U.S. patent number 3,775,071 [Application Number 05/164,381] was granted by the patent office on 1973-11-27 for method for feeding dry coal to superatmospheric pressure.
This patent grant is currently assigned to Hydrocarbon Research, Inc.. Invention is credited to Franklin D. Hoffert, Harold H. Stotler.
United States Patent |
3,775,071 |
Hoffert , et al. |
November 27, 1973 |
METHOD FOR FEEDING DRY COAL TO SUPERATMOSPHERIC PRESSURE
Abstract
A method for continuous feeding of dry coal particles from
essentially atmospheric pressure to the superatmospheric pressure
level of a coal gasifier or coal liquefaction reactor is achieved
by a series of screw feeding devices each partially boosting the
pressure level of the coal in stages to provide the dry coal at
reactor pressure.
Inventors: |
Hoffert; Franklin D.
(Mountainside, NJ), Stotler; Harold H. (Westfield, NJ) |
Assignee: |
Hydrocarbon Research, Inc. (New
York, NY)
|
Family
ID: |
22594230 |
Appl.
No.: |
05/164,381 |
Filed: |
July 20, 1971 |
Current U.S.
Class: |
48/210; 48/63;
48/202; 208/400; 252/373; 415/72; 48/73; 48/206; 208/407; 414/218;
417/247 |
Current CPC
Class: |
C10J
3/482 (20130101); B01J 3/02 (20130101); C10G
1/06 (20130101); C10J 3/30 (20130101); C10J
2300/1659 (20130101); C10J 2300/0966 (20130101); C10J
2300/1807 (20130101) |
Current International
Class: |
C10G
1/00 (20060101); C10G 1/06 (20060101); B01J
3/02 (20060101); C10J 3/02 (20060101); C10J
3/30 (20060101); C10g 001/06 (); C10j 003/16 ();
C10j 003/50 () |
Field of
Search: |
;48/63,64,73,76,77,78,99,101,197R,202,203,204,206,210 ;208/8,10
;214/17B ;415/72 ;417/247 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Scovronek; Joseph
Claims
We claim:
1. In a method of hydroconversion of coal wherein the coal in
particulate form and hydrogen are passed upwardly through a
reaction zone in a liquid phase environment under hydrogenation
conditions of temperature in the range of 750.degree.-900.degree.F
and hydrogen partial pressures in the range of 500 psi to 3000 psi
with the removal of liquid and gaseous effluent from the reaction
zone, the improvement which comprises:
a. drying and grinding the coal to a moisture content of not to
exceed five weight percent and a grind less than 1/4 inch;
b. mechanically boosting the pressure on said coal solids in stages
from atmospheric to reaction zone pressure by use of high speed
screw pumps;
c. introducing said pressurized, substantially dry coal particles
into the reaction zone independent of a carrier liquid; and
d. simultaneously measuring and controlling the weight flow of coal
particles into the reaction zone to provide a constant weight flow
of coal into the reaction zone.
2. In a method of gasification of coal wherein the coal in
particulate form and reactant gases are passed upwardly through a
reaction zone under conversion conditions of temperatures up to
1800.degree.F and pressure up to 1450 psig for the gasification of
the coal, the improvement which comprises:
a. drying and grinding the coal to a moisture content of not to
exceed five weight percent and a grind less than 1/4 inch;
b. mechanically boosting the pressure on said coal solids in stages
from atmospheric to reaction zone pressure by use of high speed
screw pumps;
c. introducing said pressurized, substantially dry coal particles
into the reaction zone in the absence of a carrier liquid; and
d. simultaneously measuring and controlling the weight flow of coal
particles into the reaction zone to provide a constant weight flow
of coal into the reaction zone.
Description
BACKGROUND OF THE INVENTION
In the gasification of coal to produce synthesis gas for the
manufacture of hydrogen or ammonia and to produce pipeline gas, the
coal is gasified at pressures ranging from 400 to 1200 psig. In the
hydrogenation of coal to produce liquid hydrocarbons the coal is
liquefied at pressures ranging from 500 to 3000 psig. The coal,
usually as pulverized particles, can be charged to these
superatmospheric pressure systems as dry particles by the
conventional lock hopper system. Here the coal is fed to a lock
hopper at essentially atmospheric pressure. The lock hopper is then
pressurized with a high pressure gas stream from the coal
conversion system. The coal which is now under a pressure higher
than the gasifier or hydrogenation system pressure is then
transferred through piping to the coal conversion system. The lock
hopper now empty of coal but filled with pressurized gas is then
depressured to essentially atmospheric pressure and the coal
charging cycle is repeated.
This method for feeding the dry coal has the disadvantage of a high
loss of pressured gas during the depressuring part of the charging
cycle and large lock hopper volumes are required for commercial
coal gasification and liquefaction plants due to intermittent
feeding from the lock hoppers.
Another method for feeding pulverized coal to a pressurized system
is by mixing the pulverized coal with a liquid such as water or oil
to produce a slurry which can then be pumped into the
superatmospheric pressure system. This method has the disadvantage
of low throughput for a given slurry pump and an expensive slurry
pump design to provide a pump in which erosion is minimized. It
also suffers the disadvantage that the liquid used to prepare the
slurry must be recovered, usually by vaporization and
recondensation, in the system so that it can be recycled back to be
used to charge additional coal to the system.
