U.S. patent number 3,840,354 [Application Number 05/237,333] was granted by the patent office on 1974-10-08 for three-stage gasification of coal.
This patent grant is currently assigned to The United States of America as represented by the Secretary of the. Invention is credited to Ernest E. Donath.
United States Patent |
3,840,354 |
Donath |
October 8, 1974 |
THREE-STAGE GASIFICATION OF COAL
Abstract
A process for the production of methane-rich fuel gas by the
gasification of coal in three stages. In the first stage, partially
gasified char recycled from the process is reacted with oxygen and
superheated steam at pressures greater than 50 atmospheres and
temperatures greater than 2,500.degree.F. to yield a first stage
synthesis gas containing hydrogen and carbon oxides. In the second
stage, the first stage synthesis gas is reacted with superheated
steam and coal at pressures in excess of 50 atmospheres and
temperatures in excess of 1,600.degree.F. to yield a partially
gasified char entrained in a second stage product gas containing
methane, hydrogen and carbon oxides. In the third stage, char and
gases from the second stage form a fluidized bed reacting at a
pressure in excess of 50 atmospheres and at a temperature in excess
of 1,500.degree.F. to form char entrained in a third stage product
gas containing methane, hydrogen and oxides of carbon. The third
stage char and third stage product gas are separated with the char
recycled to the first stage and the product gas is purified by the
removal of carbon oxides, hydrogen sulfide and other impurities and
the purified product gas is methanated to produce the methane rich
fuel gas. Slag formed in the first and second stages is collected
in the third stage and is removed from the process after
elutriation from the slag of char collected with the slag, which
char is returned to the third stage.
Inventors: |
Donath; Ernest E. (St. Croix,
VI) |
Assignee: |
The United States of America as
represented by the Secretary of the (Washington, DC)
|
Family
ID: |
22893291 |
Appl.
No.: |
05/237,333 |
Filed: |
March 23, 1972 |
Current U.S.
Class: |
48/202; 48/210;
518/705; 48/206; 518/703 |
Current CPC
Class: |
C10J
3/845 (20130101); C10J 3/463 (20130101); C10J
3/485 (20130101); C07C 1/02 (20130101); C10J
3/76 (20130101); C10J 3/78 (20130101); C10J
3/466 (20130101); C10J 3/74 (20130101); C10J
3/84 (20130101); C07C 1/02 (20130101); C07C
9/04 (20130101); C10J 2300/093 (20130101); C10J
2300/0979 (20130101); C10J 2300/1823 (20130101); C10J
2300/0946 (20130101); Y02P 20/129 (20151101); C10J
2300/0959 (20130101) |
Current International
Class: |
C07C
1/00 (20060101); C07C 1/02 (20060101); C10J
3/46 (20060101); C10j 003/16 () |
Field of
Search: |
;48/202,210,77,204,197R,206,73,99 |
References Cited
[Referenced By]
U.S. Patent Documents
Other References
"Computer Study of 2 Stage Reactions in the BCR2 Stage Coal
Gasification Process" E. Donath, R. Glenn, American Chem. Society
Sept., 1967 pg. 1..
|
Primary Examiner: Bashore; S. Leon
Assistant Examiner: Kratz; Peter F.
Attorney, Agent or Firm: Price, Jr.; Stanley J.
