DE3024469A1 - METHOD AND DEVICE FOR PARTIAL OXIDATION OF CARBONATED SOLIDS - Google Patents

Description

DR. GERHARD SCHUPFNER ~ / ΙΟ 'Karlstr. ^ J Q 2 4 4 6 S. Patent attorney 2110 Buchholz i.d.N.

June 26, 1980

TEXACO DEVELOPMENT CORPORATION 2000 Westchester Aven.ue
White Plains, NY 10650
United States

PROCESS AND EQUIPMENT FOR PARTIAL OXIDATION OF SOLID CARBON FUELS

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ORK3INAL INSPECTED

Process and device for the partial oxidation of carbonaceous solid fuels

The invention relates to the generation of pure gas mixtures from H_ and CO, in particular a method and a device for cooling and cleaning the hot raw gas stream, which is generated by partial oxidation of carbonaceous solid fuels and mainly H _? , CO, C0 _? , HpO and contains entrained slag and solids.

In the partial oxidation of carbonaceous liquids and Solid fuels with steam and free oxygen for extraction of gas mixtures comprising carbon monoxide and hydrogen, the gases leave the gas generator with a Temperature of approx. 927-164-9 C. 3e after charging and operating conditions are in the one leaving the gas generator Gas stream contain varying amounts of molten slag and solids such as soot and ash. Frequently it is desirable to reduce the concentration of these entrained substances. By separating solids from the gas stream can, for. B. the service life of downstream units contacted by the gas flow be e.g. B. of gas coolers and turbines.

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- ie - 3024463

the. The solids separation from the synthesis gas is prevented furthermore, clogging of catalyst beds, and furthermore, environmentally friendly gas can be generated.

According to US Pat. No. 2,871,114, the product gas resulting from coal gasification and the slag are fed into a slag separator arranged directly below the gas generator. Water is supplied to this to absorb and solidify the slag falling out of the gas stream. The gas flow exits the slag separator and flows into a quenching storage tank, in which the gas is brought into close contact with water and cooled to a temperature of approx. 14-9-316 ° C. The gas flow emerging from the quenching vessel is saturated with H_0. Furthermore, the entire inherent heat of the gas flow is given off into the quenching water at a relatively low temperature level. If a coal-fired gas generator is introduced at a temperature of more than about 927 ⁰ C leaving crude gas directly into a gas cooler, the entrained in the gas flow slag is on the inner surfaces of the gas cooler, and dirty the heat exchange surfaces. In US-PS A 054 · 4-24 no means is given for the separation of the slag from the system.

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In contrast to the prior art, in the present invention the raw synthesis gas is purified in water without quenching and is therefore not saturated. It is cooled to a temperature of about 649 to 982 ⁰ C also, which is below the Deformation initial temperature of the slag. The thermal energy contained in the gas flow can be recovered at a high temperature level. Furthermore, the solidified slag particles are withdrawn from the system. This prevents the units that are connected downstream in order to obtain the energy from the hot gas flow from being soiled.

The invention relates to a method for generating a hot raw gas stream, which mainly consists of H_, CO, CO- and H_0 and entrained solids and slag contains, by partial oxidation of a carbonaceous solid fuel such as coal as well as cooling and cleaning of the Raw gas flow for separating the entrained solids and slag.

The method according to the invention for the partial oxidation of ash-containing solid carbonaceous fuels to obtain a purified stream of synthesis gas, heating gas or reducing gas is characterized by the following steps: Reacting particles of the solid fuel

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with a free oxygen-containing gas with or without a temperature moderator in a heat-resistant lined downdraft gas generator at a temperature of approx. 927-1704- C and a pressure of approx. 10-200 bar to obtain a raw gas stream from H ₂ , CO, C0_ and at least one of the substances H ₂ O, H ₂ S, COS, CH ^, NH ₃ , N _£ or A, which contains molten slag and / or solid particles; Passing the raw gas stream through a thermally insulated transfer line and a first gas inlet into the lower chamber of a gas-solids separation zone which comprises: a closed vertical cylindrical thermally insulated pressure vessel with the lower chamber which is coaxial with the vertical center axis of the pressure vessel and with a coaxial one upper chamber in fluid communication with the lower chamber, the lower and upper chambers being interconnected by a coaxial throttle ring passage in which a portion of the slag and / or particulate matter is separated by gravity and falls to the lower end of the lower chamber; Feeding the gas mixture from the lower chamber upwards through the throttle ring passage into the upper chamber in countercurrent with slag droplets and possibly further into a gas-solids separation unit positioned in the upper chamber; Separating slag and / or solid particles from the gas mixture in the upper chamber and withdrawing them from the container through an outlet in the bottom of the lower chamber; and

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Withdrawing purified gas from the upper chamber and discharging the gas through an outlet at the top of the vertical pressure vessel.

The invention also relates to a new gas-gas quench cooling and solids separation device which can be used in the method according to the invention. The apparatus comprises a closed cylindrical insulated vertical pressure vessel having a lower quench chamber in fluid communication with an upper solids separation chamber. The hot raw gas flow can be introduced into the lower chamber, in which the gas temperature is reduced to approx. 64-9-982 ⁰ C and below the initial deformation temperature of the slag, through direct heat exchange with an incident, oppositely directed coaxial flow cooled, purified and compressed circulating quenching gas. Solid particles are separated from the raw gas stream and discharged through an outlet at the bottom of the lower chamber. A throttle ring passage separates the lower chamber from the upper chamber. The swirled stream of cooled gas leaving the lower chamber flows upwards through the throttle ring passage in countercurrent with solid slag droplets which are separated from above by gravity. Optionally, in the lower chamber there is a solids separation unit, which can be a single or multi-stage cyclone, an impact separator, a filter or a combination of the

030065/0761 ORIGINAL INSPECTED

these devices are arranged for the separation of fine particles and containing residual carbon solid slag droplets that have remained in the cooled gas stream. In a preferred embodiment is a solids separation unit in the upper chamber, which is a single or multi-stage cyclone or a Combination of both is arranged. A cooled and purified gas stream is discharged from the upper chamber and subjected to further cooling and, if necessary, additional cleaning. A Part of this gas stream is then compressed and used as the cooled and purified recycle quench gas stream returned to the lower chamber.

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The invention is explained in more detail, for example, with the aid of the drawing. Show it:

Fig. 1 is a vertical section through the gas-gas

Quench cooler and solids separator according to the invention;

Fig. 2 is a schematic view of a plant in which the device according to FIG. 1 is used to carry out a method according to the invention will; and

3 shows a schematic view of a second installation in which the device according to FIG a second method according to the invention is used.

The present invention relates to an improved continuous process or cycle with associated Device for cooling and cleaning a hot raw gas stream, which mainly comprises H-, CO, CO- and H-O and Contains entrained solids and molten slag. The device is particularly suitable for cooling and cleaning the hot raw gas flow generated by the partial oxidation of a carbonaceous solid fuel,

The generation of energy from the partial oxidation gas generator exiting hot raw gas flow increases the heat

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ORK3SNAL INSPECTED

efficiency of the gasification process. Thus, water vapor occurring as a by-product can be used in the process or for export by heat exchange between the hot gas stream and water in a gas cooler. The energy recovery is made more difficult, however, that in the gas generator exhaust gases droplets of molten Slag are present resulting from the amalgamation of the ash content of the coal supplied to the gas generator. The present invention provides an apparatus and method for solidifying the molten slag droplets and separating the resulting particulate matter from the gases, thereby facilitating energy recovery will. Problems that usually occur in the formation of slag are thereby eliminated with the invention avoided that the slag particles are solidified before they strike solid surfaces. aside from that no solid surfaces are provided at the starting point of slag cooling.

de according to the amount of unconverted solids and ash In the raw gas stream emerging from the gas generator, the process and the device can either be used individually or follow a pre-separation of solids and liquid slag from the gases. True, it is Device according to the invention for processing the hot raw material emerging from practically every type of gas generator

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gas stream, but it is particularly suitable for use after a partial oxidation gas generator. A An example of such a gas generator is given in US Pat. No. 2,829,957. According to one embodiment According to the invention, the new gas-gas quench cooling and solids separation device can be combined with a gas cooler Be connected upstream system that has a gas generator for generating synthesis gas and a gas cooler. For example, a partial oxidation gas generator and a waste heat boiler can be separated by a pressure chamber with or without Collection containers must be connected to each other (see e.g. U.S. Patent 3,565,588). In this case, the present device can be placed in the line immediately in front of a gas cooler or waste heat boiler, in which boiler feed water is converted into steam, must be switched on. Through the invention combustion residues are deposited in the gas flow, contamination of the boiler tubes is prevented, and the The service life of convection heat exchangers is extended.

The device comprises a closed cylindrical vertical pressure vessel, the inner walls of which are thermally insulated are. For example, the interior of the container can be lined with high temperature resistant refractory material. There are two in the container cylindrical vertical refractory lined chambers are provided which are coaxial with the central axis of the container and communicate with each other. These are a lower quenching chamber and an upper solids separation chamber.

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ORIGINAL INSPECTED

302U69

A coaxial throttle ring channel connects the two chambers. The longitudinal axis of at least one pair of opposite, internally insulated inlet nozzle penetrates the walls of the lower chamber. The inlet nozzles are spaced 180 degrees apart and located on opposite sides of the lower chamber. The hot raw gas stream is passed through an inlet nozzle and a comparatively cooler and cleaner recirculating quench gas stream is passed through the opposite inlet nozzle. The two gas flows meet in the lower chamber, and the direct meeting creates a turbulent gas mixture. The strong vortex results in rapid mixing of the opposing gas flows and direct heat exchange.

The following explanation refers to the normal construction with a single pair of inlet nozzles, but there can also be several pairs, e.g. B. 2-10, similar inlet nozzles can be used. The nozzle pairs can be equally spaced around the container. The longitudinal axis of the inlet nozzles can be at an angle of inclination run so that the raw gas flow is directed upwards (see. The drawing), or enter horizontally. Alternatively the longitudinal axis can be inclined so that the raw gas flow is directed downwards if this is the overall configuration of the gas generator and the quenching separator corresponds better. So it suits every couple

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Inlet nozzles common longitudinal axis in the same plane as the vertical center axis of the container and can be below any angle in the range of about 30-150 to the vertical center axis of the container, measured clockwise from this central axis. Appropriately, this angle is in the range of about 40-135, z. B. at approx. 45 (see the drawing). The actual intended angle is a function of factors such as the temperature and speed of the gas flows as well as the composition, the concentration and properties of the to be deposited substances carried. If z. B. the raw gas flow is liquid Contains slag of high fluidity, the longitudinal axis of the raw gas inlet nozzle can be measured at an angle of approximately 45 ° clockwise from the vertical central axis of the container, upwards. Much of the Slag then runs down the transmission line and is collected in a slag container, which is connected upstream of the device discussed here. If on the other hand the liquid slag is viscous, the slag flow can be supported by opening the raw gas inlet nozzle at an angle of approx. 135, measured clockwise from the vertical center axis of the container, directed downwards. The high flow rate of the hot raw gas stream through the inlet nozzle and the force of gravity would in this case help to bring the viscous slag into the lower chamber, in which it is

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stares and is separated from the gas stream by gravity.

