U.S. patent application number 11/359608 was filed with the patent office on 2007-04-12 for method and device for high-capacity entrained flow gasifier.
This patent application is currently assigned to Future Energy GmbH. Invention is credited to Dietmar Adler, Joachim Lamp, Friedemann Mehlhose, Manfred Schingnitz.
Application Number | 20070079554 11/359608 |
Document ID | / |
Family ID | 37909963 |
Filed Date | 2007-04-12 |
United States Patent
Application |
20070079554 |
Kind Code |
A1 |
Schingnitz; Manfred ; et
al. |
April 12, 2007 |
Method and device for high-capacity entrained flow gasifier
Abstract
A method and device for the gasification of pulverized fuels
from solid fuels such as bituminous coals, lignite coals, and their
cokes, petroleum cokes, coke from peat or biomass, in entrained
flow, with an oxidizing medium containing free oxygen, by partial
oxidation at pressures between atmospheric pressure and 80 bar, and
at temperatures between 1,200 and 1,900.degree. C., at high reactor
capacities between 1,000 and 1,500 MW. The method uses the
following steps: metering of the fuel, gasification reaction in a
gasification reactor with cooled reaction chamber contour,
quench-cooling, crude gas scrubbing, and partial condensation.
Inventors: |
Schingnitz; Manfred;
(Freiberg, DE) ; Mehlhose; Friedemann; (Freiberg,
DE) ; Lamp; Joachim; (Heidelberg, DE) ; Adler;
Dietmar; (Grossschirma OT. Siebenlehn, DE) |
Correspondence
Address: |
WILLIAM COLLARD;COLLARD & ROE, P.C.
1077 NORTHERN BOULEVARD
ROSLYN
NY
11576
US
|
Assignee: |
Future Energy GmbH
Manfred SCHINGNITZ
|
Family ID: |
37909963 |
Appl. No.: |
11/359608 |
Filed: |
February 22, 2006 |
Current U.S.
Class: |
48/210 |
Current CPC
Class: |
C10J 2200/156 20130101;
C10J 3/845 20130101; C10J 3/84 20130101; C10J 2300/0959 20130101;
C10J 2200/09 20130101; Y02P 20/145 20151101; C10J 3/466 20130101;
C10J 2300/0916 20130101; C10K 1/101 20130101; C10J 2300/1634
20130101; Y02P 20/129 20151101; C10J 2300/093 20130101; C10J 3/506
20130101; C10J 2300/1687 20130101 |
Class at
Publication: |
048/210 |
International
Class: |
C10J 3/00 20060101
C10J003/00 |
Foreign Application Data
Date |
Code |
Application Number |
Oct 7, 2005 |
DE |
10 2005 048 488.3 |
Claims
1. A method for the gasification of pulverized fuels from solid
fuels such as bituminous coals, lignite coals, and their cokes,
petroleum cokes, coke from peat or biomass, in entrained flow, with
an oxidizing medium containing free oxygen, comprising the
following steps; supplying a fuel with a water content <10 wt. %
and a grain size <200 .mu.m to multiple identically engaged
metering systems that feed the fuel through transport pipes to
multiple gasification burners located at a head of a reactor, said
burners being symmetrically arranged and containing additional
oxygen infeeds; igniting said multiple burners with oxygen infeed
in the head of the reactor by ignition and pilot burners;
determining quantities of the fuel and oxygen fed to the burners,
and determining an overall total of all amounts of fuel and oxygen
supplied to the burners, regulating an oxygen ratio with a
regulating mechanism that ensures that the oxygen ratio neither
exceeds nor falls below a ratio of 0.35 to 0.65, regardless of the
distribution of fuel and oxygen to the burners; converting the fuel
in the gasification reactor at temperatures between 1,200 and
1,900.degree. C. and at pressures between atmospheric pressure and
80 bar, into a crude synthesis gas and slag; cooling the crude gas
at 1,200 to 1,900.degree. C. and the slag down to a condensation
point at temperatures between 180.degree. C. and 240.degree. C. in
a quenching cooler by injecting water; and feeding the cooled crude
gas to further treatment stages.
2. A method pursuant to claim 1, wherein there are three metering
systems conducting fuel streams through transport pipes to three
burners.
3. A method pursuant to claim 1, wherein the fuel has a grain size
of <100 .mu.m.