Claims
I claim:
1. A process for gasifying coal comprising,
introducing a partially gasified recycle char into a first
gasification zone,
introducing oxygen and steam into said first gasification zone,
reacting said oxygen and steam with said partially gasified recycle
char at a pressure of at least 50 atmospheres to produce a first
zone synthesis gas comprising hydrogen and oxides of carbon and a
molten slag formed from a molten ash of said partially gasified
char,
introducing said first zone synthesis gas and said molten slag into
a second gasification zone below said first zone,
introducing coal and steam into said second gasification zone,
reacting said coal, steam, first zone synthesis gas and molten slag
in said second gasification zone at a pressure of at least 50
atmospheres to produce a second zone product comprising solidified
slag and a second zone partially gasified char entrained in a
second zone product gas comprising methane, hydrogen and oxides of
carbon,
introducing said second zone product gas and said second zone
partially gasified char into a third gasification zone,
forming in said third gasification zone a fluidized bed of said
second zone partially gasified char in a fluidizing stream of said
second zone product gas,
reacting said second zone partially gasified char in said third
gasification zone with said second zone product gas in said third
gasification zone to produce a third zone partially gasified char
entrained in a third zone product gas comprising methane, hydrogen
and oxides of carbon,
removing from said third gasification zone said third zone
partially gasified char entrained in said third zone product
gas,
separating said third zone partially gasified char from said third
zone product gas,
mixing said third zone partially gasified char with steam to
produce said partially gasified recycle char,
recycling said partially gasified recycle char to said first
gasification zone,
purifying said third zone product gas separated from said third
zone partially gasified char to remove carbon dioxide, hydrogen
sulfide and other impurities to produce a purified third zone
product gas, and
methanating the purified third zone product gas to produce a fuel
gas containing at least 70 percent methane by volume.
2. A process for gasifying coal as set forth in claim 1 which
includes,
conducting the reaction in said third gasification zone at a
temperature within the range of from about 1,500.degree.F. to about
1,600.degree.F.
3. A process for gasifying coal as set forth in claim 1 which
includes,
maintaining a residence for said second zone partially gasified
char in said third gasification zone of at least five times the
residence time of said second zone product gas in said third
gasification zone.
4. A process for gasifying coal as set forth in claim 1 which
includes,
passing said first zone synthesis gas and said molten slag from
said first gasification zone through a mixing zone prior to
introducing said first zone synthesis gas and said molten slag from
said first gasification zone into said second gasification zone to
assure rapid mixing and rapid reaction in said second gasification
zone between said coal, said first zone synthesis gas and said
steam and to assure the rapid transfer of heat from said molten
slag from said first gasification zone to said coal.
5. A process for gasifying coal as set forth in claim 1 which
includes,
moving downwardly through said first gasification zone said oxygen,
said steam and said partially gasified recycle char,
moving downwardly through said second gasification zone said first
zone synthesis gas, said solidified slag, said coal and said steam,
and
moving upwardly through said third gasification zone said second
zone partially gasified char and said second zone product gas.
6. A process for gasifying coal as set forth in claim 5 which
includes,
mixing said molten slag with said coal in said second gasification
zone to transfer heat from said molten slag to said coal and
thereby form a solidified particulate slag in said second
gasification zone,
collecting said solidified particulate slag and a portion of said
second zone partially gasified char in a lower portion of said
third gasification stage,
removing said solidified particulate slag and said second zone
partially gasified char from said third gasification zone,
contacting said solidified particulate slag and said second zone
partially gasified char with elutriating steam,
returning a portion of said elutriating steam with said second zone
partially gasified char entrained therein to said third
gasification stage for reaction therein, and
quenching said solidified particulate slag after elutriation.
7. A process for gasifying coal as set forth in claim 1
wherein,
at least part of said second gasification zone is enclosed by said
third gasification zone, and
introducing said second zone partially gasified char, said second
zone product gas and said slag directly into a portion of said
third gasification zone from said second gasification zone.
8. A process for gasifying coal as set forth in claim 1 which
includes,
mixing said third zone product gas and said third zone partially
gasified char with water to cool said third zone partially gasified
char,
separating said third zone partially gasified char into a heavier
coarse portion of said third zone partially gasified char and a
lighter fine portion of said third zone partially gasified char
entrained in said third zone product gas,
mixing said heavier coarse portion of said third zone partially
gasified char with steam,
recycling said heavier coarse portion of said third zone partially
gasified char with steam to said third gasification zone,
separating said lighter finer portion of said third zone partially
gasified char from said third zone product gas,
mixing said lighter fine portion of said third zone partially
gasified char with steam, and
recycling said lighter fine portion of said third zone partially
gasified char with steam to said first gasification zone.
