U.S. patent number 3,876,392 [Application Number 05/373,553] was granted by the patent office on 1975-04-08 for transfer line burner using gas of low oxygen content.
This patent grant is currently assigned to Exxon Research and Engineering Company. Invention is credited to Theodore Kalina, Harry A. Marshall, Edward L. Wilson.
United States Patent |
3,876,392 |
Kalina , et al. |
April 8, 1975 |
Transfer line burner using gas of low oxygen content
Abstract
Carbonaceous solids are heated by passing a stream of such
solids through a transfer line burner, introducing a stream of gas
of low oxygen content into the burner near the lower end thereof in
a quantity sufficient to produce a transition from dense phase to
dilute phase flow, and introducing into the upper portion of the
burner at one or more points a gas of higher oxygen content in a
quantity sufficient to promote the conversion of carbon to carbon
dioxide and the generation of sufficient heat to raise the
temperature of the solids to the desired level.
Inventors: |
Kalina; Theodore (Morris
Plains, NJ), Marshall; Harry A. (Madison, NJ), Wilson;
Edward L. (Baytown, TX) |
Assignee: |
Exxon Research and Engineering
Company (Linden, NJ)
|
Family
ID: |
23472874 |
Appl.
No.: |
05/373,553 |
Filed: |
June 25, 1973 |
Current U.S.
Class: |
48/210; 48/202;
48/206 |
Current CPC
Class: |
C10J
3/723 (20130101); C10J 3/482 (20130101); C10J
3/78 (20130101); C10J 3/54 (20130101); C10J
2300/0946 (20130101); C10J 2300/0976 (20130101); C10J
2300/0959 (20130101); C10J 2300/1807 (20130101); C10J
2300/1606 (20130101); C10J 2300/093 (20130101); C10J
2300/0956 (20130101) |
Current International
Class: |
C10J
3/54 (20060101); C10J 3/46 (20060101); C10j
003/12 () |
Field of
Search: |
;48/202,204,206,210,197R,DIG.4 ;201/38,31 ;252/373 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Bashore; S. Leon
Assistant Examiner: Kratz; Peter F.
Attorney, Agent or Firm: Reed; J. E.
Claims
What is claimed is:
1. In an endothermic process carried out in a fluidized bed wherein
a stream of carbonaceous solids is continuously withdrawn from the
fluidized bed and introduced into the lower end of a transfer line
burner for the generation of heat and wherein unburned solids are
withdrawn from the said transfer line burner near the upper end
thereof and returned to the said fluidized bed, the improvement
which comprises introducing a gas of low oxygen content containing
up to about 10 volume percent of oxygen into said transfer line
burner containing said carbonaceous solids near the lower end
thereof in a quantity sufficient to produce dilute phase flow of
said carbonaceous solids upwardly within said transfer line burner
and introducing a gas having a higher oxygen content than said gas
of low oxygen content into an upper portion of said transfer line
burner in an amount sufficient to raise the temperature of said
unburned solids to a level above the temperature in said fluidized
bed.
2. A process as defined by claim 1 wherein said gas of low oxygen
content is a flue gas.
3. A process as defined by claim 1 wherein said gas of higher
oxygen content is air.
4. A process as defined by claim 1 wherein said gas of higher
oxygen content is introduced into said transfer line burner at a
plurality of points spaced about the periphery of said transfer
line burner.
5. A process as defined by claim 1 wherein said gas of higher
oxygen content is introduced into said transfer line burner at at
least two points sufficiently far apart to permit the consumption
of substantially all of the oxygen introduced at one of said points
before the oxygen introduced at the other of said points contacts
said carbonaceous solids.
6. A process as defined by claim 1 wherein said gas of low oxygen
content is a mixture of flue gas and air containing less than about
6 percent oxygen by volume.
7. A process as defined by claim 1 wherein at least part of said
gas of higher oxygen content is introduced into said transfer line
burner at a point near the upper end thereof.
