DE202005021662U1 - Apparatus for producing synthesis gases by partial oxidation of slurries produced from ash-containing fuels with partial quenching and waste heat recovery - Google Patents

Abstract

Device for the gasification of solid fuels, such as hard coal and coke, such as hard coal, lignite, biomass and petroleum coke, in flowing stream with a free oxygen-containing oxidant by partial oxidation at pressures between ambient pressure and 100 bar and temperatures between 1200 to 1900 degrees,
marked by:
A plant for the production and supply of slurry (1), a gasification reactor (2) with cooled reaction space contour, a quench cooler (3) for partial cooling of the raw gas, a waste heat boiler (4), a scrubber (5) and a partial condenser (6), wherein crude scrubber (5) and partial condenser (6) can be replaced or supplemented by a device for dry dust separation, which are connected in series, wherein
- A reactor (2) for gasifying the supplied fuel dust with a free oxygen-containing oxidant consisting of the delivery tube (1.1) for the fuel slurry and a line for the oxidant (2.1) by means of burner (2.2) in the reaction space (2.3) consisting of a gas-tight, welded, water-cooled pipe.

Description

The The invention relates to a device according to the preamble the first protection claim.

The device comprises the slurry production, fuel supply, gasification reaction, partial quenching, gas scrubbing and partial condensation, gas scrubbing and partial condensation can be replaced by a mechanical dust separation, to produce CO and H ₂ -containing gases by partial oxidation of dusty, ash-containing fuels with a gasification agent containing free oxygen at high temperatures and elevated pressure.

Around To reach long operating times must be the pressure jacket of the gasification reactor reliable against the action of raw gas and against the high Gasification temperatures of 1,200-1,900 ° C protected be. This is done by limiting the reaction or gasification space through a cooled pipe screen, which is in the pressure jacket is mounted. The annular gap between pipe shield and pressure jacket is rinsed.

Of the Fuel is produced as slurry by pumping to gasification pressure brought and fed at the top of the reactor via burner. It can be one or more fuels or coals at the same time to be gassed. The raw gas leaves the gasification room together with the liquefied slag at the bottom of the reactor and is then injected by injection Water at 700 ° C to 1100 ° C partially cooled and after the waste heat recovery of entrained particulate matter freed. Subsequently, the scrubbed raw gas is further treatment stages fed.

In the technology of gas generation, the autothermal entrained flow gasification of solid, liquid and gaseous fuels has been known for many years. The ratio of fuel to oxygen-containing gasification agents is chosen so that due to the synthesis gas quality higher carbon compounds to synthesis gas components such as CO and H _{2 are} completely split and the inorganic components are discharged as molten slag, see J. Carl, P. Fritz, NOELL CONVERSION PROCESS, EF-Verlag for Energy and Environmental Technology GmbH, 1996, p. 33 and p. 73 ,

According to various systems introduced in the art, gasification gas and molten slag can be separated or discharged together from the reaction space of the gasification device, such as DE 197 18 131 A1 shows. For the inner confinement of the reaction space structure of the gasification system, both refractory lined or cooled systems have been introduced, see DE 4446 803 A1 ,

EP 0677 567 B1 and WO 96/17904 show a method in which the gasification space is limited by a refractory lining. This has the disadvantage that the refractory brickwork is detached by the liquid slag produced during the gasification, which leads to rapid wear and high repair costs. As the ash content increases, this wear process increases. Thus, such gasification systems have a limited duration to the renewal of the lining. In addition, the gasification temperature and the ash content of the fuel are limited. The supply of fuel as a coal-water slurry brings significant efficiency losses, see C. Higman u. M. van der Burgt, "Gasification", ELSEVIER, USA, 2003 which can be reduced or avoided by using oil as a carrier medium or by preheating the coal-water slurries. Furthermore, a quenching or cooling system is described, in which the hot gasification gas and the liquid slag together via a guide tube, which begins at the lower end of the reaction chamber, discharged and passed into a water bath. This common removal of gas Ver gas and slag can lead to blockages of the guide tube and thus to limit the availability.

DE 3534015 A1 shows a method in which the gasification media fine coal and oxygen-containing oxidant are introduced through several burners in the reaction space so that the flames deflect each other. At the same time, the gasification gas flows upwards, laden with fine dust, and the slag flows down into a slag cooling system. As a rule, a device for indirect cooling using the waste heat is provided above the gasification space. By entrained liquid slag particles, however, there is a risk of deposition and occupancy of the heat exchanger surfaces, which leads to the obstruction of heat transfer and possibly to blockage of the pipe system or erosion. The risk of constipation is counteracted by the hot raw gas is cooled with a recirculating cooling gas.