Description
BACKGROUND OF THE INVENTION
1. Field of the Invention
This invention relates to the production of methane-rich fuel gas
by the gasification of coal in three stages at high pressures and
temperatures.
2. Description of the Prior Art
Methane-rich fuel gas is produced by a two-stage gasification
process wherein particulate coal and steam are reacted in the
second stage with synthesis gas from the first stage at a
temperature in excess of 1,600.degree.F. and a pressure in excess
of 50 atmospheres to produce char and a product gas containing
hydrogen, methane and oxides of carbon. The char and product gas
are withdrawn and separated and the product gas is thereafter
treated to remove carbon oxides and other diluents and is
ultimately methanated to produce a methane-rich fuel gas. The char
is recycled to the first gasification stage for reaction with steam
and oxygen at a temperature in excess of 2,500.degree.F. and a
pressure in excess of 50 atmospheres to produce a first stage
synthesis gas containing hydrogen and oxides of carbon for reaction
in the second gasification stage. A portion of the char, which has
low sulfur content, can be burned to produce process energy. Slag
produced from the reactions in the first and second stages
gravitates to the lower sections of the reactor in the first stage
where the slag is cooled and removed from the process. Reaction
times and residence times of the reactants in the first and second
stages are limited and minimized to prevent softening and
agglomeration of the coal in the second stage.
The two-stage gasification process described above was developed at
Bituminous Coal Research, Inc. at Pittsburgh, Pennsylvania (BCR).
The process is described in a publication of the Department of
Interior, Office of Coal Research (OCR), dated 1965 and entitled,
"Gas Generator-Research and Development Survey and Evaluation."
That process was described also in a computer study entitled,
"Computer Study of Stage-Two Reactions in the BCR Two-Stage Super
Pressure Gasification Process," presented at the national meeting
of the American Chemical Society, Division of Fuel Chemistry,
Chicago, Ill. in September, 1967.
SUMMARY OF THE INVENTION
This invention resides in a process for three-stage gasification of
coal to produce a methane-rich fuel gas. In the first stage,
recycled char is reacted at high temperature with oxygen and steam
at a pressure of at least 50 atmospheres to yield a first stage
synthesis gas containing hydrogen and carbon oxides. In the second
stage, synthesis gas from the first stage is reacted with
superheated steam and coal at a high temperature and at a pressure
of at least 50 atmospheres to produce a second stage product gas
containing methane, hydrogen and oxides of carbon. In the third
stage, partially gasified char is maintained as a fluidized bed by
second stage product gas which reacts with the char to yield
partially gasified char from the third stage entrained in a third
stage product gas containing methane, hydrogen and oxides of
carbon. The temperatures and residence times of reactants in the
first and second stages are controlled to convert char ash to
molten slag in the first stage and to convert coal partially into a
gas containing methane, hydrogen and carbon oxides, at temperatures
above the range of coal plasticity in the second stage. The
temperature in the third stage is lower, and the residence time of
the solid reactants in the third stage is longer, than those in the
first and second stages to permit more complete utilization of the
reactants in the third stage. The char and third stage product gas
are separated and, while the char is recycled to the first stage
for further reaction in the process, the third stage product gas is
purified for conversion and removal of carbon oxides, hydrogen
sulfide and other impurities and is thereafter methanated to
produce a fuel gas containing at least 70 percent methane.
In one embodiment, the third stage and the fluidized char bed are
in direct communication with a part of the second stage. In other
embodiments, the third stage is separated from the first and second
stages. Slag formed in the first and second stages is collected in,
and removed from, a lower portion of the third stage.
Third stage gasification of char fluidized in product gas from a
two-stage gasification process permits further reaction of the
partially gasified char in the hydrogen-rich second stage product
gas at lower temperatures and for longer residence times, thereby
providing a higher methane yield with greater carbon utilization at
lower oxygen requirements.
BRIEF DESCRIPTION OF THE DRAWINGS
FIG. 1 is a diagrammatic illustration of apparatus adapted for use
in the process of this invention wherein the third stage portion of
the gasification vessel communicates with the second stage
portion.