8. A process as defined by claim 1 wherein said gas of higher
oxygen content is introduced into said transfer line burner in a
quantity sufficient to raise the temperature of said solids about
50.degree. to about 300.degree. F. above the temperature of said
fluidized bed.
9. A process as defined by claim 1 wherein said carbonaceous solids
comprise coal char particles.
10. In a coal gasification process wherein coal char particles are
continuously withdrawn from a fluidized bed gasifier, passed to a
transfer line burner for the combustion of carbon and the
generation of heat, and the heated particles are thereafter
returned to said gasifier, the improvement which comprises
introducing a gas of low oxygen content containing up to about 10
percent oxygen by volume and comprising flue gas into said transfer
line burner containing said char particles near the lower end
thereof in an amount sufficient to effect a transition in the flow
of said particles from dense phase flow to dilute phase flow,
introducing air into an upper portion of said burner in an amount
sufficient to heat said char particles to a temperature about
50.degree. to about 300.degree. F. above the temperature of said
fluidized bed, withdrawing a gas stream containing entrained
particles from the upper end of said burner, separating entrained
particles from said gas stream, and returning the separated
particles to said gasifier.
11. A process as defined by claim 10 wherein said gas of low oxygen
content is a flue gas containing less than 1 percent oxygen by
volume.
12. A process as defined by claim 10 wherein said gas of low oxygen
content is introduced into said burner in an amount between about
0.1 and about 5 cubic feet per pound of char solids, measured at
the burner temperature and pressure conditions.
13. A process as defined by claim 10 wherein the superficial gas
velocity in said burner above the point at which said gas of low
oxygen content is introduced is maintained between about 15 and
about 100 feet per second.
14. A process as defined by claim 10 wherein said air is introduced
into said burner at at least two vertically-spaced points
sufficiently far apart to permit the consumption of substantially
all of the oxygen introduced at the lowermost of said points before
oxygen introduced at a higher point contacts said char
particles.
15. A process as defined by claim 10 wherein said gas of low oxygen
content is a mixture of flue gas and air containing less than about
6% oxygen by volume.
Description
BACKGROUND OF THE INVENTION
1. Field of the Invention
This invention relates to the heating of fluidized beds containing
coal particles or other carbonaceous solids and is particularly
directed to coal gasification and related processes in which heat
is generated by burning a portion of the carbonaceous solids in a
transfer line burner.
2. Background of the Invention
Fluidized bed processes for the conversion of coal and similar
carbonaceous materials into gases useful as fuels normally require
the continuous input into the system of large quantities of heat.
One of the methods by which this can be done is through the use of
a transfer line burner. Such a burner normally consists of a large
vertical line into the lower end of which finely divided coal char
or similar carbonaceous material is introduced from the fluidized
bed reaction zone. Air or other oxygen-containing gas is introduced
into the burner near the lower end thereof in a sufficient quantity
to carry the carbonaceous solids upwardly through the burner in
dilute phase flow. The oxygen present in the gas stream burns a
portion of the carbon from the solids, thus generating sufficient
heat to raise the unburned particles to the desired temperature
level. The hot solids carried overhead by the combustion gases are
removed by means of cyclone separators or similar equipment and
recycled to the fluidized bed. The gases, which will normally
contain ash and fines not removed by the separation equipment, are
then generally scrubbed and handled in the conventional manner.
The use of a transfer line burner for heating solids withdrawn from
a fluidized bed as described above has important advantages over
other heat-generating systems but also has certain disadvantages.
Experience has shown that the combustion taking place in the burner
is difficult to control. The transient temperature rise which takes
place directly above the air injection point is high and may result
in localized overheating in areas where the relative ratio of air
to char or other carbonaceous solids is higher than average.