From Ch. Higman and M. van der Burgt is published in "Gasification", page 124, publisher Elsevier 2003 , a method is presented in which the hot gasification gas leaves the carburetor together with the liquid slag and enters directly into a waste heat boiler arranged vertically below, in which the raw gas and the slag are cooled using the waste heat to generate steam. The slag collects in a water bath, the cooled raw gas leaves the waste heat boiler sideways. The advantage of waste heat recovery after this Sys There are a number of disadvantages. Mention may be particularly the formation of deposits on the heat exchanger tubes, which lead to the obstruction of heat transfer and corrosion and erosion and thus lack of availability.

CN 200 4200 200 7.1 describes a "solid powdered fuel gasifier" in which the coal dust is pneumatically supplied and gasification gas and liquefied slag are introduced into a water bath via a central tube for further cooling in. This central discharge in said central tube is susceptible to blockages which interfere with overall operation reduce the availability of the entire system.

outgoing From this prior art, it is an object of the invention, a To create a device that is reliable in operation takes into account the different ash contents of the fuels and has high availability.

These The object is achieved by a device according to the features of the first Protection claim solved. Subordinate claims advantageous embodiments of the invention again.

The apparatus for the gasification of solid ash-containing fuels with an oxygen-containing oxidant in a trained as a fly-reactor gasification at pressures between ambient pressure and 100 bar, wherein the reaction space contour is limited by a cooling system, wherein the pressure in the cooling system is always kept higher than the pressure in the reaction space , characterized by the following features:
The fuel, z. As hard coal, lignite and lignite coke and biomass coke and / or petroleum coke or their mixtures are crushed to a grain size <500 microns, preferably <200 microns and with the addition of liquids such as water or oil to a fuel-water or fuel Oil suspension, a so-called slurry, mixed. When using water as the carrier medium is achieved with the addition of surfactants stable solids concentrations up to 70 Ma%. These are brought by suitable pumps to the desired gasification pressure up to a maximum of 100 bar and fed via suitable burners, which are attached to the head of the gasification reactor, the gasification reaction. The fuel concentration in the slurry as well as the flowing amount of slurry are monitored, measured and controlled by measuring, regulating and monitoring devices. The burner is simultaneously fed to a free oxygen-containing oxidant and the fuel slurry is converted by partial oxidation in a Rohsynthesegas. The gasification takes place at temperatures between 1,200 and 1,900 ° C at pressures up to 100 bar. The reactor is equipped with a cooling screen consisting of gas-tight welded and water-cooled pipes.

The hot raw synthesis gas leaves together with the liquid slag formed from the fuel ash Gasification reactor and enters a vertically arranged below Space in which by injecting water or by feeding a cool gas a Teilquenchung, so a cooling at temperatures between 700 ° C and 1100 ° C takes place. At this temperature, the entrained liquid Slag cooled down so far that it no longer adheres to the metallic Can adhere to surfaces. That to the temperatures of 700 ° C and 1100 ° cooled raw gas passes thereafter together with the likewise cooled solid slag into a waste heat boiler to use the sensible heat for steam generation. Through this previous partial quenching or Partial cooling will increase the risk of caking prevented or greatly limited to the waste heat cooling tubes. The water required for the partial quenching or recycled Gas condensate is supplied via nozzles, which are located directly on the jacket. The cooled slag collects in a water bath at the bottom of the waste heat boiler is arranged. That at about 200 ° C-300 ° C cooled raw gas leaves the side of the waste heat boiler and gets into a Rohgaswäsche, the more appropriate Way is designed as Venturiwäsche. Here is the entrained dust up to a grain size away from about 20 microns. This degree of purity is still enough not to subsequently catalytic processes such as to carry out a crude gas conversion. It is further to consider that additionally carried salt mist in the raw gas be released from the fuel dust during gasification and be discharged with the raw gas. To both the fine dust <20 microns as well as to remove the salt mist, the scrubbed crude gas fed to a condensation stage in which the raw gas indirectly is cooled by 5 ° C to 10 ° C. there is condensed water from the water vapor-saturated crude gas, which absorbs the described fine dust and salt particles. In a subsequent separator is the dust and Salt particles contained condensed water deposited. That so purified crude gas can then directly, for example, a crude gas conversion or desulfurization, fed.