FIG. 2 is a diagrammatic illustration of apparatus adapted for use
in the process of this invention wherein the third stage is
separate from the first and second stages.
FIG. 3 is a diagrammatic illustration of apparatus adapted for use
with the process of this invention wherein the third stage is
separate from the first and second stages and a portion of the char
produced in the third stage is cooled and recycled to the third
stage.
FIG. 4 is a diagrammatic illustration of apparatus adapted for use
in the process of this invention wherein the third stage is
separate from the first and second stages and wherein char
separated from the second stage gas is moved into the third stage
and is fluidized in the third stage by hydrogen-rich gas passed
upwardly through the third stage to form a fluidized bed.
DESCRIPTION OF THE PREFERRED EMBODIMENTS
In this specification, the term "coal" means any carbonaceous
material including all ranks of coal, lignite, and the like.
The term "gasification" means the heating of coal in the presence
of reacting agents whereby all or part of the volatile portion of
the coal is liberated and at least part of the carbon in the
residual char is reacted with those reacting agents or with other
reactants present in the gasification process.
The term "product gas" means a methane containing gas such as the
gas produced in the third stage of the three stage gasification
process described herein.
THREE-STAGE GASIFICATION WITH PARTIALLY CONFINED SECOND STAGE
REACTION
In the process illustrated in FIG. 1, a gasification vessel,
indicated generally by reference numeral 10, includes a first stage
portion 12, a second stage portion 14 and a third stage portion 16.
Recycled partially gasified char is conducted through a conduit 18
to first stage portion 12 of gasification vessel 10. Oxygen and
steam are conducted through a conduit 20 into the first stage
portion 12 and are reacted therein with the partially gasified char
while flowing downwardly through the first stage portion 12. That
reaction yields a first stage synthesis gas containing hydrogen and
oxides of carbon and other products including molten slag formed
from char ash.
In first stage portion 12 of gasification vessel 10 the reaction is
conducted at a pressure of at least 50 atmospheres and preferably
at a pressure greater than 70 atmospheres. The temperature and
residence time of reactants in first stage portion 12 are
controlled to assure rapid gasification of the char at a
temperature above the char ash melting point. A temperature of at
least 2,500.degree.F. is preferred, and a residence time of less
than 2 seconds is preferred in the first stage of the process.
The molten slag and first stage synthesis gas flow downwardly
through a mixing portion, or throat, 22 in gasification vessel 10
wherein the velocity of the first stage synthesis gas and slag
flowing into the upper portion of the second stage portion 14 is
increased. Coal and steam are introduced through nozzles 24 into an
upper area 26 of second stage portion 14 near the location at which
mixing portion 22 opens into second stage portion 14.
Alternatively, coal and steam nozzles 24 can open into mixing
portion 22 above second stage portion 14. Feeding of coal and steam
through nozzles 24 and feeding of first stage synthesis gas and
molten slag through mixing portion 22 assure the rapid and intimate
mixing of those reactants upon their entry into the upper area 26
of second stage portion 14, thereby assuring rapid reaction of the
coal with the first stage synthesis gas and steam and rapid
transfer of a substantial quantity of sensible heat from the molten
slag to the reacting coal. As a consequence of the rapid transfer
of heat from the molten slag to the coal, the molten slag cools and
solidifies rapidly before any appreciable accumulation of molten
slag on the walls of the gasification vessel 10 in second stage
portion 14. The rapid transfer of heat from the slag to the coal
also provides more complete and efficient utilization of the
carbon.
In the second stage portion 14, the coal reacts with the steam and
first stage synthesis gas to yield a second stage product including
partially gasified char entrained in a second stage product gas
containing methane, hydrogen and oxides of carbon. The second stage
reaction is conducted at a pressure of at least 50 atmospheres, and
preferably greater than 70 atmospheres, and at a temperature and
residence time controlled to assure rapid reaction of the coal at a
temperature above the range of coal plasticity. It is preferred
that the second stage temperature be at least 1,600.degree.F. It is
preferred that the residence time for the coal in the second stage
be less than 10 seconds, and more preferably, less than 4
seconds.
