direction of the hot syngas flow, 30-60 °, more preferably about 45 ° relative to a plane perpendicular to the longitudinal axis of the connecting conduit or the cooling vessel. Mist is injected at an angle of. Alternatively, the mist injection in the cooling vessel may be performed by injecting the mist in the same direction as the synthesis gas flow path, preferably downward.

According to another preferred embodiment, the injected mist is at least partially encased by a shielding fluid. This reduces the risk of forming a local deposit. The shielding fluid can be any suitable fluid, but is preferably selected from the group consisting of inert gases such as N ₂ and CO ₂ , synthesis gas, water vapor, and combinations thereof.

According to a particularly preferred embodiment, the amount of mist to be injected, H _{2 O} in the synthesis gas raw exiting the cooling vessel is at least 40% by volume, preferably 40 to 60 vol% H _{2 O,} more preferably 45 to 55 is selected to include a volume% of _{H 2} O.

  In another preferred embodiment, if one chooses to perform a so-called overquenching, the amount of water added relative to the raw synthesis gas is even greater than the preferred range described above. In an over-quenched process, the amount of water added, preferably the amount added to the cooling vessel, does not evaporate all of the liquid water, and some of the liquid water is in the cooled raw syngas. It is the amount that remains. Such a process is advantageous because it eliminates the downstream dry solids removal system. In such a process, the raw syngas exiting the cooling vessel is saturated with water. The weight ratio of raw syngas to water injection can be 1: 1 to 1: 4.

  The over-quenching process conditions can be realized by injecting a large amount of water into the synthesis gas flow path, passing the synthesis gas flow through a water tank disposed at the lower end of the cooling vessel, or a combination of these means.

  It has been found that this eliminates the need for additional water vapor in any downstream water shift conversion process, or significantly reduces the capital cost because the required amount of water vapor is significantly reduced. Here, the capital cost means the capital cost for the steam boiler.

In the preferred process of the invention, the synthesis gas or part thereof exiting the quench zone, in particular the synthesis gas saturated with water, is preferably shift-converted, whereby at least a part of the water reacts with CO and CO ₂ . by generating the H _2, obtaining a shift converted synthesis gas stream. Those skilled in the art will readily understand what a shift converter means and will not be further described. Preferably, the raw syngas is heated in the shift-converted syngas stream in a heat exchanger before the raw syngas is shift converted. This further reduces the energy consumption of the method. In this regard, it is also preferable to heat the liquid before using the liquid to be injected as mist in the method of the present invention. Preferably, the heating of the liquid is performed by indirect heat exchange on the shift-converted synthesis gas stream.

A part of the synthesis gas is water-shifted to obtain a stream with less CO, and another part of the synthesis gas is bypassed by the water-shifting device, and the H ₂ / Any desired molar ratio of CO can be obtained. By selecting the ratio of feed to bypass and shift, the most desirable ratio for the preferred downstream process can be achieved.

DETAILED DESCRIPTION OF THE DRAWINGS The present invention will now be described in detail with reference to the accompanying drawings by way of non-limiting example. The same reference numbers used in the following indicate similar structural elements.

  Please refer to FIG. FIG. 1 schematically shows a system (1) for producing synthesis gas. In the gasification reactor (2), the carbon-based stream and the oxygen-containing stream are supplied to the gasification chamber (2) from the pipes (3) and (4), respectively. In the gasification chamber (2), raw synthesis gas and slag are obtained. For this purpose, several burners (not shown) are usually provided in the gasification chamber (2). Usually, the partial oxidation in the gasification chamber (2) is 1 to 200 bar, preferably 20 to 100 bar, more preferably 40 to 70 bar at a temperature in the range 1200 to 1800 ° C, preferably 1400 to 1800 ° C. Run at pressure.

  The produced raw synthesis gas is sent to the cooling vessel (9) via the connecting conduit (5). Mist water (17) is injected into the connecting conduit (5), and the synthesis gas is cooled to below 500 ° C., for example, about 400 ° C.

  The ash component present in most preferred feedstocks forms so-called liquid slag at these temperatures in the gasification chamber (2). Preferably, this slag forms a layer inside the wall of the gasification chamber (2), thereby providing an insulating layer. The temperature conditions are selected such that the slag can create such a protective layer on the one hand and still flow to the slag outlet (7) provided on the bottom for any further processing on the other hand. .

  As shown in the embodiment of FIG. 1, the partially cooled synthesis gas (8) enters the cooling vessel (9). In the cooling vessel (9), the synthesis gas (8) is brought into contact with a predetermined amount of water (6) in the over-quenching process mode to obtain a water-saturated synthesis gas (10).