In this invention a method is provided for feeding dry pulverized
coal continuously to a system operating at superatmospheric
pressure whereby the lock hopper volume, and the loss of
pressurized gas are minimized and since the coal is fed dry no
recovery of slurrying liquid is required.
SUMMARY OF THE INVENTION
Dry pulverized coal is fed continuously to a coal gasifier or coal
hydrogenator operating at superatmospheric pressure by the use of a
series of screw pumps each operating against a differential
pressure and with intermediate pressure surge hoppers whose
pressures are maintained essentially constant with a small gas
bleed stream.
DESCRIPTION OF THE DRAWING
The drawing is a schematic flow diagram of equipment for feeding
coal to a coal conversion reactor.
DESCRIPTION OF PREFERRED EMBODIMENT
A coal such as bituminous, semibituminous, subbituminous or lignite
or a similar material such as shale, is initially elevated to the
inlet 10 of the atmospheric coal hopper 12 as by elevator, not
shown. Preferably, such coal has previously been surface dried and
ground to a desired mesh as hereinafter described.
The coal fines discharging into the atmospheric coal hopper 12 may
be purged of air if desired with inert gas at 14 and with purge gas
from the coal liquefaction system at 16.
The coal then enters the screw feeder 20 which is appropriately
driven by motor 22 and by which the coal can be boosted to 215 psig
and discharged into the low pressure coal hopper 24. Ultimately,
the coal then discharges into the next suitable screw feeder 26,
thereby increasing the pressure to 430 psig.
In turn, the coal discharges into the intermediate pressure coal
hopper (IPCH) 28 and in due course drops into the third screw
feeder 30. Thereby the pressure on the coal is thus raised to the
pressure in the high pressure hopper (HPCH) 32 of approximately 645
psig. From this high pressure coal hopper 32, the coal then
discharges into the screw feeder 36 again to be boosted in pressure
and discharging into the transfer line 40 at approximately 750-850
psig.
The transfer line 40 is fed with recycle gas from the coal
liquefaction system at 42 which transports the coal in a dense
phase condition into the coal reactor 45.
As described in U.S. Patents Nos., RE.25,770 and 3,519,555, which
relate to coal liquefaction, the environment within the reactor 45
is liquid phase as a result of the feed of hydrogen at 46 at such
temperature and pressure as will convert the coal to liquid
condition. Some supplemental liquid may be introduced at 48 if
desired. The reactor 45 can contain an ebullated bed of catalyst to
promote the rate of conversion.
The conditions in reactor 45 being such as to continuously convert
the solid coal to liquid and gas, the gas is removed at 50 and the
liquid and unconverted coal are removed through the down pipe
52.
The type of screw feeder shown in the drawing at 20, 26, 30 and 36
is a high speed screw pump which can pump the solids against a
pressure differential in the order of 215 pounds per square inch.
Hence, if the reaction chamber is at 750 psig, four stages are
adequate whereas if a higher pressure is desirable, additional
screw pumps can be used. Such pumps are commercially available from
Fuller Co. (Fuller-Kenyon pump) and from Robbins & Meyers
(Moyno pump).
A particular advantage of the screw pump is that there is a
continuous uniform increase in pressure with no substantial gas
loss or solids backflow. The operation is continuous which is
particularly beneficial in the hydrogenation of coal or the
gasification of coal.
To maintain appropriate pressures in the respective coal hoppers,
we have shown a gas circulating system wherein the gas from coal
hoppers 24, 28 and 32 pass through back pressure control valves 60
A, 60 B and 60 C respectively and into line 62 to scrubber 64 where
it is appropriately scrubbed with water. The gas then enters surge
drum 66 from which it can be recompressed by compresser 68 into the
line 70.
Under control of valve 72, appropriately pressurized gas will pass
through line 74 into the intermediate pressure coal hopper 28 and
under control of the valve 76 and line 78 into the low pressure
coal hopper 24. By line 80, it will pass into the high pressure
coal hopper 32. The solids levels in coal hoppers 24, 28 and 32 are
controlled by the speed of the screw feeding device. The speed of
screw feeder 36 is controlled by the flow of gas and solids to
reactor 45 in line 90 as by a flow controller.
As a result of such operation, there is a minimum loss of recycle
gas which may, of course, be recovered by suitable means from the
gas overhead line 50.
A comparison of the dry feed with a slurry feed for a 100,000 BPSD
refinery indicates a saving of capital investment of nearly 70%
($7.2 MM vs. $2.3 MM).
The operation cost for charging the coal shows an annual savings of
nearly 70 percent ($2.8 MM vs. $0.9 MM) which, based on gasoline
cost, would show a saving of about 0.14 cents/gallon gasoline.
Preferred operating conditions in the coal liquefaction reactor
would be in a pressure range of 500 to 3000 psi hydrogen partial
pressure, a temperature range in the order of
750.degree.-900.degree.F, a typical hydrogenation catalyst such as
cobalt molybdate on alumina, the coal being predried to a moisture
content not to exceed five weight percent, and with a coal size of
less than one-fourth inch.
Preferred operating conditions for a coal gasifier, such as
disclosed in U.S. Pat. No. 2,634,198 and No. 3,226,204, are as
follows:
Temperature;1100.degree.-1800.degree.F;
Pressure; atmosphere -1450 psig, usually above 450 psig.
While we have shown and described a preferred form of embodiment of
our invention, we are aware that modifications may be made within
the scope and spirit thereof.
* * * * *