At the bottom of the second stage portion 14, the partially
gasified char entrained in the second stage product gas, passes
through a deflection portion 28 of gasification vessel 10, which
changes the direction of flow of the second stage products and
diverts them into the third stage portion 16 which extends upwardly
around and partially encloses the second stage portion 14.
As a result of the rapid cooling of the molten slag in the upper
area 26 of second stage portion 14 and the further loss of heat by
the slag passing downwardly through second stage portion 14, the
slag solidifies to form granules and larger particles which
gravitate down through the entrained char and second stage product
gas and collect, by reason of their greater density and larger
size, in a slag collection portion 30 of gasification vessel 10
within third stage portion 16 below a deflection portion 28. The
slag collected in portion 30 passes downwardly through a conduit 32
into an elutriation portion 34 of gasification vessel 10 where the
slag is elutriated with steam, to separate the lighter particles of
partially gasified char which are trapped in slag collection
portion 30 from the slag. The elutriated char passes with a portion
of the elutriation steam upwardly into third stage portion 16.
Baffles or other deflecting means in the deflection portion 28
prevent the entry of the elutriated char into the second stage
portion 14.
The heavier slag particles pass with a portion of the elutriation
steam downwardly through a conduit 36 into a slag quenching portion
38 where the slag is quenched with water and ultimately removed
from the process through conduit 40 as cool slag.
The dimensions of the third stage portion 16 are selected and
maintained such that the char and second stage product gas form a
fluidized bed in third stage portion 16 which partially encloses
the second stage portion 14. The linear gas velocities in third
stage portion 16 are controlled and maintained to assure the
formation of the desired fluidized bed. Linear gas velocities in
third stage portion 16 are suitable in the range from about 0.5 to
about 20.0 feet per second and linear gas velocities in the range
of from about 1.0 to about 10.0 feet per second are preferred.
The reaction in the third stage of the process is conducted near
the pressure of the second stage. The temperature maintained in the
third stage is lower than the temperature in the second stage and
the residence time for char in the third stage is substantially
longer than the residence time in the first and second stages of
the process. A third stage temperature in the range of from about
1,500.degree.to about 1,650.degree.F. is suitable. In the third
stage the residence time of the char should be at least five times,
and preferably 20 or more times, the residence time of the second
stage product gas and other gases therein. A char residence time in
the third stage of 20 minutes or more is preferred, especially when
high rank coals are used.
The elutriation of the reaction of carbon with hydrogen to form
methane exhibits higher methane yields for lower temperatures.
Therefore, the reaction in the third stage at a temperature lower
than that in the second stage with longer residence and reaction
times in the presence of the larger amount of char and larger
volume of hydrogen rich product gas contained in the third stage,
results in a higher gasification rate and a higher yield of methane
with lower oxygen requirements than those for a two-stage
gasification process.
Among the products from the third gasification stage, partially
gasified char, entrained in a third stage product gas containing
methane, hydrogen and oxides of carbon, is withdrawn through
conduit 42 to a separator 44, such as a cyclone separator, where
the partially gasified char is separated from the third stage
product gas. The char is conducted through conduit 46 to a steam
ejector 48 where the char is mixed with steam at a pressure at
least slightly greater than the pressure in first gasification
stage. The char and steam are conducted through conduit 18 for
recycling to the first stage portion 12 for further reaction in the
process.
Separated third stage product gas is withdrawn through conduit 50
and conveyed to purification apparatus 52 wherein third stage
product gas is purified by conversion and the removal therefrom of
carbon oxides, hydrogen sulfide and other impurities. The purified
third stage product gas passes through conduit 54 to methanation
apparatus 56 wherein the purified third stage product gas is
catalytically methanated and removed through conduit 58 to yield a
fuel gas containing at least approximately 70 percent methane by
volume, and preferably at least 90 percent methane by volume.