4. A method pursuant to claim 1, wherein the fuel has a water
content of <2 wt. %.
5. A method pursuant to claim 1, wherein the fuel is fed to the
reactor in as a pulverized fuel-in-water slurry, with each burner
having its own infeed system.
6. A method pursuant to claim 1, wherein the fuel is fed to the
reactor as a pulverized fuel-in-oil slurry, with each burner having
its own infeed system.
7. A method pursuant to claim 1, wherein more than one fuel is
gasified at the same time.
8. A method pursuant to claim 1, wherein a different fuel is
gasified by each burner.
9. A method pursuant to claim 1, wherein the fuel is fed through
the burners pneumatically or as a slurry.
10. A method pursuant to claim 1, further comprising the steps of
partial cooling to temperatures between 700 and 1,100.degree. C.
and waste heat recovery by steam generation from the heat of the
crude gas, following the step of converting.
11. A device for the gasification of pulverized fuels from solid
fuels such as bituminous coals, lignite coals, and their cokes,
petroleum cokes, coke from peat or biomass, in entrained flow, with
an oxidizing medium containing free oxygen, comprising: a metering
system for passing multiple streams of pulverized fuel, comprising
a bunker connected to pressurized sluices that conduct the streams
of pulverized fuel to metering tanks, and multiple transport lines
running from the metering tanks; a high-capacity reactor connected
to the transport lines, said reactor having multiple gasification
burners and an ignition and pilot burner symmetrically arranged at
a head of the reactor; a measuring system at the gasification
burners to measure and regulate amounts of pulverized fuel and
oxygen flowing in, with integral monitoring and regulation of
overall total amounts of pulverized fuel and oxygen flowing to the
reactor; a quenching chamber connected to the reactor to cool crude
gas and slag produced in the reactor; a crude gas scrubber
connected to the quenching chamber; a cooler connected to the
scrubber for performing a partial condensation.
12. A device for the gasification of pulverized fuels from solid
fuels such as bituminous coals, lignite coals, and their cokes,
petroleum cokes, coke from peat or biomass, in entrained flow, with
an oxidizing medium containing free oxygen, comprising: a metering
system for metering fuel through transport pipes; a high-capacity
reactor connected to the transport pipes, said reactor having 3
gasification burners and an ignition and pilot burner at a head of
the reactor; a system to measure and regulate amounts of pulverized
fuel and oxygen flowing into the gasification burners with integral
monitoring and regulation of overall total amounts of pulverized
fuel and oxygen flowing to the reactor; a quenching chamber
connected to the reactor for partial cooling of the crude gas and
slag produced in the reactor; a waste heat boiler connected to the
quenching chamber to recover steam with further cooling of crude
gas and slag; and a water scrubber and partial condenser connected
to the waste heat boiler.
13. A device pursuant to claim 11, wherein each gasification burner
has its own associated metering system.
14. A device pursuant to claim 12, wherein each gasification burner
has its own associated metering system.
Description
BACKGROUND OF THE INVENTION
[0001] 1. Field of the Invention
[0002] The invention relates to a method for entrained flow
gasification with very high capacity that can be used for supplying
large-scale syntheses with synthesis gas. The invention enables the
conversion of fuels refined into pulverized fuel, such as lignite
and bituminous coals, petroleum coke, solid grindable refuse, and
solid-liquid suspensions, so-called slurries, into synthesis gas.
The fuel is reacted at temperatures between 1,200 and 1,900.degree.
C. with a gasification medium containing free oxygen, at pressures
up to 80 bar, by partial oxidation to gases containing CO and
H.sub.2. This is done in a gasification reactor that is
distinguished by a multiple-burner system and by a cooled
gasification chamber.
[0003] 2. The Prior Art
[0004] The autothermic entrained flow gasification of solid,
liquid, and gaseous fuels has been known in the technology of gas
production for years. The ratio of fuel to gasification medium
containing oxygen is chosen so that higher carbon compounds are
completely cracked for reasons of synthesis gas quality into
synthesis gas components such as CO and H.sub.2, and the inorganic
components are discharged as molten slag; see J. Carl, P. Fritz,
NOELL-KONVERSIONSVERFAHREN, EF-Verlag fur Energie- und
Umwelttechnik GmbH, 1996, p. 33 and p. 73.