The water-saturated synthesis gas (10) is sent directly to the wet gas scrubber (11) and then sent to the shift converter (13) via the line (12) to react CO with at least a portion of the water. by generating the ₂ and H _2, to obtain a shift conversion gas stream in line (14). Part of the cleaned gas (12) may bypass the shift converter (13). This gas and stream (20) may optionally be mixed after both streams have undergone further gas treatment (not shown). The wet gas scrubber (11) and the shift converter (13) itself are known and will not be described in further detail here. Waste water from the gas scrubber (11) is withdrawn from the line (22) and optionally part of it is recirculated to the gas scrubber (11) via the line (23). Preferably, black water which is part of the waste water from the gas scrubber (11) can be used as liquid water injected via line (17) or (6). In non-over-quenched mode, the synthesis gas (10) is preferably sent to a dry solids removal device to remove at least a portion of the dry ash. Preferred solid removal devices are, for example, the cyclones or filter units described in EP-A-551951 and EP-A-14999418.

  Further improvements are realized when the raw synthesis gas in line (12) is overheated with the shift-converted synthesis gas in line (14) leaving the shift converter (13) in the heat exchanger (15). Is done.

  Furthermore, according to the invention, the energy contained in the stream in the line (16) exiting the heat exchanger (15) is transferred to the line (17) before being used in the first or second cooling step. It is preferably used to warm water. For this purpose, the stream in the line (16) may be sent to the indirect heat exchanger (19) for indirect heat exchange with the stream in the line (17).

  As shown in the embodiment of FIG. 1, the stream in line (14) is first passed to the heat exchanger (15) before entering the indirect heat exchanger (19) via line (16). Sent. However, those skilled in the art may omit the heat exchanger (15) if necessary, or the stream in the line (14) may first be subjected to an indirect heat exchanger (19) prior to heat exchange in the heat exchanger (15). ) Will be easily understood.

  The CO-depleted synthesis gas in line (20) leaving the indirect heat exchanger (19) may be further processed if necessary for further heat recovery and gas treatment.

  If necessary, the heated stream in line (17) may be partially used as water supply (line (21)) to the gas scrubber (11).

  FIG. 2 is a longitudinal cross-sectional view of a gasification system that can be part of the system 1 of FIG. FIG. 2 shows the gasification reactor (43) of FIG. 1 of WO-A-2004 / 005438 in combination with a connecting conduit, ie a downstream cooling vessel or quenching vessel (44) fluidly connected by a transfer duct (45). Indicates. FIG. 2 shows a gasification chamber (47), which is connected to a tubular portion (51), and the tubular portion (51) connects the gasification chamber (47) to the upper wall portion by a connecting conduit. It connects with the inside of a cooling container (44) via (52). An injection means (48) for injecting a liquid or gaseous cooling medium is provided at the lower end of the tubular portion (51). The cooling vessel (44) further comprises an outlet (49) for the cooled synthesis gas.

  The system of FIG. 2 differs from the system of FIG. 1 of WO-A-2004 / 005438 in that the cooling vessel 3 of FIG. 1 is omitted and a simple means (46) for adding liquid water is provided. It differs in that it is replaced by a container. Another difference is that the injection means (48) is suitable for injecting mist of liquid water.

  Preferably, the walls of the gasification chamber (43) and / or the walls of the connecting conduit (51) are provided with cooling means. Preferably, the cooling means has a structure composed of water-cooled tubes, and more preferably takes the form of a membrane wall.

  FIG. 2 also shows the burner (50). Suitably the burner configuration may be as described in EP-A-0400420, incorporated herein for reference. Preferably, various other details of the gasification reactor (43) and transfer duct (45) as well as the top configuration of the cooling vessel (44) are described with respect to the apparatus of FIG. 1 of WO-A-2004 / 005438. It may be as disclosed.

  The method of the present invention when retrofitting an existing gasification reactor by replacing the synthesis gas cooler of the prior art publication with a cooling vessel (44), or while maintaining the actual gasification reactor of the prior art. Is preferred, the embodiment of FIG. 2 is preferred.

  Thus, preferably in the system according to the invention, the cooled synthesis is provided with an inlet at its upper end for receiving the hot synthesis gas of the cooling vessel so that a substantially downward flow path of the synthesis gas is produced in use. An outlet for gas is provided at the lower end thereof, and an injection means for injecting water mist is provided in the downward flow path.

  FIG. 3 shows the upper end of the gasification reactor (43) and the upper end of the gasification chamber (47). This upper end is fluidly connected to another cooling vessel (53) by a connecting conduit (51). An injection means (48) is provided for injecting a gas or liquid quenching medium according to the method of the present invention.

  In the cooling vessel (53), a dip pipe (54) is provided to create a downward flow path of the synthesis gas. An injection means (46) is provided at the upper end of the dip pipe (54) for injecting mist of liquid water into the synthesis gas. The dip tube is partially submerged in the water tank (55). In use, the synthesis gas flows through the water tank (55) into the annular space (56) that exists between the dip tube (54) and the wall of the cooling vessel (53). From the annular space (56), water-saturated synthesis gas is discharged from the cooling vessel via a conduit (57).

  FIG. 3 also shows a pump (58) for recirculating water (59), providing an effluent stream (60) and a fresh water feed stream (61).