The hot raw gas stream passes through an inlet nozzle with a temperature of about 927-1704 ⁰ C, about 1092 to 1649 ⁰ C, in particular approximately 1260 to 1538 ⁰ C, z. B. 1371 ⁰ C. The pressure is in the range of about 10-200 bar, about 25-85 bar and typically about 40 bar. The flow velocity is approx. 3-30 m / s, e.g. B. approx. 6-15 m / s, typically approx. 9 m / s. The solids concentration in the incoming hot raw gas stream is approximately in the range of approx. 0.1-4.0 g / 0.028 m ³ , e.g. B. approx. 0.25-2.0 g / 0.028 m ³ . The particle size can be in the range of approx. 40-1000 μm or approximately equal to the coarse dust according to Stairmand (cf. Filtration and Separation, Vol. 7, No. 1, p. 53, 1970 Uplands Press Ltd., Croydon, England) .

The cooled, purified quench gas recirculation stream entering through the opposite inlet nozzle is made up of at least a portion, ie about 20-80 mol%, e.g. B. about 30-65 mol%, and typically about 60 mol%, of the overhead product stream from the device with or without further purification and / or cooling. The temperature of the quenching is in the range of approximately 93.3 to 427 ⁰ C, for. B. about 149-316 ° C and typically about 177 ° C. The mass throughput and / or the flow rate of the hot raw gas stream and the cooled, purified quenching gas

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Circulating flow are adjusted so that the kinetic energy of the two oppositely directed inlet gas flows is about the same.

In the following table I are in columns 3 and 4 indicates the temperature and composition of typical gas mixtures that are generated when a stream of raw synthesis gas and a stream of cooled, purified quench circulating gas having those indicated in columns 1 and 2 Temperatures meet in the lower quenching chamber.

Table I.

Gas mixture escaping from the lower quenching chamber

synthesis Circulation temperature Quenching circulating gas raw gas shock gas ° C proportion in the mixture ⁰ C ⁰ C 649 Get- " 1704 427 704 85 927 149 816 30th 1538. 316 927 62 1371 204 871 41 1454 260 982 52 1454 260 760 43 1454 260 61

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The ends of each pair of opposing inlet nozzles preferably do not extend substantially into the chamber. The opposite inlet nozzles preferably end in planes perpendicular to their center lines. As a result, a deviation of these currents with respect to concentricity is kept small. The gas jets emerging from the opposite nozzles flow approx. B. approx. 2.4 m before they meet directly. The high turbulence resulting in the lower chamber favors the rapid mixing of the gas flows. This accelerates the gas-particle heat transfer. By vortex mixing of the cooled and the cooling gas stream, the outer layer of the slag particles solidifies before the slag can strike solid surfaces. There is produced a gas mixture whose temperature is below the Deformation output temperature of the incoming raw gas stream with the slag, that is, at approximately 64-9-982 ⁰ C, typically at about 760 ° C. The entrained slag is cooled and a solidified shell is formed on the slag particles which prevents the particles from adhering to the interior walls of the device or to any solid component therein. In one embodiment, between 1 and 50 volume percent of the quench gas recirculation stream is introduced into the quench separator through a plurality of tangential nozzles positioned at the top of the lower chamber and / or the lower end of the upper chamber. This will make the upward

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given a vortex motion to flowing gases. In addition, this results in a protective belt of cooler gas along the length the inner wall of the throttle ring and above.

Solids, d. H. unreacted coal, carbon particles, carbonaceous solid particles, slag particles, Ashes and particles of refractory material detach themselves from the raw gas stream and fall to the lower end of the lower one Chamber where they pass through an outlet in the bottom of the pressure vessel removed. With the lower outlet is a sluice funnel system connected to maintain the pressure in the container. The lower end of the pressure vessel preferably has has a low point connected to the lower outlet. For example, the lower end of the pressure vessel can be a Truncated cone or spherical or elliptical shape.

The throttle ring forms a connecting passage or corridor between the lower and the upper chamber. It is used for Attenuating the turbulence of the gas flow from the lower chamber. As a result, the upward gas flow is evened out. The gas flow rising through the upper chamber is relative to the turbulence in the lower chamber quiet, reducing the gravity separation of solid particles which fall through the throttle ring passage into the lower end of the lower chamber. Preferred the throttle ring consists of a heat-resistant refractory material. Its diameter is smaller than the diameter

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knives of the upper or lower chamber. The diameters of the upper and lower chambers depend on factors such as the flow rate of the gas flowing through them and the size of the particles carried along. The relationship the diameter d of the upper chamber to the diameter d, the lower chamber is in the range of about 1.0-1.5, typically about 1.0. The ratio of the diameter d of the throttle ring to diameter d, the lower camc 1

mer is in the range of about 0.5-0.9, e.g. B-. approx. 0.6-0.8, typically 0.75.

Although the upper chamber can be empty, so that additional space for the gravity separation of entrained solids is present, but preferably at least one, about 2-12, e.g. B. two gas-solid separators arranged for separating at least some of the solid particles remaining in the gas stream. Typical Gas-solid separation devices used in the upper chamber can be provided are a single-stage cyclone separator, a multi-stage cyclone separator, an impact separator, a filter, and combinations of these Devices. In a preferred embodiment as gas-solids separators, single or multi-stage cyclone separators or combinations thereof are used. The number of gas-solid separation devices used in practice depends on factors such as dimensions

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the upper chamber and the actual volume of the gas flow approaching the inlet of the gas-solids separation device in the upper part of the upper chamber. At this point the solids concentration is in the range of approx. 0.05-2 g / 0.028 m. The particle size is in the range of approx. 4-0-200 µm, which corresponds approximately to the fine dust according to Stairmand. Any conventional continuous gas-solids separation device which removes greater than about 65% by weight of the particulate matter from the gas stream and which can withstand the operating conditions in the upper chamber can be used. The pressure drop through the gas-solid separation device is preferably less than 20 inflow dynamic pressure units. The separation device should also be resistant to hot, abrasion-causing gas flows with a temperature of up to approx. 1093 ^° C. or up to approx. 1649 ^° C.

Typical gas-solids separation devices used in the can be used in the upper chamber are single-stage cyclone separators, Gas-solid impact separator, filter and Combinations of these devices.

Preferred gas-solids separators are cyclone separators. A cyclone is essentially a settling room in which gravity is replaced by centrifugal acceleration. In the case of the dry cyclone separator, the particulate matter partially

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Chen loaded raw gas stream tangentially at one or more Entrance at the top of a cylindrical conical space. The gas flow path is double Vortex, with the raw gas stream flowing downwards in a spiral shape on the outside and the cleaned gas stream flowing into it the inside flows spirally upwards to a central or concentric gas outlet pipe at the top. The purified gas stream exits the cyclone and then flows out of the container through an outlet at the top. The solid particles Due to their inertia, they have a tendency to move in the cyclone towards the separator wall, from the they are passed through a central outlet at the lower end into a discharge pipe. Small particles form clusters which can be easily removed from the cyclone. The discharge or immersion pipe runs in the pressure vessel from the lower end of the Cyclones to preferably below the longitudinal axes of the inlet nozzles in the lower chamber and below the area stronger Downward vortex. Solid particles separated in the cyclone can thus be passed through the dip tube and through a shut-off valve in the lower end of the lower chamber be discharged below the area of strong mixing. The dip tube can go off track in the following way the slag droplets be removed: The dip tube can run close to the wall of the container, it can the axis of the hot gas and quench gas inlet nozzles can be arranged spanning, or ceramic dip tubes can be arranged in the refractory wall should be embedded. It is also possible

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lent to shorten the dip tubes so that they could be attached to any End point above the top of the lower chamber.

For example, at least one single-stage cyclone is arranged in the upper chamber so that its inflow opening is the horizontal circular component of an ascending one Spiral current course is facing that in one embodiment is present in which part of the quenching gas enters the container tangentially, or the in generated in another way by the cyclone inlet flow will. When several single-stage cyclones are connected in parallel the discharge from the gas outlet pipe of each cyclone can take place in a common inner pressure chamber, which is arranged in the upper chamber. The cleaned gas stream emerges from the pressure chamber through the gas outlet on From the top of the upper chamber. In another embodiment, at least one multi-stage cyclone is in the arranged upper chamber. The partially cleaned gas stream emerging from a first inner cyclone stage is thereby into a second cyclone stage, which is arranged in the upper chamber. The purified gas stream from each second cyclone stage is in a common internal pressure chamber, which is located at the top of the upper chamber is carried out. From there the purified gas is then discharged through an outlet at the top of the upper chamber. In other embodiments, outside of the

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upper chamber one- and two-stage cyclones arranged, cyclones can be provided within the upper chamber, but this is not required. (One detailed explanation of cyclone and impact separators can be found e.g. B. "CHEMICAL ENGINEER'S HANDBOOK" Perry and Chilton, Fifth Edition 1973, McGraw-Hill Book Co., pp. 20-80 to 20-87.)

A discharge or immersion pipe runs in the pressure vessel from the lower end of the cyclone, preferably to below the axes of the Inlet nozzles in the lower chamber and under the highly turbulent area. Solid particles separated in the cyclone are passed through the immersion tube and through a shut-off device in the immersion tube in the lower part of the lower chamber under the zone of strong mixing, discharged. The immersion tube can be dislodged as follows Slag droplets are removed: It can run close to the wall of the container, it can be the axis of the Hot gas and quench gas inlet nozzles can be arranged spanning, or ceramic immersion tubes can be inserted into the refractory Be embedded in the wall. Alternatively, it is possible to shorten the dip tubes so that they can be attached to any End point above the top of the lower chamber.