[0005] According to various systems used in industry, gasification
gas and molten slag can be discharged separately or together from
the reaction chamber of the gasification device, as shown in German
Patent No. DE 197 131 A1. Either systems with refractory linings or
cooled systems are used for the internal confinement of the
reaction chamber structure of the gasification system; see German
Patent No. DE 4446 803 A1.
[0006] European Patent No. EP 0677 567 B1 and International
Publication No. WO 96/17904 show a method in which the gasification
chamber is confined by a refractory lining. This has the drawback
that the refractory masonry is loosened by the liquid slag formed
during gasification, which leads to rapid wear and high repair
costs. This wear process increases with increasing ash content.
Thus, such gasification systems have a limited service life before
replacing the lining. Also, the gasification temperature and the
ash content of the fuel are limited; see C. Higman and M. van der
Burgt, "Gasification", Verlag ELSEVIER, USA, 2003. A quenching or
cooling system is also described, with which the hot gasification
gas and the liquid slag are carried off together through a conduit
that begins at the bottom of the reaction chamber, and are fed into
a water bath. This joint discharge of gasification gas and slag can
lead to plugging of the conduit and thus to limitation of
availability.
[0007] German Patent No. DE 3534015 A1 shows a method in which the
gasification media, powdered fuel and oxidizing medium containing
oxygen, are introduced into the reaction chamber symmetrically
through multiple burners in such a way that the flames are mutually
diverted. The gasification gas loaded with powdered dust flows
upward and the slag flows downward into a slag-cooling system. As a
rule, there is a device above the gasification chamber for indirect
cooling utilizing the waste heat. However, because of entrained
liquid slag particles, there is the danger of deposition and
coating of heat exchanger surfaces, which hinders heat transfer and
may lead to plugging of the pipe system and/or erosion. The danger
of plugging is counteracted by taking away the hot crude gas with a
circulated cooling gas.
[0008] Ch. Higmann and M. van der Burgt in "Gasification", page
124, Verlag Elsevier 2003, describe a method in which the hot
gasification gas leaves the gasifier together with the liquid slag
and directly enters a waste heat boiler positioned perpendicularly
below it, in which the crude gas and the slag are cooled with
utilization of the waste heat to produce steam. The slag is
collected in a water bath, while the cooled crude gas leaves the
waste heat boiler from the side. A series of drawbacks detract from
the advantage of waste heat recovery by this system. Deposits form
on the heat exchanger tubes, which lead to hindrance of heat
transfer and to corrosion and erosion, and thus to lack of
availability.
[0009] Chinese Patent No. CN 200 4200 200 7.1 describes a "Solid
Pulverized Fuel Gasifier", in which the powdered coal is fed in
pneumatically and gasification gas and liquefied slag are
introduced into a water bath through a central pipe for further
cooling. This central discharge in the central pipe is susceptible
to plugging that interferes with the overall operation, and reduces
the availability of the entire system.
[0010] The capacity of the various gasification technologies
mentioned is limited to about 500 MW, which is attributable in
particular to the fuel infeed to the gasification reactor.
SUMMARY OF THE INVENTION
[0011] It is therefore an object of this invention to provide a
gasification method that permits maximum capacities of 1,000 to
1,500 MW with reliable and safe operation.
[0012] This object is achieved by a gasification method for the
gasification of solid fuels containing ash at very high capacities
with an oxidizing medium containing oxygen based on an entrained
flow reactor whose reaction chamber contour is confined by a
cooling system, with the pressure in the cooling system always
being kept higher than the pressure in the reaction chamber. The
process for preparing the fuel and feeding it to the gasification
burners is as follows: with dry pneumatic infeed by the dense-flow
transport principle, the fuel is dried, pulverized to a grain size
of <200 .mu.m, and passed through operational bunkers to
pressurized sluices, in which the dust-like fuel is brought to the
desired gasification pressure by introducing a non-condensing gas
such as N.sub.2 or CO.sub.2. Different fuels can be used here at
the same time. Via a system of multiple such pressurized sluices,
they can be loaded and pressurized alternately. The dust under
pressure then is sent to metering tanks, in the bottom of which a
very dense fluidized bed is produced by likewise introducing a
non-condensing gas, with one or more transport pipes immersed in
the bed and opening into the burners of the gasification reactor. A
separate infeed and metering system is associated with each
high-capacity burner. The fluidized fuel dust flows to the burners
by applying a pressure differential between the metering tanks and
the burners of the gasification reactor. The amount of flowing fuel
dust is measured, regulated, and monitored by measurement devices
and monitors.