THREE-STAGE GASIFICATION WITH SEPARATE THIRD STAGE
In the process illustrated in FIG. 2, certain process modifications
within the concept of this invention are illustrated. Partially
gasified recycle char mixed with steam is introduced through
conduit 60 into a first gasification stage portion 62 of a
two-stage gasification vessel indicated generally by reference
numeral 64. Oxygen and steam are introduced through conduit 66 into
the first stage portion 62 and reacted with the char therein to
produce a first stage synthesis gas.
The process illustrated in FIG. 2 does not include passage of the
first stage synthesis gas and other first stage reaction products
through a mixing portion or throat as was employed in the process
illustrated in FIG. 1. In the instant process, the synthesis gas
and other reaction products from the first stage pass directly into
the upper portion 68 of a second gasification stage portion 70,
where rapid and substantial mixing between and among the synthesis
gas and other reaction products from first stage are effected by
the introduction into the upper portion 68 of coal and superheated
steam through nozzles 72 controlled to provide the necessary
reactant velocities and direction to achieve the desired mixing and
rapid heat transfer reaction. The first stage and second stage
reaction temperatures, pressures and residence times are
substantially the same as for those described in the process
illustrated in FIG. 1.
In the instant process, a third gasification stage portion 74 is
provided and maintained separate from the first stage portion 62
and second stage portion 70. Partially gasified char from the
second stage, entrained in second stage product gas containing
methane, hydrogen and oxides of carbon, is conducted through a
conduit 76 to a lower portion 78 of third stage portion 74, where
the second stage char is maintained in a fluidized bed by the
hydrogen-rich second stage product gas. Third stage temperature,
pressure and residence times are substantially the same as those
described for the third stage of the process illustrated in FIG. 1.
It should be noted, however, that in the instant process, residence
times can be longer and methane yield and carbon utilization can be
higher while oxygen consumption is lower because separation of the
third stage portion 74 from contact with the second stage portion
70 avoids the transfer of heat from second stage portion 70 to the
fluidized char bed in the third stage portion 74, which heat
transfer might raise the temperature, especially in the upper
portion of the fluidized char bed in the third stage portion 74,
thereby tending to reduce the yield of methane from the reaction of
carbon with hydrogen.
In the instant process, slag is transported by the second stage
product gas and entrained char through conduit 76 for collection in
the lower portion 78 of third stage portion 74. The elutriation,
quenching and removal of slag from third stage portion 74 is
conducted as previously described for the process illustrated in
FIG. 1. Hereinafter, those process elements which are identical
with process elements described in previous embodiments and
drawings will be identified by identical reference numerals as used
in said previous embodiments and drawings.
The removal of third stage char and third stage product gas,
including their subsequent recycling and purification and
methanation, respectively, is the same as described for the process
illustrated in FIG. 1, with the exception that, in the instant
process, hydrogen sulfide gas, removed from the third stage product
gas in the purification process, is withdrawn through conduit 80
and reacted in a sulfur reclamation reactor, such as a Claus
reactor 82, to produce elemental sulfur.
SEPARATE THIRD STAGE GASIFICATION OF RECYCLED THIRD STAGE CHAR
In the process illustrated in FIG. 3, the process steps through the
first gasification stage and the second gasification stage are
identical with the process steps for the process illustrated in
FIG. 2 with the exception that the char and steam recycled to the
first stage has a slightly different composition, which will be
explained more fully below.
Second stage product gas and char, introduced into the third stage
portion 74 through conduit 76, are reacted in the third stage to
produce partially gasified char entrained in a third stage product
gas containing methane, hydrogen and oxides of carbon, while slag
collection, elutriation and removal from the third stage portion 74
are conducted as previously described.