Maldistribution is particularly apt to occur as the char entering
the burner moves from the region of dense phase flow into the
region of dilute phase flow near the point of air injection. The
char solids employed may contain ash having a fusion temperature
only slightly higher than the desired transfer line exit
temperature and hence fused ash deposits may form in such areas of
localized overheating. Such deposits may produce plugging problems
and other difficulties. In addition, the efficiency with which the
combustion air is utilized may be reduced considerably due to the
reduction of carbon dioxide to carbon monoxide as the combustion
gases move upwardly in contact with the hot char. This increases
the cost of operating the transfer line burner and may make it more
difficult to handle the flue gases.
SUMMARY OF THE INVENTION
The present invention provides an improved method for the operation
of transfer line burners used in coal gasification and similar
operations which at least in part eliminates the difficulties
outlined above. In accordance with the invention, it has now been
found that the operation of such burners can be significantly
improved by injecting sufficient flue gas or other gas of low
oxygen content into the lower end of the burner to convey the
carbonaceous particles upwardly in the burner and produce a
transition from dense phase to dilute phase flow and then injecting
air or other gas of higher oxygen content into the burner at one or
more higher points in a quantity sufficient to convert carbon to
carbon dioxide and generate the heat required to elevate the
carbonaceous particles to the desired final temperature. The gas
introduced near the lower end of the burner to effect the
transition from dense phase to dilute phase flow may contain up to
about 10 percent oxygen by volume but will preferably contain less
than about 6 percent by volume. This results in relatively low
temperatures in the lower part of the burner and thus avoids
localized overheating and ash fusion problems in the area where the
transition from dense phase flow to dilute phase flow takes place.
The introduction of air or other gas of higher oxygen content at
one or more points in the upper part of the burner permits
generation of the heat required to raise the temperature of the
solids to the desired level and reduces the time during which
carbon dioxide contacts the hot carbonaceous solids. This in turn
decreases the production of carbon monoxide by the reaction:
CO.sub.2 +C .fwdarw. 2CO, and improves the thermal efficiency of
the process.
Studies have shown that the rate at which carbon dioxide reacts
with the solid carbonaceous particles tends to be proportional to
the total surface area of the particles, including the area of the
internal pores; whereas the primary combustion reaction wherein
carbon is burned to carbon dioxide tends to proceed at a rate
proportional to only the external surface area of the solid
particles. Since the internal surface area is normally much greater
than the external area, the reaction of carbon dioxide with carbon
to form carbon monoxide tends to reduce the size of large and small
particles alike. Because the fine particles have a much greater
external surface-to-internal surface ratio than do the larger
particles, the introduction of the combustion air into the upper
part of the burner tends to minimize the overall reduction in
particle size and instead promotes the preferential burning of
fines carried over from the fluidized bed reaction zone to generate
heat and carbon dioxide. This results in more efficient utilization
of the carbonaceous solids by reducing the amount of unburned fines
carried overhead with the flue gases.
As indicated above, the method of the invention makes possible
significant improvements in the operation of transfer line burners
for the heating of coal char particles and similar finely-divided
carbonaceous solids. The introduction of recycled flue gas or a
similar gas stream of low oxygen content into the lower part of the
burner to produce a transition from dense phase to dilute phase
flow and the injection of air or other oxygen-containing gas for
combustion of carbon to carbon dioxide into the burner at a higher
point or points eliminates localized overheating in the transition
zone and related problems due to ash fusion, results in more
efficient combustion and the transfer of more heat to the suspended
solids, and permits significant reductions in the amount of carbon
monoxide and fines in the flue gases, thus reducing pollution
problems and simplifying later treatment of the gas stream to
comply with applicable pollution control regulations. These and
other advantages provide economic incentives for use of the
method.