The surface velocity of the ascending gas stream in the upper chamber and diameter and height of the upper one

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Chamber are preferably designed so that the inflow opening in the (or the) cyclone separator lies above the throttle ring by an amount which is at least equal to the transport separation height (TDH = Transport Disengaging Height), also known as the equilibrium detachment height. Above the rate of decrease approaches the transport separation level entrained solid particles in the gas stream zero. the Particle entrainment changes with factors such as viscosity, Density and flow rate of the gas stream; the weight and size distribution of the solid particles; and the height above the throttle ring. The gas flow speed through the throttle ring can be set in a range of approx. Fluctuate 0.61-1.52 m / s. The gas flow rate through the basic useful cross-section of the upper chamber can be in Range of approx. 0.30-0.91 m / s. The transport height can be between approx. 3.05 and 7.62 m. If z. B. the gas flow speed through the throttle ring approx. 1.07 m / s and through the basic overall cross-section of the upper one Chamber is approx. 0.61 m / s or 0.76 m / s due to the basic useful cross-section of the upper chamber, then the transport separation height can be in an upper chamber with an inner diameter of approx. 3.05-4.57 m are approx. 4.57-6.1 m.

The gas stream emerging from the pressure chamber at the top of the cyclone separator flows through an outlet in the top Part of the upper chamber with a temperature of approx. 649-982 ° C. The pressure drop of the gas-solid separator

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device flowing through synthesis gas is less than approx. 0.3A bar. The solids concentration in the from the The gas stream exiting from the separator is in the range of approx. 30-700 mg / 0.028 m. Part of this gas flow becomes subjected to further cooling with or without additional cleaning in a downstream conventional unit, so that the aforesaid quench gas recirculation flow is generated. For example, a conventional gas-solid separation device then to the gas-gas quench cooling and solids separation facility in the system are provided. This gas-solid separation device can be a single-stage or multi-stage cyclone separator, an impingement separator, a filter device, an electrostatic one Be separators and combinations of these devices.

Advantageously, with the device explained approx. 85-95 wt. 56 of the entrained solids and slag from the partial oxidation gas generator leaving hot raw gas stream deposited, while the temperature of the gas stream is reduced to a value that the downstream device for energy recovery from the hot gas flow can withstand. None is preferred Washer fluid used. This is the inherent heat of the hot gas flow is not consumed by evaporating scrubbing liquid, which then contaminates the gas flow. in the

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On the contrary, the intrinsic heat in the purified gas flow leaving the device, the downstream, if necessary is still further cooled and / or cleaned, remains in a downstream convection waste heat boiler to be recovered. Thus, through indirect heat exchange H ~ 0 or boiler feed water converted into steam. The steam can be used elsewhere in the process, e.g. B. for heating purposes, for power generation or in gas generators. Alternatively or additionally, the energy recovery done in a different way. For example, part of the cooled and cleaned gas stream is passed through an expansion turbine guided so that mechanical energy and / or electrical energy is generated.

It should be noted that in some embodiments of The method according to the invention, the proportion of in the hot raw gas stream, which in the lower chamber of the device for Purification of a raw gas stream entering entrained slag by adjusting the composition of the carbonaceous Solid fuel and the temperature in the gas generator is kept low or eliminated. In this case it can the meeting of the gas streams and the quench cooling of the incoming hot raw gas stream by a cooled and purified circulating gas stream advantageously minimized or omitted entirely. In this case, the gas stream leaves the gas cleaning device in the essentially at the same temperature as the entering

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de hot raw gas flow, minus normal thermal losses. All other aspects of the antechamber are the same those operating with gas-gas quenching.

The invention includes an improved continuous process for Cooling and cleaning of a hot raw gas stream, which mainly consists of H-, CO, CO- and one or more of the substances H-O, H-S, COS, CH., NH ,, N- and A is composed and molten Contains slag and / or entrained solids. The hot raw gas stream is through the partial oxidation of a ash containing carbonaceous solid fuel, e.g. B. Coal, produced. The specified method can contain the raw gas stream exiting from the gas generator Combustion residues partially solidified and reduced to tolerable concentration values and particle sizes be reduced. This gas can then be used as synthesis gas, heating gas or reducing gas.

In the specified processes, the thermal efficiency of the gasification is increased by partial oxidation, that energy is recovered from the hot raw gas stream by using by-product steam in the process or for export by heat exchange of the hot gas stream either with water in a gas cooler or with Boiler feed water and steam is generated in a main gas cooling zone. As already said, the energy return is

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recovery through the presence of droplets of molten slag and / or solid particles in the gas generator exhaust gases difficult. In the method according to the invention, the molten slag droplets are partially solidified and deposited before they impinge on heat transfer surfaces. Due to the partial consolidation of the Slag particles before they hit solid surfaces and / or by depositing solid particles, which are entrained in the gas stream, the commonly occurring problems of contamination of the Gas cooler avoided. Solid surfaces are removed from the starting point of slag cooling. For heat transfer comparatively simple, inexpensive gas coolers are used. With the invention, the recovery simplified by thermal energy from the hot gases.

These special gas cooler systems for energy recovery can be used for processing the hot raw gas stream emerging from practically every type of gas generator However, they are particularly suitable for use as a downstream partial oxidation gas generator Facilities. Such a gas generator is z. See, for example, U.S. Patent 2,871,114. In the upper part of the gas generator a burner is arranged for introducing the feed streams. A typical ring burner is e.g. B. in the U.S. Patent No. 2,928,460.

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The reaction zone of the gas generator, which can be freely flowed through is contained in a vertical cylindrical steel pressure vessel, the inside with a heat-resistant material is lined. Preferably, the pressure vessel comprises the following three in connection with one another standing sections: 1) a reaction zone, 2) a gas deflection chamber, and 3) a quenching chamber. the vertical center axes of the three sections are preferably coaxial. Alternatively, the three sections can be split into two or three separate pressure vessels connected in series can be provided. In-the main embodiment is the Reaction zone in the upper part of a pressure vessel, the gas deflection chamber is located approximately in the middle part of the same Pressure vessel, and the quenching chamber is located in the lower part of the same pressure vessel under the gas deflection chamber. In the gas deflection chamber, part of the molten slag and / or the solids is removed from the by gravity separated hot gas stream and passed through a lower outlet into the quench chamber. The main gas flow is diverted away from the inlet to the quench chamber, which is positioned below it, and into a lateral exit channel. The quenching chamber contains water for Quench cooling the slag and / or solids, d. H. unreacted coal and ash. Slag, solids and Water is withdrawn from the bottom of the quench chamber through an outlet in the bottom of the container.

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The hot raw gas stream generated in the reaction zone leaves it through a central outlet in the lower end of the reaction zone, which is coaxial with the central longitudinal axis of the gas generator. The hot gas stream flows through this lower one Outlet and relaxes directly into the gas deflection chamber, which is preferably immediately below the reaction zone. The flow rate of the hot gas stream is reduced, and molten slag and / or particulate matter fall down from the gas stream. These solids and / or molten slag arrive as a result of the Gravity through an outlet located in the lower end of the gas deflection chamber into that in the quenching chamber below contained water. About 0-20% by volume, e.g. B. 0.5-15% by volume, of the raw gas flow can be used as a bleed gas flow are passed through the lower outlet of the gas deflection chamber and thereby takes the separated molten Slag and / or the solid particles with. The partially cooled bleed gas flows through from the quenching chamber a side outlet and a cooled control valve withdrawn. The hot tapped gas stream going through the lower Flows outlet of the gas deflection chamber, prevents an accumulation of solids, which bypass the lower outlet and would clog. The lower outlet of the gas deflection chamber is preferably central and coaxial with the vertical axis of the Arranged gas deflection chamber. The quenching chamber is preferably located directly below the lower outlet of the gas deflection

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chamber. The gas turning chamber can be cylindrical, or it can follow from the inlet to a larger central portion be designed to diverge on the outside or to widen conically, followed by a conically narrowing one Part towards the lower end and the side outlets.

At least a part, ie approx. 80-100% by volume, of the hot gas flow entering the gas deflection chamber is directed into a heat-resistant lateral outlet channel connected to an antechamber through the internal configuration of the gas deflection chamber, which if desired has baffles is. The angle between this lateral outlet channel and the longitudinal axis of the antechamber is in the range of about 30-135 °, about 45-105 °, e.g. B. approx. 60 , measured clockwise from the vertical center axis of the antechamber and starting in the third quadrant. There is essentially no temperature or pressure drop in the gas flow while it flows through the gas deflection chamber.

The hot raw gas flow leaving the gas deflection chamber through the heat-resistant lined outlet channel occurs directly into the inlet of the above-described device for cooling and cleaning the hot raw gas stream (hereinafter referred to as "antechamber"); further slag and / or solid particles are separated there, and optionally the gas stream is partially cooled. This will

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pollution of the boiler tubes in the main gas cooling section is reduced and maintenance problems are minimized. the Pre-chamber is connected upstream of the main gas cooling part.

In some embodiments, instead of or in addition to to the gas-solid separation device, the is arranged in the upper chamber of the antechamber, downstream of the antechamber and in front of the main gas cooling zone outer Gas-solid separation means can be provided. These are Single or multi-stage cyclone separator, gas-solid impact separator, Filter devices, electrostatic precipitators, and combinations thereof.

In preferred embodiments of the invention, a main gas cooling zone is located immediately behind the antechamber or any solids separation device downstream of the antechamber. The temperature of the entering into the main gas cooling zone the gas stream is in the range of about 64-9-164-9 ⁰ C, such as about ⁰ C 64-9-982, z. B. approx. 871 ⁰ C. The solids concentration of this gas stream is in the range of approx. 10-700 mg / 0.028 m. Subsequently, most of the inherent heat of the gas flow is withdrawn in the main gas cooling zone, which has one or more interconnected gas coolers, each consisting of a jacket and straight heating tubes, ie tubular heat exchangers. Each gas cooler has one or more shell-side and

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pipe-side passages and preferably includes fixed heating tube walls. Compared to the gas coolers that Used in the process set forth herein are the conventional synthesis gas coolers for generation formed by high pressure steam with spiral tubes, helical tubes or coiled tubes. Gas cooler with such coils are difficult to clean and maintain; they are relatively expensive; and there is a risk of constipation, when the solids concentration in the gas is considerable. When serviced boilers with such coils expensive shutdown times result. Advantageously, these problems are addressed in the present Process avoided because here one or more gas coolers are used, each of which has a jacket or a housing and a plurality of parallel straight heating tubes.

In the method, the gas coolers are preferably arranged in such a way that there are two cooling stages, namely a first or high temperature stage and a second or low temperature stage. In the first or high temperature stage, a preferred embodiment comprises one of the jacket and straight heating tubes existing tubular heat exchangers with fixed heating tube walls and with a passage on the Shell and pipe side. The raw gas is on the pipe side and the coolant on the shell side.