[0013] With the reactor according to the invention, there is still
also the ability to pulverize the undried fuel to a grain size of
<200 .mu.m and to mix the pulverized fuel with water or oil and
to feed it as a slurry to the burners of the gasification reactor.
The method of infeed, which is not described at this point, is
configured by one skilled in the art according to known
methods.
[0014] An oxidizing medium containing free oxygen is supplied to
the burners at the same time, and the slurry is converted to crude
synthesis gas by partial oxidation. The gasification takes place at
temperatures between 1,200 and 1,900.degree. C. and at pressures up
to 80 bar. The reactor has a cooled reaction chamber contour that
is made up of a cooling shield. This consists of a tubular shield
welded gas-tight that is studded and lined with a material that is
a good heat conductor.
[0015] The crude gas produced in the gasification reactor leaves
the gasification reactor together with the liquid slag formed from
the fuel ash and is sent to a chamber located perpendicularly below
it, in which the hot crude gas and the liquid slag are cooled by
injecting water. The gas can be cooled completely down to the
condensation point of the gas by spraying in excess water. The
temperature is then between 180 and 240.degree. C., depending on
the pressure. However, it is also possible to feed in only a
limited amount of cooling water and to cool the crude gas and slag
by partial cooling to 700 to 1,100.degree. C., for example, and
then to utilize the sensible heat of the crude gas to produce steam
in a waste heat boiler. Partial quenching or partial cooling
prevents or sharply reduces the risk of slag caking on the tubes of
the waste heat boiler. The water or recycled gas condensate needed
for complete or partial cooling is supplied through nozzles that
are located directly on the jacket of the cooling chamber. The
cooled slag is collected in a water bath and is discharged from the
process. The crude gas cooled to temperatures between 200 and
300.degree. C. is then sent to a crude gas scrubber, which is
preferably a Venturi scrubber.
[0016] The entrained dust is thereby removed down to a particle
size of about 20 .mu.m. This degree of purity is still inadequate
for carrying out subsequent catalytic processes, for example crude
gas conversion. Salt mists are also entrained in the crude gas,
which have detached from the powdered fuel during gasification and
are carried off with the crude gas. To remove both the fine dust
<20 .mu.m and the salt mists, the scrubbed crude gas is fed to a
condensation step in which the crude gas is chilled indirectly by 5
to 10.degree. C. Water is thereby condensed from the crude gas
saturated with steam, which takes up the described fine dust and
salt particles. The condensed water containing the dust and salt
particles is separated from the crude gas in a following separator.
The crude gas purified in this way can then be fed directly, for
example, to a desulfurization system.
BRIEF DESCRIPTION OF THE DRAWINGS
[0017] Other objects and features of the present invention will
become apparent from the following detailed description considered
in connection with the accompanying drawings. It is to be
understood, however, that the drawings are designed as an
illustration only and not as a definition of the limits of the
invention.
[0018] In the drawings, wherein similar reference characters denote
similar elements throughout the several views:
[0019] FIG. 1 shows a block diagram of the technology according to
the invention;
[0020] FIG. 2 shows a metering system for pulverized fuel according
to the invention;
[0021] FIG. 3 shows a device for feeding pulverized fuel for
high-capacity generators;
[0022] FIG. 4 shows a gasification reactor with full quenching;
and
[0023] FIG. 5 shows a gasification reactor with partial
quenching.
DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENT
[0024] FIG. 1 shows a block diagram of the process steps of
pneumatic metering of pulverized fuel, gasification in a
gasification reactor with cooled reaction chamber structure 2,
quench-cooling 3, crude gas scrubbing 4, in which there can be a
waste heat boiler 4.1 between the quench-cooling 3 and the crude
gas scrubbing 4, and a condensation or partial condensation 5
follows the crude gas scrubber 4.
[0025] FIG. 2 shows a metering system for pulverized fuel
consisting of a bunker 1.1 followed by two pressurized sluices 1.2,
into which lead lines 1.6 for inert gas, and at the top of which
depressurization lines 1.7 exit, with lines to the metering tank
1.3 leaving the pressurized sluices 1.2 from the bottom. There are
fittings on the pressurized sluices 1.2 for monitoring and
regulating. A line 1.5 for fluidizing gas leads into the metering
tank from below, which provides for fluidizing the gas, and the
fluidized pulverized fuel is fed through the transport line 1.4 to
a gasification reactor 2.