BRIEF DESCRIPTION OF THE DRAWING
The single FIGURE in the drawing is a schematic flow sheet of a
process for the production of a methane-rich gas from coal in which
the improved transfer line burner of the invention is employed.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
The drawing depicts a process for the production of product gases
of relatively high methane content from bituminous coal,
subbituminous coal, lignite, or similar carbonaceous solids. The
solid feed material employed in the process, preferably a
bituminous or lower rank coal, is introduced into the system
through line 10 from a suitable feed preparation plant or storage
facility which is not shown in the drawing. To facilitate handling
of the solid feed material in a fluidized state, the coal or other
carbonaceous material is introduced into the system in the form of
finely-divided particles, preferably less than about 8 mesh on the
Tyler screen scale. The process depicted is operated at elevated
pressure and hence the coal or other feed material introduced
through line 10 is fed into vessel 11, from which it is discharged
through a star wheel feeder or similar feeding device 12 into line
13 at the system operating pressure or at a slightly higher
pressure. In lieu of or in addition to vessel 11 and star wheel
feeder 12, parallel lock hoppers, aerated stand pipes operated in
series, or other conventional equipment may be employed to permit
introduction of the input stream of coal or other solids into the
system at the required pressure.
A feed gas stream is introduced into the system through line 14 to
permit the entrainment of solid particles from line 13 and the
introduction of the solids into gasifier 15. High pressure steam,
product gas, or an inert gas may be employed as the feed gas. The
use of recycled product gas simplifies downstream processing of the
product and is normally preferred. The feed gas stream is
introduced into the system at a pressure between about 50 and about
1000 psig, depending upon the pressure at which gasifier 15 is
operated and the solid feed material employed. This stream is
injected into the gasifier through one or more shrouded nozzles 16
into which steam is admitted through line 17 to keep the nozzle
temperature below about 600.degree. F. and thus minimize
difficulties due to fouling of the nozzle with agglomerating coal
solids. If an agglomerating coal feed material is employed, an
injection nozzle designed to promote intimate and extremely rapid
mixing of the injected coal with the hot solids present in the
gasifier will normally be used. Nozzles especially designed for
this purpose have been described in the literature and will be
familiar to those skilled in the art.
The gasifier vessel 15 which is employed in the system shown in the
drawing contains a fluidized bed of char particles introduced into
the lower part of the vessel through line 18. Steam for maintaining
the particles in the fluidized state and reacting with the char to
produce a synthesis gas containing substantial quantities of
hydrogen and carbon monoxide is introduced into line 18 by means of
line 19. Additional steam may be introduced through line 20. The
total steam rate will generally range between about 0.5 and about
2.0 pounds of steam per pound of coal feed. The entering steam and
char particles form a fluidized bed which extends upwardly above
distribution grid or similar device 21 to a level above the point
at which the coal particles are introduced through nozzle 16. The
upper surface of this fluidized bed is indicated by reference
numeral 22.
The lower portion of the fluidized bed in gasifier 15 between grid
21 and the level at which the coal solids are introduced, indicated
generally by reference numeral 23, serves as a steam gasification
zone. Here the steam introduced through lines 19 and 20 reacts with
carbon in the hot char to form synthesis gas in accordance with the
reaction: H.sub.2 O+C .fwdarw. H.sub.2 +CO. At the point of steam
injection near the bottom of the gasifier, the hydrogen
concentration in the gaseous phase of the fluidized bed is
essentially zero. As the steam moves upwardly through the fluidized
char particles, it reacts with the hot carbon to produce synthesis
gas and the hydrogen concentration in the gaseous phase therefore
increases. The temperature in the steam gasification zone will
generally range between about 1450.degree. and about 1800.degree.
F. Depending upon the particular feed material and the particle
sizes employed, the gas velocities in the fluidized bed will
normally range between about 0.2 and about 3.0 feet per second.