03006S / Ö781

Entry and exit ends of the plurality of straight parallel tubes in the tube bundle contained in the pressure vessel are supported at each end by a heating tube sheet. The pipe ends are in flow connection with stationary inlet and outlet heads, ie one at the front and one at the rear end. The inlet and outlet sections and the
Inlet tube sheets are clad heat-resistant. The first
The heat exchanger is designed to be as short as possible in order to simplify the cleaning of the tubes and to minimize the thermal expansion stress acting on the fixed tube sheets. The tube sheets themselves are designed so that they are slightly deflectable in order to eliminate excessive thermal stresses. The pipe outside diameter is that
1.5-2.0 times the outer pipe diameter of the second stage cooler. This is intended to keep the risk of the heat exchanger clogging to a minimum. The gas velocity is set high enough to keep pollution problems within a tolerable range. (Further details of the tube and boiler-side structure of heat exchangers with a fixed tube sheet can be found, for example, in "Chemical Engineers'Handbook", Perry and Chilton,
5th ed., McGraw-Hill Book Co., New York, pp. 11-5 through 11-6, Fig. Ll-2 (b), and pp. 11-10 through 11-18.)

In some embodiments, the second or low temperature stage of the gas cooler have two pipe-side passages or trains and a jacket-side train. This

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The heat exchanger is constructed similarly to that of the first stage; however, because of the lower Clogging problems at lower temperatures pipes with a smaller diameter are used. Through this the surface available for a certain bowl diameter is increased. For example, the pipe outside diameter is in the gas cooler of the first stage 76.2 mm, while in the gas cooler of the second stage z. B. 50.8 mm.

The longitudinal axes of the straight heating tube heat exchangers can be horizontal, vertical or combined in both directions get lost. However, the longitudinal axes of the tubular heat exchangers preferably run in the vertical direction (see the drawing). This results in a gravity separation of entrained solid particles from the gas flow and a allows easy removal of solids from an outlet in the lower end of the gas cooler. Besides, the Inlet into the first gas cooler stage is preferably immediate above the antechamber or any additional separation device for solids that are downstream of the antechamber.

The preferred combination of tubular heat exchangers with a jacket and straight vertical heating tubes as well as with one and two tube-side trains and fixed tube sheet is shown in the drawing and will be explained in more detail below

030065/0781

explained. The hot gas stream is in the first gas cooler stage to a temperature of about 427-649 C, about 482-593 ⁰ C, z. B. approx. 538 ⁰ C, cooled by indirect heat exchange with a coolant, ie boiler feed water or steam. The hot gas stream flows through a bundle of parallel straight pipes. The only pull of the straight tubes distributes the thermal stress evenly over the solid tube sheet. In the second gas cooler stage, the temperature of the gas stream is then reduced to a value that is within approximately -9.4 ° C. to 32.2 ° C., e.g. B. is within about -6.67 C, the selected steam temperature. For example, the second stage gas cooler gas stream leaving a temperature of about 232-310 ⁰ C, z. For example, about 288 ⁰ C. In the second gas cooler stage is effectively increased by using two pipe-trains the length of the pipes at a given coat size. This results in savings in terms of construction. Multiple pulls on the pipe side serve the purpose of reducing thermal stresses on the solid pipe sheet caused by expansion. The required base area or the height is also reduced depending on the orientation of the heat exchanger by means of multiple passes on the pipe side.

In other embodiments, the second or low temperature stage of the gas cooler with one or more heat exchangers comprising a jacket and straight heating pipes include solid tube sheet, with shell and tube side

G3Ö08S / 01S1

one or more trains are provided. The interpretation the second gas cooler stage corresponds to the largest Part of those of the first gas cooler stage, but tubes with a smaller diameter can be used in a second gas cooler stage should be used as there are fewer clogging problems due to the lower temperatures. Through this the surface area available for a given jacket diameter can be increased. For example, the Pipes in the first gas cooler stage have an outside diameter of approx. 76 mm, while in the second gas cooler stage have an outside diameter of approx. 50.8 mm. In a preferred embodiment, the second stage has two Gas cooler on. One gas cooler overheats saturated steam that is generated in the other gas coolers. At a Another embodiment is the superheater in the first Level arranged.

The course of the longitudinal axes of the tubular heat exchanger with jacket and straight heating tubes in the main gas cooling zone can be horizontal, vertical, or both directions. However, the longitudinal axes preferably run (see the drawing) all tube heat exchangers vertical. The upright arrangement creates a gravity separation entrained solid particles from the gas stream and allows solid particles to be easily withdrawn from an outlet in the lower end of the gas cooler. Further lies

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the inlet to the gas cooler of the first stage is preferably un- ' indirectly above the antechamber or any of these downstream additional separation devices for entrained solids.

For the generation of superheated steam in the main gas cooling zone, the preferred combination of gas coolers comprises three interconnected tubular heat exchangers with a jacket and straight vertical heating pipes with one or two pipe-side passes, a jacket-side pass and a fixed tube sheet (cf. the drawing). The structure of this gas cooler will be explained in detail later. In this embodiment, the hot gas stream, which has a temperature of about 64-9-1649 ⁰ C, about 64-9-982 ⁰ C, z. B. approx. 871 C, and a pressure of. 10-200 bar, in indirect heat exchange with boiler feed water upwards through the plurality of parallel straight pipes on the pipe side of the first upright gas cooler, which has a pipe-side and a jacket-side draft. The partially cooled gas stream passes out of the first gas cooler to a temperature of about 593-1093 ° C, such as about 593-871 ⁰ C, z. B. approx. 6 ^ 9 C, from. The coolant, ie boiler feed water from a steam boiler in the first gas cooler on the shell side at a temperature of about 10-316 ⁰ C, for example about 254-316 ° C, for example. B. approx. 299 ⁰ C, initiated and occurs as saturated steam with a temperature of approx. 221-316 ⁰ C,

G3Q065 / 0781

about 254-316 ° C, e.g. B. approx. 299 ⁰ C, from. The saturated data is stored in the steam boiler.

At least a portion, ie 50-100% by volume, about 80-100% by volume, e.g. B. 90 vol .-%, of the gas flow emerging from the first gas cooler is introduced into the second vertical gas cooler as a hot stream. The largest amount of the hot gas flow from the first gas cooler is preferably introduced into the straight tubes of the second gas cooler. The part of the gas that bypasses the second gas cooler is determined by the desired steam temperature when leaving the second gas cooler. The hot gas stream is passed downwardly through the plurality of parallel straight tubes of a train on the pipe and the shell side of second gas cooler in indirect heat exchange with saturated steam and occurs at a temperature of about 454-732 ⁰ C, such as about 454- 732 ⁰ C, e.g. B. approx. 510 ⁰ C, from. At least a part, ie approx. 80-100 vol. 56, e.g. B. about 90 vol .-% of the saturated steam generated in the process, which is stored in the steam boiler, is introduced into the second gas cooler on the shell side as a coolant. Superheated steam is from the second gas cooler with a superheat of approx. 37.8-243 ⁰ C, approx. 37.8-210 ° C, z. B. about 138 ° C, deducted. This superheated steam, which occurs as a by-product, can be used elsewhere in the process as a heating medium or as a working medium in a turbine for generating mechanical and / or electrical energy.

Excess superheated steam can be exported.

The partially cooled gas flow emerging from the second gas cooler is mixed with the remainder of the partially cooled gas flow from the first gas cooler, which bypasses the second gas cooler. This gas stream, which has a temperature of about ή-27-6 ^ 9 ⁰ C, ζ. B. approx. 538 ⁰ C, is led through the plurality of parallel straight tubes of the vertical third gas cooler, which has two pipe-side trains and a jacket-side train, in indirect heat exchange with boiler feed water. The gas stream flows up through the tubes in the first tube side pass and then down through the tubes in the second tube side pass. The partially cooled gas stream leaves the third gas cooler at a temperature of about 232-371 ⁰ C, for example about 266-371 ⁰ C, z. B. approx. 310 ⁰ C. The pressure drop through the main gas cooling zone is approx. 0.07-0.7 bar overpressure. The coolant, ie boiler feed water from the boiler is introduced into the third gas cooler shell side at a temperature of about 10-316 ⁰ C and exits as saturated steam at a temperature of about 221-316 C, for example about 254-316 ⁰ C. , e.g. B. 299 ° C. The saturated steam is stored in the steam boiler.

In the third gas cooler, the length of the pipes for a given is determined by using two pipe-side pulls effectively increased in size, creating structural savings

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are achievable. Pipe-side multiple pulls are used Reduction of thermal stresses that act on the fixed tube sheets as a result of expansion. Also is through Pipe-side multiple passes, the required floor space or the height depending on the orientation of the heat exchanger reduced.

Typically, superheated steam is generated by heating saturated steam in a conventional external / fired heater. In another embodiment of the present method, superheated steam emerging from the second gas cooler is passed through an externally fired heating device in which it absorbs further heat. Due to this combination of steam heating devices, superheated steam with higher temperatures, ie with an overheating of approx. 149-299 ⁰ C, approx. 149-266 ⁰ C, z. B. 221 ⁰ C, are generated. It also minimizes the stress on the fired heater.

As a temperature control for the superheated steam, water can optionally be added to the superheated steam coming from the fired heating device leaks, are injected to thereby lower the degree of overheating, while that of the heater the amount of fuel to be supplied is set.

03006S / 0761

The second and third gas coolers in the low-temperature stage are designed so that they have a maximum inlet gas temperature withstand. If z. B. dirty the pipes of the first gas cooler in the high temperature stage are, so that the temperature of the gas flow emerging from the first gas cooler rises, is optionally a Steam injection auxiliary circuit provided, which the second and third gas cooler protects against damage. So if the temperature of the inlet gas is a safe maximum temperature exceeds, a temperature sensor in the gas inlet line of one or both gas coolers activates one Temperature regulator so that it opens a shut-off device in the high-pressure steam auxiliary line. The control valve will is opened and steam is injected into the hot gas stream, reducing the gas temperature.

In the present process, the term "heating tube" means that the hot gas is always parallel through the series straight pipes of the gas cooler is guided. The coolant flows on the shell side. The coolant flow in the Gas cooler is controlled by the following elements: one or more inlet and outlet nozzles and their positioning; Number, positioning and design of cross baffles, partitions and stowage devices. Baffles do not serve only directing the shell-side coolant on a predetermined path, but are usually also used for this used to support the straight tubes in the tube bundle.