In the instant process, third stage char and third stage product
gas are removed through a conduit 82 from third stage portion 74
and quenched with water or other suitable fluid, and passed to a
primary separator 84. Separator 84 separates the third stage
product gas, steam and fine char entrained therein from the coarse
heavier char particles from the third stage. The cooled coarse char
is conducted through a conduit 86 to a steam ejector 88. The steam
and coarse char are introduced through a conduit 90 into the lower
portion 78 of third stage portion 74 to enable further temperature
control of the reactants in that stage and to provide additional
carbon and other reactants in the char for the third stage
reaction. Recycling of additional quantities of char, at low
temperatures, to third stage portion 74 provides further increase
in methane yield and carbon consumption at low oxygen
requirements.
The third stage product gas and entrained fine char separated in
primary separator 84 is withdrawn therefrom through a conduit 92
and passed to a secondary separator 94, wherein the fine char is
separated from the third stage product gas which is conducted
through a conduit 76 to purification and methanation with
production of elemental sulfur as previously described in FIG. 2.
The separated fine char withdrawn from secondary separator 94 is
conducted through a conduit 98 to a steam ejector 100 for recycling
through conduit 102 as a mixture of steam and char at a pressure
greater than the pressure existing in the first stage.
SEPARATE THIRD STAGE GASIFICATION WITH A COUNTER FLOW FLUIDIZED
BED
In the process illustrated in FIG. 4, recycle char and steam are
introduced through a conduit 104 into a first gasification stage
portion 106 of a gasification vessel 108. Steam and oxygen are
introduced through a conduit 110 into first stage portion 106 and
flow upwardly therethrough with the recycled char into a second
gasification stage portion 112. The reaction conditions in the
first and second stages are similar to those described for the
other processes described herein except that flow through the first
and second gasification stages is in the upward direction and a
mixture of coal and steam is introduced through a conduit 114 into
second stage portion 112 above the first stage portion 106 for
entrainment in the first stage synthesis gas and other first stage
products as the synthesis gas and other products travel upwardly
into second stage portion 112.
Molten slag formed from char ash produced in the first and second
stages accumulates on the walls of the first and second stage
portions 106 and 112 of gasification vessel 108. The accumulated
molten slag gravitates to the lower portion 116 of the first stage
portion 106 where the molten slag collects and is removed through a
conduit 118 for quenching and disposal from the system.
Second stage product gas with entrained char is removed through a
conduit 120 and passed to a primary char separator 122. In
separator 122 the fine second stage char mixed with the second
stage product gas is separated and removed from coarse char which
is conducted through a conduit 124 to an upper portion 126 of third
gasification stage portion 128. As coarse char moves downwardly
through third stage portion 128, a hydrogen-enriched gas is
conducted through a conduit 130 to a lower portion 132 of third
stage portion 128 and travels upwardly through the third stage
portion 128 to form a fluidized bed with the downwardly moving
coarse char. The instant process enables the use of a smaller size
third stage portion 128 of gasification vessel 108 because the use
of hydrogen or a hydrogen-rich fluidizing gas permits higher
methane yields with smaller volumes of fluidizing gas.
The hydrogen-rich gas is compressed to a pressure of at least 1,100
psig. before introduction into the third stage and maintains the
gravitating coarse char in a fluidized bed. As the gravitating
coarse char passes the location of the point of introduction of the
hydrogen-rich gas at lower portion 146, the gravitating char enters
an elutriation portion 134 wherein the hydrogen-rich gas is
replaced by an elutriating fluid such as steam. Some char particles
are carried upwardly by the elutriating steam from elutriation
portion 134 and returned to the reaction in third stage.
The remaining char particles elutriated in elutriation portion 134
pass downwardly therefrom through a conduit 136 to a steam ejector
138. A mixture of steam and char is then recycled through conduit
104 to the first stage portion 106 as described above.
The second stage product gas with entrained fine char removed from
primary separator 122 is passed through a conduit 138 and mixed
with quenching water for introduction into secondary separator 140.
The third stage product gas with entrained char is conducted
through a conduit 142 from the upper portion 126 of third stage
portion 128 and mixes in conduit 138 with the quenched char and
second stage product gas from primary separator 122 for
introduction into secondary separator 140.