The upper part of the fluidized bed in reactor vessel 15, indicated
generally by reference numeral 24, serves as a hydrogasification
zone where the feed coal is devolatilized and a portion of the
rapidly convertible carbonaceous material in the coal reacts with
hydrogen generated in the steam gasification zone to produce
methane as one of the principal products. The point at which the
coal feed stream is introduced into the gasifier through nozzle 16
and hence the location of the steam gasification and
hydrogasification zones depends primarily upon the properties of
the particular coal or other carbonaceous solid which is employed
as the feedstock. It is generally preferred to select the nozzle
location so that the methane yield from the gasifier will be
maximized and the tar yield will be minimized. Generally speaking,
the amount of methane produced increases as the coal feed injection
point is moved nearer the top of the reaction vessel. The tar
formed from some coals has a tendency to foul downstream processing
equipment. The tar yield normally increases as the coal injection
point is moved upwardly in the gasifier, and decreases as the coal
input point is moved nearer the bottom of the reaction vessel,
other operating conditions being the same. The coal feed stream
should therefore generally be injected into gasifier 15 at a point
where the hydrogen concentration in the gas phase is in excess of
about 15 percent by volume, preferably between about 25 percent and
about 50 percent by volume. To secure acceptable methane
concentrations in the product gas stream, the upper surface 22 of
the fluidized bed should normally be located at a level
sufficiently above the nozzle 16 to provide at least about 4
seconds of residence time for the gas phase in contact with the
fluidized solids in hydrogasification zone 24. A residence time for
the gas in contact with the solid phase above the point of coal
feed injection between about 7 and about 20 sec. is generally
preferred. It will be understood, of course, that the optimum coal
injection point and the optimum gas residence time above the point
of coal injection will vary with different types and grades of feed
coal and will also change with variations in the gasifier
temperature, pressure, steam rate, and other process conditions.
Higher rank coals normally require somewhat more severe reaction
conditions and longer gas residence times to obtain high methane
yields than do coals of lower rank. Similarly, higher reactor
temperatures and lower steam rates, for a given solids holdup below
the coal injection point, generally tend to increase the hydrogen
concentration in the gas phase and thus reduce the gas residence
time needed for acceptable methane yields from a particular feed
coal.
The heat required to sustain the overall endothermic reaction
taking place within gasifier 15 and maintain the gasifier operating
temperature within the range between about 1500.degree. and about
1800.degree. F. is provided by withdrawing a portion of the char
solids from the fluidized bed through line 25 and passing this
material into the lower end of transfer line burner 26. Steam may
be injected into line 25 in the vicinity of bends in the line in
order to promote smooth flow of the solids and avoid any danger of
clogging. The solid particles moving downwardly through line 25
will be in dense phase flow. Recycled flue gas or a mixture of flue
gas and air containing up to about 10 percent, preferably less than
6 percent, oxygen by volume is introduced through line 27 and
multiple injection nozzles 28 into the solids stream near the
bottom of burner 26, preferably in a volume sufficient to provide
the particle and gas velocities necessary for the transition from
dense phase to dilute phase flow. The recycled flue gas will
normally be injected in an amount between about 0.1 and about 5
actual cubic feet of gas per pound of char solids, as measured at
the temperature and pressure of the mixed gas and char. The
superficial gas velocity in the transfer line burner above the flue
gas injection nozzles 28 will normally range between about 15 and
about 100 feet per second. The recycled flue gas will preferably
contain less than 1 percent oxygen by volume and will consist
primarily of nitrogen and carbon dioxide. Small amounts of water
vapor, carbon monoxide, and other gases will, of course, also be
present. As the recycled flue gas and entrained solids move
upwardly within the transfer line burner, little combustion takes
place. At a higher point in the burner, a gas of higher oxygen
content, preferably air, is injected into the burner through lines
29 and 30 and multiple injection nozzles 31 spaced at intervals
about the periphery of the burner to provide intimate contact
between the upflowing solids and injected gas.
The oxygen in the injected gas stream rapidly reacts with carbon on
the surface of the entrained particles to form carbon dioxide. This
reaction is accompanied by the reduction of carbon dioxide by hot
carbon to form carbon monoxide which takes place more slowly. After
essentially all the free oxygen in the gas stream has been
exhausted, this second reaction tends to cause a reduction in the
carbon dioxide content and a corresponding increase in the carbon
monoxide content of the gas. The discharge of substantial
quantities of carbon monoxide represents a loss in the thermal
efficiency of the process. To maintain an acceptably low carbon
monoxide concentration in the burner gases discharged from the
system, all or part of the oxygen used to support combustion should
therefore be injected into the burner at a point or points
sufficiently near the upper end of the burner that the exposure of
carbon dioxide to hot carbon in the absence of free oxygen is
minimized. Studies of a typical transfer line burner used in coal
gasification operations have shown that the injected oxygen is
generally consumed by the time the gases have moved downstream from
the injection point a distance of from about 30 to about 36 inches.