[0026] FIG. 3 shows another design of the device for feeding
pulverized fuel for high-capacity generators 2, wherein a bunker
1.1 has three discharges for pulverized fuel, each leading to
pressurized sluices 1.2, with each of the three pressurized sluices
transporting pulverized fuel streams to one of three metering tanks
1.3, from which transport lines 1.3 lead to the dust burners 1.2
with oxygen infeed of the reactor. There are three dust burners 2.1
on each reactor 2 with oxygen feed, with an ignition and pilot
burner 2.2 to start the reaction. Because of such intensive
fluidized fuel flows and the presence of three burners 2.1, it is
possible to achieve maximum capacities of 1,000 to 1,500 megawatts
with reliable and safe operation.
[0027] FIG. 4 shows a gasification reactor 2 with full quenching 3,
with the ignition and pilot burner 2.2 and the dust burners 2.1,
through which the fluidizing gas or a slurry of fuel and liquid is
fed into the reactor, being positioned in the center of the head of
the reactor 2. The reactor has a gasification chamber 2.3 with a
cooling shield 2.4 whose outlet opening 2.5 leads to the
quench-cooler 3, whose quenching chamber 3.1 has quenching nozzles
3.2, 3.3, and a crude gas discharge 3.4, through which the finished
crude gas can leave the quench-cooler 3. The slag that leaves the
quench-cooler through an outlet opening 3.6 is cooled in the water
bath 3.5.
[0028] FIG. 5 shows a gasification reactor 2 with partial
quenching, with the gasification reactor located in the upper part,
in which dust burners 2.1 gasify the dust from the transport line
1.4, and with an ignition and pilot burner 2.2 positioned in the
center. Gasification reactor 2 has a bottom opening into quenching
chamber 3.1, into both sides of which lead quenching nozzles 3.2,
with waste heat boilers 4.1 placed below this.
[0029] The function will be described with a first example with
reference to material flows and procedural processes:
[0030] 240 Mg/h of pulverized coal is fed to a gasification reactor
with a gross capacity of 1500 MW. This pulverized fuel prepared by
drying and grinding crude bituminous coal has a moisture content of
5.8%, an ash content of 13 wt. %, and a calorific value of 24,700
kJ/kg. The gasification takes place at 1,550.degree. C., and the
amount of oxygen needed is 208,000 m.sup.3 I. H./h. The crude coal
is first fed to a state-of-the-art drying and grinding system in
which the water content is reduced to 1.8 wt. %. The grain size
range of the pulverized fuel produced from the crude coal is
between 0 and 200 .mu.m. The ground pulverized fuel (FIG. 1) is
then fed to the metering system, the functional principle of which
is shown in FIG. 2. The metering system consists of three identical
units, as shown in FIG. 3, with each unit supplying 1/3 of the
total amount of powder, or 80 Mg/h, each to a dust burner. The
three dust burners assigned to them are at the head of the
gasification reactor, whose principle is shown in FIG. 4. The
usable pulverized fuel according to FIG. 2, which shows one unit of
the powder metering system, goes from the operational bunker 1.1 to
alternately operated pressurized sluices 1.2. There are 3
pressurized sluices in each unit. Pressurized suspension to the
gasification pressure is performed with an inert gas such as
nitrogen, for example, which is fed in through the line 1.6. After
suspension, the pressurized pulverized fuel is fed to the metering
tank 1.3. The pressurized sluices 1.2 are depressurized through the
line 1.7 and can be refilled with pulverized fuel. The 3 mentioned
pressurized sluices in each unit are loaded alternately, emptied
into the metering tank, and depressurized. This process then begins
anew. A dense fluidized bed is produced in the bottom of the
metering tank 1.3 by feeding in a dry inert gas through the line
1.5, likewise nitrogen, for example, that serves as the transport
gas; 3 dust-transport lines 1.4 are immersed in the fluidized bed.
The amount of pulverized fuel flowing in the transport lines 1.4 is
measured and regulated in relation to the gasification oxygen. The
transport density is 250-420 kg/m.sup.3.