At The washing and condensation stage can be set at 200 ° C provided to 300 ° C working mechanical dust separation be used with centrifugal or filter systems can be.

The invention will be described below with reference to FIGS Ren and an embodiment explained in more detail. The figures show:

1 : Block diagram of the technology

2 : Gasification reactor with partial quenching and vertically arranged waste heat boiler

3 : Gasification reactor with partial quenching and waste heat boiler on the side A quantity of coal of 320 t / h with a composition of C 71.5 Ma% H 4.2 Ma% O 9.1 Ma% N 0.7 Ma% S 1.5 Ma% Cl 0.03 Ma% an ash content of 11.5 Ma% and a moisture content of 7.8 Ma% is to be gasified at a pressure of 40 bar. The calorific value of the coal is 25,600 kJ / kg. The gasification takes place at 1450 ° C. For the gasification, an amount of oxygen of 245,000 m ³ i. N./h needed. The coal is first fed to a state-of-the-art grinding plant, in which the comminution is carried out to a granulation between 0 and 200 microns, then with water with the addition of surfactants to a stable coal dust-water suspension, the so-called slurry in a special facility 1 to 1 to be mixed. The solids concentration in this slurry is 63% by mass, the amount of slurry is 465 t / h. The slurry is brought to the desired gasification pressure at 100 bar by means of a suitable for the promotion of solid-liquid suspensions pump and via the delivery line 1.1 the burner of the gasification reactor 2 to 1 supplied, the amount is monitored, measured and regulated. To save oxygen, the slurry before feeding to the gasification reactor 2 depending on the gasification pressure preheated to 400 ° C.

The gasification reactor is in the 2 and 3 shown. The about the support line 1.1 The 465 t / h slurry flowing into the gasification reactor is communicated with the via line 2.1 inflowing oxygen amount of 245,000 m ³ i. N./h in the gasification room 2.3 subjected to partial oxidation at 1450 ° C, wherein 565,000 m ³ i. N./h raw gas of the following composition arise: H ₂ 18.5 % Vol. CO 70.5 % Vol. CO ₂ 6.1 % Vol. N ₂ 2.3 % Vol. NH ₃ 0,003 % Vol. HCN 0,002 % Vol. H ₂ S 0.5 % Vol. COS 0.07 % Vol.

The gasification room 2.3 is from a cooling screen 2.4 limited, which consists of a gas-tight welded, water-cooled pipe system. The raw gas flows together with the liquid slag via the outlet opening 2.5 in the room 3.1 for partial quenching / partial cooling of the raw gas to temperatures of 700 ° C-1100 ° C. At this temperature, in addition to the raw gas and the slag cooled down so far that they are not in the pipes 4.1 after 1 can deposit subsequent heat recovery boiler. The in the waste heat boiler 4 generated steam is used in the process for preheating the oxygen-containing oxidant or as a gasification moderator for preheating the slurries. The slag collects in a water bath 4.2 , which is located at the bottom of the heat recovery boiler and is over 4.3 discharged. The raw gas leaves the waste heat boiler 4.4 and gets into the raw gas scrubber 5 to 1 , The waste heat boiler 4 can after 3 directly under the gasification reactor 2 and partial quenching 3 but also, how 4 shows, be arranged adjacent. In this case, it is under both the partial quenching 3 a slag deduction 4.3 as well as below the waste heat boiler 4.6 , That the waste heat boiler 4 over the exit 4.4 leaving raw gas then passes into the crude gas scrubbing 5 to 1 , which is designed as a controllable Venturi wash and applied with about 100 m ³ / h of wash water. The wash water is usually freed from the absorbed solids and fed back to the Venturi wash. The washing water can be preheated to moisten the raw gas during washing at the same time. In order to remove fine dust <20 μm as well as salt mist not separated in the Venturi wash, the water-washed crude gas becomes a partial condensation 6 to 1 subjected to, wherein the raw gas is cooled indirectly by 5-10 ° C. By condensing water vapor during cooling, the finest dust and salt particles are absorbed and thus removed from the raw gas. The crude gas purified from solids then has the following composition: H ₂ 13.4 % Vol. CO 51.4 % Vol. CO ₂ 4.5 % Vol. N ₂ 1.5 % Vol. NH ₃ 0.0022 % Vol. HCN 0.0012 % Vol. H ₂ S 0.36 % Vol. COS 0.05 % Vol. H ₂ O 37.30 % Vol.

The purified wet raw gas quantity is 775,000 Nm ³ / h. It can be fed directly to a crude gas conversion or other treatment stages.