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For the gas coolers affected here, tubes with a small outer diameter (25.4-10.1 mm) can be used. Of the Pipe diameter is determined on the basis of an economic analysis of the effect of the diameter on the Heat transfer, the pressure drop and the risk of contamination and clogging. Long tubes offer considerable structural savings at higher pressures, since the investment per unit area of the Heat transfer performance is lower with longer heat exchangers. The gas and coolant flow rates in the heat exchanger are limited in order to avoid mechanical damage due to vibrations or erosion, to maintain a tolerable pressure gradient and to keep the formation of deposits under control. For example, the flow rate of the hot gas through the straight tubes can be 50.8 mm approx. 12.2-16.7 m / s depending on the temperature and pressure at any particular point in the Heat exchanger. Larger diameter pipes are used when heavy pollution is expected and to facilitate the mechanical cleaning of the inside of the pipe. The fastening of the pipes to the pipe sheet takes place z. B. by a combination of pipe end welding and expansion by rolling. The pipes can with Triangular division, square division or twisted square division be arranged. The center distances, the pipe spacing,

03006S / 0761

The type and spacing of the baffles are chosen so that there is good coolant circulation while avoiding hotter Places on the inlet pipe bottom results. Usually the jacket of the heat exchanger used here consists of Quality carbon steel. When generating high pressure steam or is overheated, alloy steels can be used, on the one hand, to achieve the required jacket thickness reduce and, on the other hand, lower the costs of the system,

The inlet and outlet sections of the gas cooler are usually made of alloy steels, because of the temperature and the hydrogen partial pressure im Raw gas. Pipe materials are usually made of the same Reasons alloy steels; however, in some cases the last passes of the second gas cooler stage are made of carbon steel. The flow path between The jacket-side and pipe-side fluids can be countercurrent, cocurrent or a combination of both types of flow.

The size of the heat exchanger and thus its costs Factors include: Pressure drop, gas composition, gas and coolant flow rates, the logarithmic Average of temperature differences and pollution factors. An optimal heat exchanger design is that Function of a large number of the interacting parameters discussed above.

030065/0761

Although any suitable liquid or gaseous coolant can be passed through the shell side of the gas cooler, boiler feed water or steam are preferred as the coolant. Characterized bar can be generated as a byproduct of saturated steam or superheated steam having a temperature of about 271-482 ⁰ C and pressures of approximately 100, which is used either in the system or can be exported.

By guiding the hot, solids-containing gas flow through the straight tubes of the gas cooler explained, the following advantages are achieved compared to conventional synthesis gas coolers with tube coils: 1) heat transfer due to less pollution, higher heat transfer capacities are achieved; 2) pollution - pollution is reduced due to the flow velocities of the hot gases through the pipes; the straight pipes allow mechanical cleaning; 3) Pressure Drop - less pressure drop due to a reduced number of bends and less chance of clogging; and k) costs reduced manufacturing costs through simpler construction,

The gas stream leaving the main gas cooling zone can be used as synthesis gas, as reducing gas or as heating gas will. Alternatively, the inherent heat remaining in the gas flow can be stored in one or more exhaust gas preheaters, i. H. Heat exchangers, by preheating boiler feed water

030065/0761

be pulled. Further entrained solid particles can then be removed from the gas stream by washing with water in a carbon scrubber. This further reduces the concentration of entrained solids to less than 2 mg / m. The cleaned gas stream leaving the carbon scrubber and saturated with water is then dewatered. The gas flow is cooled to a temperature below the dew point by indirect heat exchange with boiler feed water or purified heating gas. Condensation water is separated from the gas flow in a separator drum. The condensate is returned to the carbon scrubber, optionally with the addition of additional water, and used as a final stage detergent. The emerging from the upper end of the discharge drum purified gas stream has a temperature of about 93 to 316 ⁰ C, such as about 135 to 204 · ⁰ C, z. B. approx. 171 ° C. A portion of this purified gas stream, namely about 0-80% by volume, about 30-60% by volume, e.g. B. approx. 50 vol .-%, is compressed to a higher pressure than the pressure in the antechamber. The compressed gas stream is recirculated to the antechamber, where it is introduced into the lower quenching chamber as quenching gas. The remaining cooled, purified gas stream is withdrawn as product gas from the upper end of the separator drum.

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If a bleed gas flow is used in the gas deflection chamber, it is also cooled and washed together with the main gas flow in the gas scrubbing zone. The bleed gas flow, which is separated from the main gas flow in the gas deflection chamber, is passed through the lower outlet of the gas deflection chamber and then through a submerged pipe which leads out under water and is connected to the outlet. As a result, the bleed gas stream and separated molten slag and / or solid particles are cooled in the water contained in the lower end of the quenching chamber. The quench water may have a temperature of about 10 to 316 ⁰ C. If necessary, the hot quenching water can be used on its way to a carbon recovery unit to preheat one or more feed streams of the gas generator by indirect heat exchange. After quenching, the bleeding gas flow has a temperature of approx. 93-316 ° C.

A large number of ash-containing, combustible, carbon-containing solid fuels can be used in the present process. The term carbonaceous solid fuel, as described here for various suitable input materials includes 1) pumpable suspensions of solid carbonaceous fuels; 2) gas-solid suspensions, z. B. finely ground carbonaceous solid fuels, either in a temperature moderating gas, a gaseous hydrocarbon or a free acidic

030065/0761 '".

substance-containing gas are dispersed; and 3) gas-liquid-solid dispersions such as atomized liquid hydrocarbon fuel or water and carbonaceous solid fuel dispersed in a temperature moderating gas or a gas containing free oxygen. The carbon-containing solid fuel can be subjected to partial oxidation either by itself or in the presence of a heat-liquefiable or vaporizable hydrocarbon or a carbon-containing material and / or water. Alternatively, the carbonaceous solid fuel, which is free of surface moisture, can be supported by a gaseous carrier such as steam, C0_, N _? , Synthesis gas or a gas containing free oxygen can be taken into the gas generator. Carbon-containing solid fuels are z. B, coal such as hard coal, fat coal, semi-fat coal, coke of coal and brown coal; Oil shale; Tar sands; Petroleum coke; Asphalt; Bad luck; Carbon particles (soot); concentrated sewage sludge; and mixtures of these materials. The carbonaceous solid fuel can be ground to a particle size of 12.5 mm (ASTM Ell-70 Sieve Designation Standard (SDS)) to 75 μm (Sieve No. 200). Pumpable masses of carbonaceous solid fuels can have a solids content of approx. 25-65% by weight, e.g. B. 45-60 wt .-% depending on the properties of the fuel and the slurry medium. The latter can be water, liquid hydrocarbon, or both.

030065/0761

The term liquid hydrocarbon includes im present context the most diverse materials, such. B. liquefied petroleum gas, petroleum distillates and - residues, gasoline, naphtha, kerosene, crude oil, asphalt, gas oil, residual oil, tar sand and shale oil, derived from coal Oil, aromatic hydrocarbons (e.g. benzene-toluene and xylene fractions), coal tar, cycle gas oil from FCC processes, furfural extract from coker gas oil, and Mixtures of the same. The definition of liquid hydrocarbons also includes oxygen-enriched ones substances containing hydrocarbons such as carbohydrates, cellulose derivatives, Aldehydes, organic acids, alcohols, ketones, fuel oil enriched with oxygen, waste water and by-products from chemical processes, the oxygen-enriched hydrocarbonaceous organic Contain materials, and mixtures thereof.

The use of a temperature moderator to moderate the temperature in the reaction zone of the gas generator is optional and usually depends on the carbon / hydrogen ratio of the feed material and the oxygen content of the oxidant stream. Suitable temperature moderators are e.g. B. H-O, high-CO_-containing gas, liquid CO-, part of the cooled, cleaned exhaust gas from a gas turbine connected downstream in the process with or without admixture of air, by-product nitrogen from the air

030065/0761

separation device, which is used to generate essentially pure oxygen, and mixtures of the aforementioned temperature moderators. No temperature moderator is required for slurries of water and carbonaceous solid fuel to be fed. However, with slurries of liquid hydrocarbon fuels and carbonaceous solid fuel, steam can be used as a temperature moderator. Typically, a temperature moderator is used with liquid hydrocarbon fuels and essentially pure oxygen. The temperature moderator is introduced into the gas generator as an admixture with either or both of the solid carbonaceous fuel feed stream or the free oxygen containing stream. Alternatively, the temperature moderator can be introduced into the reaction zone of the gas generator through a separate line in the burner. If additional H _? 0 is introduced into the gas generator either as a temperature moderator, as a slurry medium or both, the weight ratio of the make-up water to the carbon-containing solid fuel plus, if applicable, the liquid hydrocarbon-containing fuel is preferably in the range of approx. 0.2-0.5.

The term free oxygen-containing gas includes in the present context air, enriched with oxygen Air, d. H. with more than 21 mol-56 oxygen, and

030065 / Q761

essentially pure oxygen, ie with more than 95 mol% oxygen (remainder N ₂ and noble gases). Gas containing free oxygen can be introduced into the burner at a temperature of approximately ambient to 64-9 ° C. The atomic ratio of free oxygen in the oxidizing agent to carbon in the feed stream (O / C ratio) is preferably in the range of about 0.7-1.5, e.g. B. approx. 0.85-1.2.

The relative proportions of carbonaceous solid fuel, optionally liquid hydrocarbon fuel, water or another temperature moderator and oxygen in the feed streams supplied to the gas generator are carefully adjusted so that a very large part of the carbon, e.g. B. at least 80 wt. 56, in carbon oxides, e.g. B. CO und'CO-, converted and an autogenous reaction zone temperature in the range of about 927-1704 · ⁰ C is maintained. For example, in one embodiment, using a feed stream from a coal-water slurry with a working slagging gas producer at a temperature of about 1260-1538 ⁰ C operated. With the same fuel one working with fly ash seizure coal gasifiers can operate of about 927-1149 ⁰ C at a lower temperature. The pressure in the reaction zone is in the range from approx. 10-200 bar. The residence time in the reaction zone is about 0.5-50 s, e.g. B. approx. 1.0-10 s.

030065/0761

The gas stream emerging from the partial oxidation gas generator has the following composition in mol%: 8.0-60.0 H ₂ , 8.0-70.0 CO, 1.0-50.0 CO ₂ , 2.0- 50.0 H ₂ O, 0-30.0 CH ₄ , 0.0-2.0 H ₂ S, 0.0-1.0 COS, 0.0-85.0 N ₂ and 0.0-2 , 0 A. Approx. 0.5-20% by weight of carbon particles (based on the weight of the carbon in the feed stream fed to the gas generator) are carried along in the exiting gas stream. Molten slag and / or fly ash resulting from the amalgamation of the ash content of the coal, particles of refractory material from the walls of the gas generator and other solid particles can also be entrained in the gas stream exiting the gas generator.