In secondary separator 140 the product gases from the second and
third stages are separated from the char from the second and third
stages. The separated char is conducted through a conduit 144 to an
intermediate portion 146 of the elutriation portion 134 to mix with
the coarse elutriated char in elutriation portion 134. The mixture
in elutriation portion 134 of coarse elutriated char and fine char
from separator 140 is introduced through the conduit 136 into steam
ejector 138 and pressurized to a pressure in excess of the pressure
existing in the first gasification stage. A resulting mixture of
char and ejector steam is recycled through the conduit 104 to the
first stage portion 106 for further reaction in the process.
The mixture of second and third stage product gases separated in
secondary separator 140 is conducted through conduit 148 to
purification apparatus 150 wherein the gases are passed through a
water-gas shift reactor and the hydrogen sulfide and carbon dioxide
are removed as separate streams. The hydrogen sulfide gas is
conducted through conduit 152 to a sulfur conversion reactor 154,
such as a Claus reactor, for conversion to elemental sulfur.
Part of the purified product gases may be conducted through
conduits 156 and 158 to a compressor 160 and then conducted through
a conduit 130 to the third stage portion 128 while the remaining
purified product gases are conducted through a conduit 162 to
methanation apparatus 164. Alternatively, a portion of the purified
product gases may be conducted through a conduit 156 to a hydrogen
separator 168, which may be a cryogenic separator, wherein hydrogen
or a hydrogen-rich gas is separated and withdrawn through a conduit
170 and passed to compressor 160 for delivery and recycling through
conduit 130 of the hydrogen-rich gas to the third gasification
stage portion 128 at a pressure greater than the pressure of the
third stage, and preferably approximately 1,100 psig.
As shown in FIG. 4, there are many possible modifications in the
ultimate use of the purified product gas transported in conduit
156. The purified product gas leaving the hydrogen separator 168 is
conducted through a conduit 172 to the methanation apparatus 164
where the purified product gas is catalytically methanated to yield
fuel gas containing at least 70 percent methane by volume and
preferably about 90 percent methane by volume.
Inordinate or undesirable temperature increase in the third stage
is prevented by steam entering the third stage portion 128 from the
elutriation portion 134 because the vaporized water in the steam
entering the third stage reacts endothermically with carbon to
produce carbon monoxide plus hydrogen gas.
The process of this invention, with certain modifications, can be
employed for the production of producer gas from the three stage
gasification of coal. In the production of producer gas, the
combination of oxygen and steam fed into the first gasification
stage is replaced by air as the gasification medium. The air should
be preheated to within a range of about 900.degree.F. to about
1,300.degree.F. or more. The air is introduced into the first
gasification stage for reaction with the recycle char therein.
Reaction pressures in the three separate stages are maintained
between approximately 5 and approximately 60 atmospheres. The rest
of the reaction conditions and process steps are as described
hereinabove. The producer gas obtained by this process using
preheated air as the first stage gasification medium is
particularly suitable as an industrial fuel or as a fuel for power
generation wherein emission of sulfur dioxide is not desirable.
The advantages to be gained with the use of the three stage
gasification process of this invention as compared to the use of
two-stage gasification process, can be illustrated by a comparison
of the following tabulated calculations of the composition of fuel
gases which may be obtained by each process and by calculation of
the possible coal and oxygen requirements for each process.
TABLE I ______________________________________ Present Process
Two-Stage 3 Stages Process ______________________________________
Analysis of gas from Gasifier, dry basis: % by volume CH.sub.4 28.2
20.5 H.sub.2 17.9 24.1 CO 27.5 34.4 CO.sub.2, H.sub.2 S 24.8 19.6
N.sub.2 1.6 1.4 For 1000 scf pipeline gas required: Coal, lb. 88.5
92.5 Oxygen, lb. 28.7 37.2
______________________________________
According to the provisions of the patent statutes, I have
explained the principle, preferred construction and mode of
operation of my invention and have illustrated and described what I
now consider to represent its best embodiments. However, it should
be understood that, within the scope of the appended claims, the
invention may be practiced otherwise than as specifically
illustrated and described.
* * * * *