1

slurry preparation and feeding

1.1

Slurryleitung

2

reactor

2.1

management for oxygen

2.2

burner

2.3

gasification chamber

2.4

cooling screen

2.5

outlet opening

3

quench

3.1

quench

3.2

Nozzles in 3

3.4

Transfer line from 3 to 4

4

waste heat boiler

4.1

Cooling tubes in the waste heat boiler 4

4.2

Water bath with slag in 4

4.3

Slag vent off 4

4.4

Opening off 4 to the crude gas scrubber 5

4.5

Water bath with slag 4

4.6

Slag vent off 4

5

Rohgaswäscher

6

partial condenser

QUOTES INCLUDE IN THE DESCRIPTION

This list The documents listed by the applicant have been automated generated and is solely for better information recorded by the reader. The list is not part of the German Patent or utility model application. The DPMA takes over no liability for any errors or omissions.

Cited patent literature

• DE 19718131 A1 [0006]
• - DE 4446803 A1 [0006]
• EP 0677567 B1 [0007]
• WO 96/17904 [0007]
• - DE 3534015 A1 [0008]
• - CN 20042002007 [0010]

Cited non-patent literature

• - J. Carl, P. Fritz, NOELL CONVERSION PROCESS, EF-Verlag for Energy and Environmental Technology GmbH, 1996, p. 33 and p. 73 [0005]
• - C. Higman u. M. van der Burgt, "Gasification", ELSEVIER, USA, 2003 [0007]
• - Ch. Higman and M. van der Burgt is published in "Gasification", page 124, publisher Elsevier 2003 [0009]

Claims (26)