The present process achieves the following advantages: 1) About 90-99.9 % by weight of the molten slag and / or solid particles that are entrained in the hot gas stream emerging from the partial oxidation gas generator can be separated off. 2) Essentially the entire inherent heat of the hot raw gas flow emerging from the partial oxidation gas generator is used, whereby the thermal efficiency of the process is increased. 3) By-product steam is generated at high temperature. The steam can be used elsewhere in the process, ie for heating purposes, for generating energy or in the gas generator. Alternatively, part of the by-product steam can be exported, ή ·) Molten slag and / or

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302U69

Particles of the carbonaceous solid fuel can be deposited in a simple manner in front of the gas cooler. This causes contamination of the heat exchanger surfaces prevented. 5) One or more gas coolers, consisting of a jacket and straight heating pipes, are used, which are relatively inexpensive to manufacture. By designing this gas cooler, thermal stresses can be uniform be distributed on the tube sheets, the cleaning and maintenance of the tubes is simplified, and the required The footprint and the height of the gas cooler are minimized.

In the following, reference is made in particular to the drawing. Fig. 1 shows a device according to the invention for quenching, cooling and cleaning a hot raw gas stream containing solids and slag, while Fig. Figures 2 and 3 respectively show two systems in each of which such a device is used. The same parts are in the systems according to FIGS. 2 and 3 are provided with the same reference numerals.

According to FIGS. 2 and 3, a slurry of hard coal with a diameter of 6.3 mm in water with a solids content of 40% by weight is conveyed by a pump 2 through line 3 into a heat exchanger k through line 1. The temperature of the coal sludge is increased in the heat exchanger k from room temperature to approx. 93 ° C, through indirect heat exchange with quenching water.

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The quenching water enters the heat exchanger ^ through the Line 5 in and out through line 6 after it has given off heat to the coal slurry. The warmed Coal sludge is then passed through line 7 and into annular passage 8 of burner 9. The burner 9 is arranged at the upper inlet 10 of the synthesis gas generator 11. At the same time a gas stream containing free oxygen, e.g. B. essentially pure oxygen, from the Line 12 is heated by indirect heat exchange with steam in the heat exchanger 13 and flows into the gas generator through the pipe 14 · and the central pipe 15 of the burner 9.

The synthesis gas generator 11 is a freely flowable steel pressure vessel with the following main sections: one Reaction zone 16, a gas turning chamber 17 and a quenching chamber 18. The reaction zone 16 and the gas turning chamber 17 are lined with heat-resistant lining on the inside. Alternatively, these three main sections can consist of two or more separate and interconnected units in flow communication.

The vertical center axis of the upper inlet 10 is aligned with the vertical center axis of the gas generator 11. The feed streams participating in the reaction meet, and the partial oxidation takes place in the reaction zone 16. A hot raw gas stream, the entrained molten

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zene slag and / or particulate matter including unconverted carbon and particles of refractory Contains material, flows through the axially aligned opening 19 in the lower end of the reaction zone 16 and occurs into a larger gas deflection chamber 17. The flow velocity and direction of the hot gas flow are in the gas deflection chamber 17 changed abruptly. A small part, i. H. a bleed stream of the raw gas is optionally withdrawn through the lower constriction 20 of the gas deflection chamber 17 and a dip tube 21 in water 22, which is in the lower end of the Quenching chamber 18 is present. This keeps the outlet 20 open, some of the molten slag and / or particulate matter is quench cooled and the slag can be solidified. Solid particles become periodically and ash from quench chamber 18 through lower axially aligned outlet 23, conduit 24, the shut-off element 25, the line 26, the lock funnel 27, the line 28, the shut-off element 29 and the line 3.0 deducted. Ash and other solids are removed from the quench water through an ash conveyor 31 and a sump 32 separated. The ash is discharged through line 33 for use as a filler. Quenching water is made from the Sump through the line 3A-, the pump 35 and the line 36 withdrawn and can be recycled to the quenching chamber. Some of the quench water is from the lower end withdrawn from the quench chamber through an outlet 37

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and passed through the line 5, as already explained, into the heat exchanger 4. The one containing carbon chilled quench water in line 6 is drained into a conventional carbon separation unit (not shown) for the recovery of the quenching water through a pipe 38 led. The recovered carbon is then added to the coal sludge as part of the feed stream to the gas generator added. Any bleed gas is discharged from the quenching chamber 18 through a side outlet 39, the line 40, a shut-off element 41 and the line 42 discharged.

The hot raw gas flow leaving the gas deflection chamber 17, from which part of the molten slag and / or the Solid particles is deposited, is directed through the heat-resistant lined lateral outlet channel 43 and then up through a heat-resistant lined transmission line 44 and an inlet 45 of the antechamber 46 (details can best be seen from FIG. 1). Alternatively, in some embodiments, this may be hot Raw gas flow through a solids and slag pre-separator 11A, e.g. B. a conventional slag catcher out before it enters the inlet 45 (see. Fig. 1). The antechamber 46 is a closed cylindrical vertical one Steel pressure vessel, the interior of which is completely lined with refractory material 47 and the one lower solids separation chamber 48, one coaxial therewith upper solids separation chamber 49 and a coaxial one Has heat-resistant throttle ring 50. The throttle ring 50

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forms a cylindrical passage of reduced diameter between the lower chamber 4-8 and the upper one Chamber 4-9. The antechamber 46 has a conical lower end 51 which converges into a heat-resistant lined coaxial lower outlet 52. A hemispherical one Dome 53 at the top of the container 46 has a heat-resistant lined upper outlet 5A-. The outlet 54 is coaxial with the vertical axis of the container 46. Two opposed coaxial inlet nozzles lined with heat resistant coating 4-5 and 55 run through the container wall and are directed into the lower chamber 48. The longitudinal axis of the Inlet nozzles 4-5 and 55 form an angle between approx. 30 and 150 with the vertical center axis of the container 46, measured clockwise from that axis, and lies in the same plane. This angle is preferably z. B. approx. 45 and approx. 60. The inlet nozzle 4-5 for introducing a hot raw gas flow is directed upwards. The inlet nozzle 55 for introducing a stream of purified and comparatively cooler cycle quenching gas is directed downward. In the drawing there are only two inlet nozzles shown, but multiple pairs can be provided.

In the preferred embodiment is in the upper chamber 49 at least one cyclone 56, the vertical longitudinal axis of which either parallels the vertical axis of the container 46

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runs parallel or coaxial, arranged. Each cyclone is heat-resistant and abrasion-resistant and has a gas inlet 57 near the top of the upper chamber. If multiple cyclones are used, these be provided equidistantly in the chamber. The front of the square inlet 57 of the cyclone 56 is preferred parallel to the vertical axis of the container 46. The inlet is oriented to face the direction of the inflowing Facing the gas. This means that the cyclone inlet or the cyclone inlets can be oriented in such a way that that the vortex direction is continuous.

The cyclone 56 is of conventional design with a cylindrical body, a conically tapered lower portion, a turning chamber, an exit pressure chamber connected to the upper outlet 54, a dip tube 58 and a valve near the bottom of the dip tube. The dip tube 58 can be offset so that it runs close to the wall of the container 46, whereby it is avoided that it intersects the common longitudinal axis of the inlet nozzles 45 and 55. This prevents the immersion tube from being contacted by uncooled slag particles or from accumulating on the immersion tube. Cooled, purified synthesis gas is discharged through the upper outlet 54. Solid particles are discharged through the lower outlet 52 via a line 59, a shut-off device 60 and a Lelfcung $ \ , and in. Eifven SoUlcusQU-

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Optional are 1-4 tangential quench gas inlets 62 equally spaced around the circumference of the container 46, e.g. B. near the top of the lower chamber 48 and / or the Lower end of the upper chamber 49 is provided. This allows an additional amount of cooled in the container 46 pure cycle quenching gas can be introduced. The clockwise spiral flow direction of the circulating gas stream helps direct all gases in the container upwards. It also makes a cooler Maintain gas flow along the wall of the container 46, whereby the heat-resistant lining is protected. The cooled, pure recycle gas stream entering the inlet nozzle 55 and possibly the tangential inlets 62 can be introduced, contains at least a portion of the cooled clean gas stream from the line 63.

When the solids concentration or the particle size of the Solids in the container 46 from the upper outlet 54 exiting gas flow is to be further reduced, the gas flow in line 64 can optionally be converted into a conventional solids separation zone 64A are passed, which can lie outside the container 46. For this purpose, cyclones, impact separators, bag filters, electrostatic Separators or combinations of these devices are used. They are connected to the antechamber and are in front of the main gas cooling zone.

030065/0761

In the embodiment according to FIG. 2, most of the inherent heat of the gas flow exiting the antechamber is withdrawn in the main gas cooling zone, which preferably has two vertically arranged heat exchangers 65 and 66, each consisting of a jacket and straight heating pipes, which are connected in series . The two gas coolers 65 and 66 have fixed tube sheets, namely a lower tube sheet 61 and an upper tube sheet 68. Both gas coolers 65 and 66 have a passage on the jacket side; the gas cooler 65 has a pipe-side passage, while the gas cooler 66 has two pipe-side passages.

The hot gas stream emerging from the container 4-6 or optionally from an additional solids separation unit (not shown), which is connected downstream of the container 4-6, is cooled by moving it upwards through a lower inlet nozzle 69 into a heat-resistant lined lower hood 70 stationary head, past the lower fixed tube sheet 67, through a tube bundle 71 consisting of a plurality of parallel straight vertical tubes positioned in a jacket 72, past the upper fixed tube sheet 68, into an upper hood 73 with a stationary head , passed through connecting channels 74 and into the left side 75 of the upper hood 76 with the stationary head of the second gas cooler 66 . A central baffle

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divides the upper hood 76 into a left half 75 and a right half 78. The gas flow in the left half 75 is past the upper fixed tube sheet 68 down through the left row of parallel straight tubes 79, through the lower fixed tube sheet 67, in the lower hood 80 with stationary head, passed upwards through the right row of parallel straight vertical tubes 81, into the right half 78 of the upper hood 76 with stationary head and through the upper outlet nozzle 82 in the stationary head into the conduit 83. Solid particles falling into the lower heads 70 and 80 of the gas coolers 65 and 66 , respectively, are discharged through lower outlets, e.g. B. a flanged nozzle 8A of the gas cooler 66, withdrawn. The drawing shows an expedient arrangement for introducing a coolant, in this case boiler feed water, into each of the two gas coolers 65 and 66 . By-product steam is generated in gas coolers 65 and 66 and stored in steam drum 90. Boiler feed water from drum 90 flows through line 91 and inlet nozzle 92 into the shell side of gas cooler 65. Steam is withdrawn from gas cooler 65 through outlet nozzle 93 and passed through line 94- into steam drum 90. Likewise, boiler feed water from the steam drum 90 is passed through the line 95 and the inlet nozzle 96 into the shell side of the gas cooler 66 . Steam is withdrawn from gas cooler 66 through outlet nozzle 97 and directed into the steam drum through line 98. Preheated boiler feed

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water is passed through line 99 into steam drum 90 introduced. Saturated steam is passed through the steam drum 90 the line 100 removed. This steam can be used elsewhere in the process, e.g. B. as a heat medium in Heat exchanger 13 or as a temperature moderator in the gas generator 11 or as a working medium in a steam turbine (not shown) for generating mechanical and / or electrical energy. Alternatively, the saturated steam get overheated.