[0031] The gasification reactor 2 is shown and further explained in
FIG. 3. The pulverized fuel flowing through the transport lines 1.4
to the gasification reactor 2 is discharged into 3 metering
systems, each with a capacity of 80 Mg/h. The total of 9 transport
lines 1.4 lead in groups of three each to 3 gasification burners
4.1 located at the head of reactor 2. At the same time, 1/3 of the
total amount of oxygen of 208,000 m.sup.3NTP/h is fed to each
gasification burner. The dust burners are arranged symmetrically at
angles of 120.degree., and in the center there is an ignition and
pilot burner that heats the gasification reactor 2 and serves to
ignite the dust burner 4.1. The gasification reaction, or the
partial oxidation at temperatures of 1,550.degree. C., takes place
in the gasification chamber 2.3, which is distinguished by a cooled
reaction chamber contour 2.4. The monitored and measured amount of
pulverized fuel is subjected to ratio regulation with the supplied
oxygen, which provides that the ratio of oxygen to fuel neither
exceeds nor falls below a range of .lamda.=0.35 to 0.65. The value
of .lamda. represents the ratio of the needed amount of oxygen for
the desired partial oxidation to the amount of oxygen that would be
necessary for complete combustion of the fuel used. The amount of
crude gas formed is 463,000 m.sup.3NTP/h and is distinguished by
the following analysis: TABLE-US-00001 H.sub.2 19.8 vol. % CO 70.3
vol. % CO.sub.2 5.8 vol. % N.sub.2 3.8 vol. % NH.sub.3 0.03 vol. %
HCN 0.003 vol. % COS 0.04 vol. % H.sub.2S 0.4 vol. %
[0032] The hot crude gas at 1,550.degree. C. leaves the
gasification chamber 2.3 together with the liquid slag through the
discharge 2.5 and is cooled to 212.degree. C. in the quenching
chamber 3.1 by injecting water through the rows of nozzles 3.2 and
3.3, and is then sent through the outlet 3.4 to the crude gas
scrubber 4, which serves as a water scrubber to remove dust. The
cooled slag is collected in a water bath 3.5 and is discharged
downward. The crude gas washed with water after the water scrubber
4 is sent for partial condensation 5 to remove fine dust <20
.mu.m in size and salt mists not separated in the water scrubber 4.
For this purpose, the crude gas is cooled by about 5.degree. C.,
with the salt particles dissolving in the condensed water droplets.
The purified crude gas saturated with steam can then be fed
directly to a catalytic crude gas converter or to other treatment
stages.
[0033] According to Example 2, the process of pulverized fuel feed
is to occur according to FIG. 2 and FIG. 3, and the actual
gasification in the same way as in Example 1. The hot crude gas and
the hot liquid slag likewise pass through discharge 2.5 into a
quenching chamber 3.1, in which the crude gas is cooled to
temperatures of 700-1,100.degree. C., not with excess water, but
only by spraying in a limited amount of water through nozzle rings
3.2, and are then sent to the waste heat boiler 4.1 to utilize the
heat of the crude gas to produce steam (FIG. 5). The temperature of
the partially cooled crude gas is chosen so that the slag particles
entrained by it are cooled in such a way as to prevent deposition
on the heat exchanger tubes. As in Example 1, the crude gas cooled
to about 200.degree. C. is then fed to the water scrubber and
partial condensation.
[0034] Accordingly, while only a few embodiments of the present
invention have been shown and described, it is obvious that many
changes and modifications may be made thereunto without departing
from the spirit and scope of the invention.
LIST OF REFERENCE SYMBOLS USED
1. Pneumatic metering systems for pulverized fuel
1.1 Bunker
1.2 Pressurized sluice
1.3 Metering tank
1.4 Transport line
1.5 Line for fluidizing gas.
1.6 Line for inert gas into 1.2
1.7 Depressurization line from 1.2
2. Gasification reactor with cooled reaction chamber structure
2.1 Dust burner with oxygen infeed
2.2 Ignition and pilot burner
2.3 Gasification chamber
2.4 Cooling shield
2.5 Discharge opening
3 Quenching cooler
3.1 Quenching chamber
3.2 Quenching nozzles
3.3 Quenching nozzles
3.4 Crude gas outlet
3.5 Water bath with slag
3.6 Bottom discharge from 3
3.7 Lining
4 Crude gas scrubber
4.1 Waste heat boiler
5 Condensation, partial condensation
* * * * *