Device for the gasification of solid fuels, such as hard coal and coke, such as hard coal, lignite, biomass and petroleum coke, in flowing stream with a free oxygen-containing oxidant by partial oxidation at pressures between ambient pressure and 100 bar and temperatures between 1200 to 1900 degrees, characterized by: - a plant for producing and supplying slurry ( 1 ), a gasification reactor ( 2 ) with cooled reaction space contour, a quench cooler ( 3 ) for partial cooling of the raw gas, a waste heat boiler ( 4 ), a scrubber ( 5 ) and a partial capacitor ( 6 ), whereby raw gas scrubbers ( 5 ) and partial capacitor ( 6 ) can be replaced or supplemented by a device for dry dust separation, which are connected in series, wherein, - a reactor ( 2 ) for the gasification of the supplied fuel dust with a free oxygen-containing oxidant, consisting of the delivery tube ( 1.1 ) for the fuel slurry and a line for the oxidant ( 2.1 ), which by means of burners ( 2.2 ) in the reaction space ( 2.3 ), which consists of a gas-tight welded, water-cooled pipes existing cooling screen ( 2.4 ) and a discharge device ( 2.5 ) in a quench cooler ( 3 ), - a quench cooler ( 3 ) without internals, in which nozzles ( 3.2 ) are arranged in one or more nozzle rings, via which the required water can be injected for partial quenching, whereby the nozzles ( 3.2 ) are arranged flush with an inner shell, - a quench cooler ( 3 ) downstream waste heat boiler ( 4 ), - apparatus are connected downstream for the purification of the gas. Device according to one of the preceding claims, characterized in that the reaction space ( 3.2 ) of the quench cooler 3 directly with the waste heat boiler ( 4 ), in which pipes ( 4.1 ) the sensible heat of the raw gas is used to generate steam and in its lower part outlet openings for the raw gas ( 4.4 ) and for slag removal ( 4.3 ) with a water bath ( 4.2 ) are arranged. Device according to one of the preceding claims, characterized in that for cleaning a crude gas scrubber ( 5 ) and a scrubber ( 5 ) downstream partial condensation plant ( 6 ) are arranged. Device according to one of the preceding claims, characterized in that as Rohgaswäsche ( 5 ) a single or multi-stage Venturi scrubber is arranged. Device according to one of the preceding claims, characterized in that for gas purification, a mechanical dry Dust collector is arranged. Device according to one of the preceding claims, characterized in that after water washing ( 5 ) and partial condenser or the mechanical dry dust separator further gas treatment stages such as a Rohgaskonvertierer or a desulfurization system are connected downstream. Device for the gasification of solid fuels, such as hard coal and coke, such as hard coal, lignite, biomass and petroleum coke, in flowing stream with a free oxygen-containing oxidant by partial oxidation at pressures between ambient pressure and 100 bar and temperatures between 1200 to 1900 degrees, characterized by - an attachment ( 1 ) for the production and supply of slurry, a gasification reactor ( 2 ) with cooled reaction space contour, a quench cooler ( 3 ) for partial cooling of the raw gas, a waste heat boiler ( 4 ), a scrubber ( 5 ) and a partial capacitor ( 6 ), whereby raw gas scrubbers ( 5 ) and partial capacitor ( 6 ) can be replaced or supplemented by a device for dry dust separation, which are connected in series, - a reactor ( 2 ) for the gasification of the supplied fuel dust ( 1 ) with a free oxygen-containing oxidant, consisting of the delivery tube ( 1.1 ) for the fuel slurry and a line for the oxidant ( 2.1 ), which by means of burners ( 2.2 ) in the reaction space ( 2.3 ), which consists of a gas-tight welded, water-cooled pipes existing cooling screen ( 2.4 ) and a discharge device ( 2.5 ) in a quench cooler ( 3 ), - a quench cooler ( 3 ), from which in the Quenchraum ( 3.1 ) partially cooled raw gas via the transfer line ( 3.4 ) to the waste heat boiler ( 4 ), - a waste heat boiler ( 4 ), which with Siederohren ( 4.1 ) and uses the sensible heat of the raw gas for steam generation, - a raw gas scrubber ( 5 ) and - a raw gas scrubber ( 5 ) downstream partial condensation plant ( 6 ), which is replaceable by a mechanical filtering dust deposit. Device according to claim 1, characterized in that both in the quencher ( 3 ) as well as in the waste heat boiler ( 4 ) Water baths ( 4.2 ) and ( 4.5 ) are arranged, in which collects the cooled slag. Device according to one of the preceding claims, characterized in that both the quencher ( 3 ) as well as the waste heat boiler ( 4 ) Vorrich for the discharge of slag ( 4.3 . 4.6 ) are arranged. Device according to one of the preceding claims, characterized in that instead of raw gas scrubbing and partial condensation a above the dew point working dry mechanical dust remover is arranged. Device according to one of the preceding claims, thereby marked that the fuel is of the following nature having: Combustible dust with a grain size <200 μm, preferably <100 μm, in a special plant with water with the addition of a surfactant to a fuel-water slurry with a solid concentration of 40-70% by weight and pump delivery brought to the gasification pressure of 100 bar, with the slurry on Temperatures preheated to 400 ° C. Device according to one of the preceding claims, characterized in that in the partial quenching a cooling of the raw gas is given at temperatures between 700 and 1,100C. Device according to one of the preceding claims, characterized in that in a waste heat boiler ( 4 ) is a cooling of the partially quenched crude gas with steam generation to temperatures between 150 and 400 ° C. Device according to one of the preceding claims, characterized in that the raw gas cooling for the removal entrained dust a Rohgaswäsche ( 5 ) and a partial condensation ( 6 ) are subordinate. Device according to one of the preceding claims 1 to 7, characterized in that the raw gas cooling For the deposition entrained dust a dry mechanical Dust separation by means of centrifugal force or filter is arranged downstream. Device according to one of the preceding claims, characterized in that the gas cooling and the dust removal device further treatment stages such as a crude gas conversion or a Desulfurization downstream. Device according to one of the preceding claims, characterized in that as Rohgaswäscher ( 4 ) a single or multi-stage Venturi scrubber is arranged. Device according to claim 11, characterized in that that the Venturi scrubber with fresh water or recycled Condensate can be fed, which is obtained during the cooling of the gas. Device according to one of the preceding claims, characterized in that the Venturi scrubber of circulating water or recirculated condensate can be fed. Device according to one of the preceding claims, characterized in that the waste heat boiler ( 4 ) is designed for operation at temperatures of 700 to 1,100 ° C. Device according to one of the preceding claims, characterized in that the raw gas scrubber ( 5 ) is designed for operation at temperatures of 150 to 300 ° C. Device according to one of the preceding claims, characterized in that the fuel as a fuel-water slurry given is. Device according to one of the preceding claims, characterized in that a plurality of burners are arranged. Device according to one of the preceding claims, characterized in that a plurality of outlets ( 3.6 ) for discharging the granulated slag from the quenching space ( 3.5 ) are arranged. Device according to one of the preceding claims, characterized in that a plurality of gas outlets ( 3.4 ) for leaving the quenched raw gas from the quenching space ( 3.5 ) are arranged. Device according to one of the preceding claims, characterized in that a device for measuring, monitoring and controlling the amount of slurry in the delivery pipe ( 1.1 ) is arranged.