Further entrained solids and inherent heat are from the * from the second gas cooler through the outlet 82 and the Line 83 removed the exiting gas stream by passing the gas stream through an exhaust gas preheater 101, a line 102 and fed into a carbon scrubber 103.

In the embodiment of FIG. 3, the largest Part of the inherent heat of the gas flow leaving the container or the antechamber is taken in the main gas cooling zone, in the preferred embodiment three vertically arranged Tubular heat exchangers 65, 66 and 67 with jacket and straight heating tubes includes. These three gas coolers show solid tube sheet, d. H. upper tube sheet 68 and lower tube sheet 69, on. While the gas cooler 65 and 66 have a pipe-side and a jacket-side passage, has the gas cooler 67 has two pipe-side passages and one jacket-side passage.

030065/0761

The hot gas flow from the antechamber 46 or optionally from an additional solids separation unit (not shown), which is connected downstream of the antechamber 4-6, is cooled by flowing upwards through the line 64 and the lower inlet nozzle 70 of the gas cooler 65 into the heat-resistant lined lower one Hood 71 with a fixed head, past the lower fixed tube sheet 69, through the tube bundle 72, consisting of a plurality of parallel straight vertical tubes within a jacket 73, past the upper fixed tube sheet 68, into the upper hood 74 with a stationary head, through upper outlet 75 and into line 76. The coolant in the gas cooler 65 is boiler feed water and saturated steam. Boiler feed water from the steam drum 77 is conveyed by a pump 78 through lines 79-81 and into the lower inlet 82 of the shell side of the gas cooler 65. Saturated steam exits the shell side of the gas cooler 65 through the upper outlet 83 and flows through the line 84 into the steam drum 77. At least a portion of the saturated steam leaves the steam drum 77 through the line 85 and enters the gas cooler 66 as coolant through the line 86 and the inlet 87 out. Any remaining saturated steam is passed through line 88, shut-off element 89 and line 90. This steam can advantageously either be used in the process or exported. For example, part of this steam can be used as a heat medium in the heat exchanger 13,

03006570761

Most of the partially cooled gas flow in line 76 is passed into vertical gas cooler 66 as a heat medium for superheating saturated steam by indirect heat exchange. The gas enters the upper hood 95 through line 91, valve 92, line 93 and an upper inlet. The gas is then passed on the tube side through the upper tube sheet 68, down through the bundle of straight parallel tubes 96 in the jacket 97, past the lower tube sheet 69, through the lower hood 98 and through the lower outlet 99 out into the line 100. Saturated steam from line 86 is introduced through inlet 87 of gas cooler 66 and flows upward on the shell side. By-product superheated steam is withdrawn through upper outlet 4-61, lines 462, 463, valve 464 and line 465. The by-product superheated steam can, within the process, e.g. B. can be used as a working medium in an expansion turbine for generating mechanical or electrical energy. In another embodiment, at least a portion of the superheated steam from the line 462 is passed through the line 166, the shut-off element 167 and the line 168 into an externally fired heating device 169, in which the temperature of the superheated steam supplied is increased. Higher temperature by-product superheated steam leaves heater 169 through lines 170 and 171. The superheating temperature of the steam can be controlled by injecting water through line 172, valve 173 and line 174.

030065/0761

In one embodiment, the one exiting gas cooler 65 is Gas flow for fine adjustment to increase the temperature of the gas flow passing through the gas cooler 66 the line 100 leaves, used. This is achieved by removing a small portion of the gas flow in line 76 through the line 175, the shut-off device 176 and the line

177 is performed and the two gas streams in the line

178 are mixed.

Additional saturated steam can be generated in gas cooler 67 by gas flow in line 178 through line 179, lower inlet 180 into left side 181 of lower hood 182, up past lower solid tube sheet 69 , up through left passage on FIG Tube side 183, into the upper hood 184, down through the right passage on the tube side 185, into the right side 186 of the lower hood 182 and through the lower outlet 187 into the line 188. The gas stream is conducted in the line 80 from the steam drum 77 in indirect heat exchange with part of the boiler feed water. The boiler feed water is fed through the line 200, the shut-off element 201, the line 202 and the lower inlet 203 into the jacket side of the gas cooler 67 having a passage. Saturated steam leaves the gas cooler 67 through the upper outlet 20A- and is fed through the line 205 into the steam drum 77.

030065/0761

Solid particles that fall into the lower hoods 71 or 98 or 182 of the gas cooler 65 or 66 or 61 can pass through lower outlets, e.g. B. the flanged outlet 206 of the gas cooler 67, are withdrawn.

An auxiliary vapor injection system is provided to control the temperature of the gas entering gas coolers 66 and 67. The temperature of the gas flowing into the gas cooler 66 through the line 93 is sensed and a temperature sensor activates a temperature controller 190 which opens a valve 191, the amount of steam from the lines 192 and 193 required to cool the gas flow from the line 76 is hiring.

Likewise, the temperature of the in the gas cooler 67 detected through the line 179 inflowing gas, and a temperature sensor activates a temperature controller 19A-, the a valve 195 opens, which controls the amount of steam from lines 196 and 197, which is used to cool the gas flow from the line 178 is required. Advantageously, will the steam for the operation of the auxiliary steam injection system generated internally.

More entrained solids and inherent heat are the gas flow, the gas cooler 67 through the outlet 187 and the Leaves line 188, thereby withdrawn in that the gas stream

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is passed through an exhaust gas preheater 101, a line 102 and into a carbon scrubber 103.

In both embodiments, the carbon scrubber comprises 103 a two-section container with an upper chamber 104-, and a lower chamber 105. The Gas flow in line 102 is through inlet 106 into lower chamber 105 and then through dip tube 107 in a water bath 108 is guided in the lower end of the lower chamber 105. The gas stream, which has been washed once, leaves the lower one Chamber 105 through outlet 109 and is passed through lines 110 and 111 into a venturi scrubber 112. there the gas stream is washed with water from line 116. The scrubbed gas stream from venturi scrubber 112 becomes into upper chamber 104 through line 117 and the inlet 118 headed. The gas stream is then passed through the immersion tube 119 into a water bath 120 and washed. Before exiting the upper chamber 104 through the upper outlet 121 in the upper end of the chamber 104 can the gas stream can be washed again by spray water 122 or by a wash tray (not shown). E.g. For example, condensate 123 may be passed from the lower end of separator drum 124 through line 125 and through the inlet be passed into the spray device 122. Water from the water bath 120 is passed through line 127, outlet 128, the Line 129, the pump 130, lines 131 and 132, the inlet

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Il -

133 and line 134 into the quench chamber 18. Some of the water in line 131 can be in the Circuit to the lower chamber 105 of the gas scrubber 103 through the line 135, the shut-off element 136, the lines 137 and 138 and inlet 139 are returned. Another part of the water in line 137 is through the line IA-O passed and with make-up water from line 14-1, the The shut-off element 14-2 and the line 14-3 in the line 116 are mixed. The water in line 116 is introduced into venturi scrubber 112 as previously discussed. Water containing dispersed solids 108 from the bottom of chamber 105 is passed through outlet 14-4, the conduit 14-5, the shut-off element 14-6, the line 147 and in the line 38 mixed with the water dispersion from the line 6. The water dispersion in line 38 is a conventional carbon recovery device (not shown) fed, in which the water is separated from the entrained solids. The recovered Water is returned to the system as make-up water. The make-up water can be used in various places, e.g. 3. through the line 14-1, as mentioned, can be introduced.

The purified gas stream that makes up the upper chamber 104 of the carbon Washer 103 leaves through the upper outlet 121 and line 155, is passed through the preheater 156, in which it is cooled to a temperature below the dew point. The wet gas stream flows through line 157 into the waste

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separator drum 124 ·, in which the condensed water from the gas flow is deposited. A cooled and purified product gas stream emerges from the separator drum 124- lines 158 and 159. Optional - but preferred if the gas generator 11 works with slag accumulation a part of this cooled and purified product gas stream through the line 160, the shut-off element 161, the Line 162, the gas compressor 163 out and in the circuit as a quenching gas flow to the lower chamber 4-8 of the container 4-6 through the line 63 and the inlet 55 and optionally through the tangential gas inlets 62.

Additional boiler feed water for cooling the tube heat - exchangers 65 and 66 with coats and straight tubes is thereby preheated that the through line 164-, as coolant through the feedwater preheater 156, through line 165, as a coolant through the feedwater preheater 101, by Line 99 and into the steam drum 90 is passed. From there, the boiler feed water is distributed to the gas coolers 65 and 66, as explained.

030065/0761

Claims (1)