  Therefore, the present invention also provides that the synthesis gas cooling container has an opening for receiving the high temperature synthesis gas at the upper end and an outlet for the cooled synthesis gas, and the synthesis gas is provided between the inlet and the outlet. And a system in which a water tank is provided in the synthesis gas flow path.

  More preferably, the present invention relates to a system in which injection means for injecting a liquid or gaseous cooling medium into the synthesis gas are provided in the connecting conduit. More preferably, the injection means is an injection means for injecting the liquid cooling medium in the form of a mist of water droplets.

  Those skilled in the art will readily appreciate that the present invention can be modified in various ways without departing from the scope described in the claims.

1 is a schematic process diagram for a system for producing a purified mixture containing carbon monoxide and hydrogen. FIG. It is a schematic longitudinal cross-sectional view of the preferable gasification system comprised from the reaction container and the cooling container. Fig. 4 schematically shows another possible embodiment for a cooling vessel.

Explanation of symbols

DESCRIPTION OF SYMBOLS 1 Syngas production system 2 Gasification reactor 3 Pipe line 4 Pipe line 5 Connection pipe 9 Cooling container 11 Wet gas scrubber 13 Shift converter 15 Heat exchanger 19 Indirect heat exchanger 43 Gasification reactor 44 Cooling container 45 Transfer duct 46 Liquid water addition means 47 Gasification chamber 48 Mist injection means 50 Burner 51 Connecting conduit 53 Cooling vessel 54 Dip pipe 55 Water tank 56 Annular space 58 Pump

Claims (15)

A gasification system comprising a gasification reactor and a synthesis gas cooling vessel, wherein the gasification reactor is
-A pressure shell to maintain a pressure higher than atmospheric pressure;
-A slag tank located at the bottom of the pressure shell;
-A gasifier wall arranged inside the pressure shell and forming a gasification chamber, comprising at least one burner;
During operation, the gasification chamber can generate synthesis gas containing carbon monoxide, carbon dioxide and hydrogen, and the open lower portion of the gasifier wall is in fluid communication with the slag tank, and the upper open end of the gasifier wall The section is in fluid communication with the synthesis gas cooling vessel via a connecting conduit;
There is an injection means for injecting a liquid or gaseous cooling medium into the synthesis gas into the connecting conduit;
The syngas cooling vessel has an inlet for receiving hot syngas at its upper end and an outlet for the cooled syngas so that a substantially downward flow path of the syngas is created in use. An injection means for forming a syngas flow path between the inlet and the outlet and injecting a mist of water is provided in the downward flow path; and the synthesis gas cooling vessel is a flow path for the synthesis gas Including an aquarium inside,
The gasification system.   The system of claim 1, wherein the walls of the gasification chamber and the walls of the connecting conduit comprise cooling means.   The system according to claim 2, wherein the cooling means has a water-cooled tube structure.   The system according to claim 3, wherein the cooling means is in the form of a membrane wall.   The gasification chamber includes one or more pairs of partial oxidation burners, and the burner includes a solid carbon-based raw material supply unit and an oxygen-containing gas supply unit. System.   The system of claim 1, wherein the outlet of the cooled synthesis gas is fluidly connected to an inlet of a wet gas scrubber.   The system of claim 6, wherein the gas outlet of the wet gas scrubber is fluidly connected to the inlet of the water shift converter. A method for producing a synthesis gas containing carbon monoxide, carbon dioxide and hydrogen by partial oxidation of a solid carbon-based raw material in the gasification system according to any one of claims 1 to 7, The solid carbon-based raw material is partially oxidized with an oxygen-containing gas to form a gas mixture in which the temperature is 1200 to 1800 ° C. and the pressure is upwardly moved to 20 to 100 bar, and a liquid cooling medium is injected into the connecting conduit. Said gas mixture is cooled to a temperature of 500-900 ° C. and then further cooled to below 500 ° C. by contacting the gas in the synthesis gas cooling vessel with water,
Performing the cooling in the connecting conduit and / or the syngas cooling vessel by injecting a mist of water droplets into the gas stream;
Said method.   The method according to claim 8, wherein the temperature of the injected water mist is at most 50 ° C below the bubble point of water at the pressure of the hot synthesis gas.   The method according to claim 8 or 9, wherein the mist comprises droplets having a diameter of 50 to 200 µm, and the mist is injected at a speed of 30 to 100 m / s.   The method according to claim 10, wherein the mist is injected at a speed of 40 to 60 m / s.   9. The method of claim 8, wherein the mist is injected at an injection pressure that exceeds the pressure of the synthesis gas present in the gasification reactor by at least 10 bar.   9. The method of claim 8, wherein the mist is injected at an injection pressure that exceeds the pressure of syngas present in the gasification reactor by 20-60 bar.   9. The method of claim 8, wherein the mist is injected using an atomizing gas having an injection pressure that is 5-20 bar higher than the pressure of the synthesis gas.   9. The mist is injected in the direction of hot syngas flow from the wall of the connecting conduit or cooling vessel at an angle of 30-60 [deg.] With respect to a plane perpendicular to the longitudinal axis of the connecting conduit or cooling vessel. The method described.