This distance will vary, of course, with changes in the dimensions
of the burner, the volume of gas injected, the oxygen content of
the gas, the type and amount of char solids entrained in the gas,
and other factors. The point at which essentially all the oxygen
has been consumed for a particular burner and said operating
conditions can be calculated or determined by taking gas samples
from the burner and hence the optimum injection point or points can
be located.
As indicated earlier, it may be preferred to introduce the
combustion oxygen into the burner at two or more points along the
length of the burner in order to further reduce the danger of
localized overheating and fusion of the ash. If this is done, the
points selected should be sufficiently far apart to permit the
consumption of substantially all of the oxygen introduced at each
point before the oxygen introduced at the next point contacts the
upflowing carbonaceous solids in the gas stream. In the system
shown in the drawing, a portion of the oxygen-containing gas passes
through line 32 and is introduced into the burner through one or
more downstream injection lines 33 and 34. The associated injection
nozzles 35 and 36 are spaced about the periphery of the burner to
provide intimate contact between the upflowing solids and injected
gas, thus resulting in more efficient utilization of the oxygen and
further reducing the danger of localized overheating of the
entrained solids. The amount of oxygen introduced through nozzles
31, 35, and 36 should be sufficient to generate enough heat to
raise the temperature of the unburned solids entrained in the gas
to a temperature of from about 50.degree. to about 300.degree.
higher than that in the fluidized bed in reaction vessel 15. A
temperature rise of about 200.degree. F. is generally preferred.
The quantity of oxygen-containing gas needed to produce this
temperature rise will depend upon the oxygen content of the
injected gas, the input temperature of the gas stream, the type and
quantity of carbonaceous solids moving upwardly within the burner,
the composition of the flue gas, and the heat losses from the
burner and can be readily calculated for any particular burner and
set of operating conditions.
The rapid combustion of carbon on the surface of the entrained
carbonaceous solids in response to the introduction of
oxygen-containing gas at one or more points in the upper portion of
the burner results in the conversion of carbon to carbon dioxide
and the generation of sufficient heat to raise the temperature of
the unburned solids to the desired level. The hot gases and
entrained solids are withdrawn from the burner and passed rapidly
to separation zone 37 to minimize the conversion of the carbon
dioxide to carbon monoxide by reaction with the hot carbon. The
separation zone will normally comprise one or more cyclone
separators designed to remove entrained solids greater than about
325 mesh on the Tyler screen scale from the gas stream. These hot
carbonaceous solids separated from the gas are withdrawn to dipleg
38 and returned to the fluidized bed through inlet 18 at the bottom
of reaction vessel 15. Flue gas containing fines not removed from
the gas stream is taken overhead from the separation zone through
line 39 and sent to downstream equipment for removal of the fines
and recovery of heat from the gas. The amount of fines in the flue
gas will generally be somewhat lower than in a conventional system
where substantially greater conversion of carbon dioxide to carbon
monoxide takes place. Similarly, the carbon monoxide content of the
flue gas will be relatively low and hence further processing of the
gas to comply with applicable pollution control regulations will be
less costly than in a conventional system. Conventional equipment
may be employed for the downstream removal of fines and recovery of
heat from the gas.