= 3 O? A 4 6 Claims 1. Process for the partial oxidation of ash containing carbonaceous solid fuel for the production of a purified stream of synthesis gas, heating gas or reducing gas characterized by the following steps: 1) Reacting particles of the solid fuel with a gas containing free oxygen with or without a temperature moderator in a heat-resistant lined downdraft gas generator at a temperature of approx. 927-17 (H ⁰ C and a pressure of approx. 10-200 bar to obtain a Raw gas stream of H-, CO, CO- and at least one of the substances H_0, HS, COS, CH., NH, N- or A, which contains molten slag and / or solid particles; 2) Passing the raw gas flow through a heat-insulated transmission line and a first gas inlet into the lower chamber of a gas-solids separation zone comprising: - a closed vertical cylindrical thermally insulated Pressure vessel with the lower chamber that is coaxial with the vertical center axis of the pressure vessel, and with a coaxial upper chamber in 030065/0761 ORK3INAL INSPECTED Flow connection with the lower chamber, wherein the lower and upper chambers are connected to one another via a coaxial throttle ring passage, wherein a part of the slag and / or the solid particles is separated by gravity and for The lower end of the lower chamber falls; 3) Passing the gas mixture from the lower chamber upwards through the throttle ring passage into the upper chamber in the Countercurrent with slag droplets and possibly further into a gas-solid separation unit positioned in the upper chamber; 4) Separation of slag and / or solid particles the gas mixture in the upper chamber and withdrawing it from the container through an outlet in the bottom the lower chamber; and 5) Withdrawing purified gas from the upper chamber and discharging the gas through an outlet at the top of the vertical pressure vessel. 2. The method according to claim 1, characterized by the following additional step: simultaneous routing of an oppositely directed Flow of cooled and purified cycle gas through a second gas inlet coaxial with the first gas inlet into the lower chamber to form a swirled gas mixture when the two gas flows meet, 03Ö06S / G761 - the molten slag entrained in the hot gas stream below the initial deformation temperature is cooled, separated by gravity and falls to the bottom of the lower chamber. 3. The method according to claim 2, marked by Introducing a portion of the purified gas stream from step 5) with further cooling and with or without further downstream Purification in the lower chamber in step 2) as at least part of the cycle gas. 4-. Method according to claim 2 or 3, characterized, that in step 2) the hot gas stream and the cooled and cleaned circulating gas stream into the lower chamber introduced by a plurality of pairs of first and second coaxial, oppositely directed inlets will. ζ. Method according to claim Ί, characterized, that the longitudinal axis of the first and second coaxial, oppositely directed inlet is in the same plane how the vertical center axis of the pressure vessel lies, and that the longitudinal axis coincides with the vertical center axis, G3Ö06S / 0761 • If clockwise starting from this, an angle of forms approx. 30-150 °. 6. The method according to any one of claims 2-5, characterized by the further step of compressing the purified circulating gas stream to a higher pressure than in the lower chamber before introducing this gas flow in step 2) into the lower chamber. 7. The method according to any one of the preceding claims, characterized by the further step of introducing a portion of the cooled and purified gas stream into the top of the lower chamber and / or the lower end of the upper chamber through tangential inlets. 8. The method according to any one of the preceding claims, characterized by the further step of introducing part of the purified gas stream from step 5) into a gas cooler in indirect heat exchange with H-O to generate steam. 9. The method according to any one of the preceding claims, characterized in, that the upper chamber of the gas-solids separation zone in Step 2) at least one gas-solid separation unit 030065/0761 has a single or multi-stage cyclone, a gas impact separator, is a filter or combinations of these devices. 10. The method according to any one of the preceding claims, characterized by the further steps: Passing the raw gas stream from step .1) down through the central outlet in the lower end of the reaction zone in a thermally insulated gas turning chamber having a side and a lower outlet; Gravity separation of molten slag and / or solid particles from the gas stream; Leading approx. 0-20% by volume of the gas flow as bleeding gas together with the separated substances through the lower Outlet of the gas deflection chamber into a slag chamber located below, and the rest of the gas flow is passed through a side outlet channel in the gas deflection chamber directly into the heat-insulated transmission line. 11. The method according to claim 10,
characterized, that the slag space in the lower end contains a quenching water bath. 12. The method according to claim 11,
characterized, 030065/0761 ORIGINAL INSPECTED that the separated molten slag and / or the solid particles with or without bleeding gas through a Immersion tube can be led into the quenching water. 13. The method according to any one of the preceding claims, characterized by the further steps: Cooling the gas stream from step 5) in a main gas cooling zone and generating by-product vapor by conducting of the gas flow in indirect heat exchange with preheated boiler feed water - first up through the tubes of a vertical high temperature gas cooler with jacket and straight heating pipes, the heat-resistant lined inlet and outlet sections, has a jacket-side and a tube-side passage as well as a fixed tube sheet, - Then down through the tubes in the first tube-side passage of a vertical low-temperature gas cooler with jacket and straight heating pipes, the two pipe-side passages and one jacket-side passage as well as fixed ones Has tube sheet, and - then up through the tubes in the second tube-side passage of the second gas cooler; Removing by-product vapor from the shell sides of the first and second gas coolers. 01006 5 / 0-761 ORK3INAL INSPECTED T-302U69 IA-. Method according to claim 13, characterized by the next step of preheating the boiler feed water by indirect heat exchange with the gas flow leaving the second gas cooler. 15. The method according to claim IA, characterized by washing the cooled gas stream with water in the gas washing zone to produce a carbon-water dispersion; Mixing at least a portion of the carbon-water dispersion with or without concentration and adding solid fuel to obtain a solid fuel slurry;
Preheating; and Gasifying the solid fuel slurry in the gas generator in step 1). 16. The method according to claim 15, characterized by directing part of the purified gas stream after it Drainage through an expansion turbine to generate mechanical and / or electrical energy. 17. The method according to claim 13, characterized by 030065/0761 simultaneous passage of separate amounts of preheated boiler feed water from a steam drum through the shell sides of the high and low temperature gas cooler and passage of the steam thus generated into the steam drum; and
Removing by-product saturated steam from the steam drum. 18. The method according to any one of claims 1-12, characterized by
the additional steps: Cooling the gas stream from step 5) in a main gas cooling zone and generating by-product saturated steam and -Hot steam by conducting the gas flow in indirect heat exchange with preheated boiler feed water - first upwards through the pipes of a first vertical high-temperature gas cooler with jacket and straight heating pipes, the heat-resistant lined inlet and outlet sections, a shell-side and a pipe-side passage and has solid tube sheets, - Then in indirect heat exchange with saturated steam downwards through the pipes of a second vertical gas cooler Jacket and straight heating pipes, which has a pipe-side and a jacket-side passage and a fixed tube sheet, - then in indirect heat exchange with preheated boiler feed water up through the pipes in the first pipe-side 030065/0761 gen passage of a third vertical low-temperature gas cooler with jacket and straight heating pipes, the two pipe-side passages and one jacket-side passage as well as solid tube sheet, and - then down through the tubes in the second tube-side Passage of the third gas cooler; and generating saturated steam on the shell sides of the first and third gas coolers, at least a portion of the Saturated steam is superheated on the shell side of the second gas cooler to generate by-product superheated steam, while any remaining saturated steam is withdrawn as by-product saturated steam; and Preheating of the boiler feed water through indirect heat exchange with the gas flow leaving the third gas cooler. 19. The method according to claim 18,
marked by simultaneous passage of separate quantities of preheated boiler feed water from a steam drum through the shell sides the first and third gas coolers and directing the steam generated thereby into the steam drum; and Introducing at least part of the saturated steam from the steam drum into the shell side of the second gas cooler. 030066/0761 024469 20. The method according to claim 18,
characterized, that about 0-50 mol% of the gas flow leaving the first gas cooler is led past the second gas cooler and mixed with the gas flow leaving the second gas cooler. 21. The method according to any one of the preceding claims, characterized by Separation of further solids from the cleaned gas stream from step 5) in a second, the gas-solids separation zone downstream gas-solids separation zone, the single or multi-stage cyclones, impact separators, filters, includes electrostatic precipitators or combinations thereof. 22. The method according to any one of the preceding claims, characterized in that that as carbonaceous solid fuel, carbon particles Coal, coal coke, brown coal, petroleum coke, oil shale, tar sands, asphalt, pitch or mixtures thereof are selected will. 23. The method according to any one of the preceding claims, characterized in that that the carbonaceous solid fuel either by itself 030065/0761 302U69 or in the presence of a hydrocarbon which is substantially liquefiable or vaporizable by heat and / or water is subjected to partial oxidation. 24. The method according to any one of the preceding claims, characterized in, that the carbonaceous solid fuel in one gaseous carrier medium, the steam, COp, N-, synthesis gas or air is introduced into the gas generator. 25. Device for generating an H-, CO, CO- and H_0 comprehensive and entrained solids and slag-containing hot gas stream by partial oxidation of a carbonaceous solid fuel as well as for cooling and Cleaning of the hot raw gas flow and separation of entrained solids and slag from it, marked by 1) a partial oxidation gas generator (11) for generating the hot gas stream; 2) a separate closed vertical cylindrical pressure vessel (46), the interior of which is coated with high temperature resistant Refractory material (47) is lined and the one coaxial lower gas-gas quench cooling and - Solids separation chamber (48) in flow communication with a coaxial upper chamber (49), wherein the chambers (48, 49) are connected by a coaxial orifice ring passage (50) of smaller diameter; 030065/0761 ORIGINAL INSPECTED 302U69 3) a first gas inlet nozzle (45) connected to the gas generator (11) for introducing the hot raw gas stream into the lower chamber (48) and a second gas inlet nozzle (55) directly opposite and coaxial with the first gas inlet nozzle (45) is for introducing a cooled and purified gas stream into the lower chamber (48), whereby - the gas flows meet, - The hot raw gas flow through direct heat exchange with the cooled and cleaned gas flow to a Temperature is cooled below the deformation start temperature of the entrained slag, and - Solids and slag are separated by gravity and to the bottom of the lower chamber (48) fall as the stream of cooled gas exits lower chamber (48) and up through the orifice ring passage (50) flows into the upper chamber (49), in which further solids and slag are separated and fall to the bottom of the lower chamber (48); 4) an outlet (54) in the upper part of the upper chamber (49) for discharging a cooled and purified gas stream; and 5) a lower outlet (52) in the lower end of the lower * Chamber (48) for removing the solids and slag. 030065/0761 ORfGlNAL INSPECTED 26. Device according to claim 25, characterized by at least one arranged in the upper chamber (4-9) Gas-solids separation unit (56), which removes the gas mixture flowing upwards through the container (46) from step (3) receives, separates additional solids therefrom and these solids are discharged into the lower chamber (48). 27. Device according to claim 26, characterized in that that the gas-solids separation unit (56) is a single-stage, a multi-stage cyclone separator, an impact separator, is a filter or a combination of these devices. 28. Device according to one of claims 25-27, characterized by at least one in the upper part of the lower chamber (48) or in the lower part of the upper chamber (49) or in both positioned tangential inlet (62) for introduction part of a cooled and purified recycle gas stream. 29. Device according to one of claims 25-28, characterized by Means for introducing at least a portion of the cooled and purified gas stream of step (4) as cooled and 030065/0761 purified gas stream in step (3), with further cooling and with or without additional purification the pressure vessel (4-6). 30. Device according to one of claims 25-29, characterized in that that outside the container (4-6) this a gas-solid separation unit (64A) is connected downstream for separating further solids from the gas stream of step (4). 31. Device according to claim 30, characterized in that that the gas-solids separation unit arranged outside the container (46) (64A) a single stage or a Multi-stage cyclone separator, an impact separator, is an electrostatic precipitator, a filter, and / or a combination thereof. 32. Device according to one of claims 25-31, characterized by a plurality of pairs of first gas inlets (45) and second gas inlets (55) coaxial therewith in step (3). 030065/0761 33. Device according to one of claims 25-32, characterized in that that the longitudinal axis of the first and the second gas inlet (45, 55) in the same plane as the vertical central axis of the container (46), and that the longitudinal axis with the vertical central axis, starting from this in clockwise direction, an angle of forms approx. 30-150 °. 34. Device according to one of claims 25-33, marked by a solids and slag pre-separation unit (HA), between the outlet of the gas generator (11) in (1) and the inlet of the first gas inlet nozzle (45) in (3) is switched. 030065 / 07B1 ORfGlNAL JNSPECTTED