The product gas formed in fluidized bed reaction vesssel 15 passes
through a separation zone 40 which will normally consist of one or
more cyclone separators and is taken overhead through line 41. The
more effective utilization of relatively fine char particles in the
burner system results in the return of fewer fines to the fluidized
bed through dipleg 38 and injection nozzle 18 and thus reduces the
range of particle sizes within the fluidized bed. This permits
better control of the bed, makes possible higher gas velocities
within the reactor, and reduces somewhat the volume of fines taken
overhead with the product gas. This all tends to improve carbon
utilization in the process and results in greater thermal
efficiency than might otherwise be obtained.
The nature and objects of the invention can be further illustrated
by considering the following specific example of a coal
gasification process carried out in accordance therewith. A
subbituminous Western coal dried to 4 weight percent moisture and
ground and screened to a particle size less than about 8 Tyler mesh
is fed into a gasifier system of the type shown in the drawing, at
a feed rate of 100,000 pounds per hour. The ultimate analysis of
the feed coal is:
Pounds/Hour Carbon 65,700 Hydrogen 4,600 Oxygen 16,400 Nitrogen 900
Sulfur 500 Ash 7,900 Water 4,000 Total 100,000
The feed coal is introduced into the gasifier with 16,700 pounds
per hour of steam. The gasifier operates at a pressure of about 165
psig.
The coal flows into the upper hydrogasification zone where
devolatilization takes place. Steam at a temperature of 400.degree.
F. and a pressure of 175 psig is introduced into the lower part of
the gasifier at the rate of 47,300 pounds per hour. Synthesis gas
produced by reaction of the steam with char in the steam
gasification zone moves upwardly through the fluidized bed with a
gas velocity of about 1.0 foot per second. In the hydrogasification
zone, this synthesis gas reacts with the volatile products from the
feed coal to produce the methane-rich product gas. This gas is
taken overhead from the gasifier at the rate of 113,800 pounds per
hour. The component mass rates for this gas are as follows:
Pounds/Hour CO 35,700 CO.sub.2 26,600 H.sub.2 4,400 H.sub.2 O
31,200 CH.sub.4 9,000 C.sub.2.sup.+ Hydrocarbons 4,600 Other 2,300
Total 113,800
To maintain the fluidized bed temperature of about 1650.degree. F.,
char particles are continuously withdrawn from the fluidized bed in
the gasifier and passed to the transfer line burner at a rate of
about 2,138,000 pounds per hour. To promote transition of the solid
stream from dense phase to dilute phase flow, diluent gas is
introduced into the lower end of the burner at the rate of about
22,600 standard cubic feet per minute. This is equivalent to about
0.21 actual cubic feet per pound of char solids. This diluent gas
consists of flue gas recycled from the burner and has the following
component mass rates:
Pounds/Hour CO 4,600 CO.sub.2 27,300 H.sub.2 100 H.sub.2 O 1,200
N.sub.2 74,600 Others 1,400 Total 109,200
The diluent gas rate is sufficient to produce a superficial gas
velocity of 30 feet per second in the lower section of the transfer
line burner.
Air is introduced into the upper portion of the transfer line
burner at the rate of 55,000 standard cubic feet per minute, having
the following component mass rates:
Pounds/Hour O.sub.2 58,400 N.sub.2 190,200 Other 3,200 Total
251,800
The air stream will normally be preheated to a temperature of
450.degree. F. The combustion gases and entrained solids are taken
overhead from the burner at a temperature of about 1850.degree. F.
and separated to remove solid particles greater than about 325
Tyler mesh. The flue gas stream from the separator is treated
downstream for the removal of fines. The flue gas stream has the
following component mass rates:
Pounds/Hour CO 16,400 CO.sub.2 96,400 H.sub.2 200 H.sub.2 O 13,000
N.sub.2 263,700 Others 4,800 Total 394,500
About 16,700 pounds per hour of fines having an average particle
size of about 20 microns are recovered from the flue gas stream.
The larger particles removed from the gas in the separation zone at
the upper end of the transfer line burner are recycled to the
gasifier at the rate of about 2,087,800 pounds per hour. A portion
of the flue gas is cooled and recompressed for use as the diluent
gas shown above.
* * * * *