U.S. patent application number 12/603069 was filed with the patent office on 2010-02-18 for method for thermally upgrading carbonaceous materials.
This patent application is currently assigned to Evergreen Energy Inc.. Invention is credited to Robert F. Hogsett, Philippus J. Meyer, Michael F. Ray, Michael L. Schlegel, Sheldon L. Schultz.
Application Number | 20100037516 12/603069 |
Document ID | / |
Family ID | 35185610 |
Filed Date | 2010-02-18 |
United States Patent
Application |
20100037516 |
Kind Code |
A1 |
Hogsett; Robert F. ; et
al. |
February 18, 2010 |
METHOD FOR THERMALLY UPGRADING CARBONACEOUS MATERIALS
Abstract
Carbonaceous materials are thermally upgraded in a pressurized
steam environment to remove moisture and other byproducts. A
variety of water/solid separation devices may be employed in a
process vessel to maximize moisture removal from the upgraded
charge. Heating media inlet nozzles and process chamber vents are
strategically positioned at the process vessel wall to minimize
short circuiting of heating media to vessel outlet vents and to
continuously separate hot water removed from the charge and
condensed steam, such that the upgraded material removed from the
process vessel is not discharged with accompanying free moisture.
After upgrading, the charge may be rehydrated to improve its
stability during shipping and storage.
Inventors: |
Hogsett; Robert F.;
(Lakewood, CO) ; Meyer; Philippus J.; (Secunda,
ZA) ; Ray; Michael F.; (Canyon Lake, TX) ;
Schlegel; Michael L.; (Story, WY) ; Schultz; Sheldon
L.; (Boise, ID) |
Correspondence
Address: |
HARNESS, DICKEY & PIERCE, P.L.C.
P.O. BOX 828
BLOOMFIELD HILLS
MI
48303
US
|
Assignee: |
Evergreen Energy Inc.
Denver
CO
|
Family ID: |
35185610 |
Appl. No.: |
12/603069 |
Filed: |
October 21, 2009 |
Related U.S. Patent Documents
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Application
Number |
Filing Date |
Patent Number |
|
|
11486349 |
Jul 13, 2006 |
|
|
|
12603069 |
|
|
|
|
10837998 |
May 3, 2004 |
7198655 |
|
|
11486349 |
|
|
|
|
Current U.S.
Class: |
44/626 |
Current CPC
Class: |
B01J 8/0065 20130101;
B01J 2208/00132 20130101; C10L 9/06 20130101; F28D 7/00 20130101;
B01J 2219/00038 20130101; F28C 3/14 20130101; B01J 2219/0004
20130101; C10L 9/08 20130101 |
Class at
Publication: |
44/626 |
International
Class: |
C10L 5/00 20060101
C10L005/00 |
Claims
1. A method for upgrading energy content of a charge of
carbonaceous material having a first equilibrium moisture level
comprising: directly contacting the charge with a heating medium
under pressure to heat the charge to drive moisture from the charge
to a second moisture level below the first equilibrium moisture
level and to lower an equilibrium moisture level of the charge to a
value between the first equilibrium moisture level and the second
moisture level; and separating driven moisture from the charge.
2. The method of claim 1 further comprising heating at least a
portion of the charge via indirect heat exchange.
3. The method of claim 1 further comprising: sizing the charge
prior to direct contact with the heating medium within preselected
upper and lower size limits.
4. The method of claim 3 wherein sizes of charge material are
distributed within the upper and lower size limits following a
Rosin-Rammler index for the charge material.
5. The method of claim 1 wherein the carbonaceous material
comprises coal.
6. Carbonaceous material upgraded by the method of claim 1.
7. The method of claim 1 further comprising venting non-condensable
gas while heating the charge so as to maintain uniform temperature
conditions throughout the charge.
8. The method of claim 7 wherein the venting is performed
continuously while heating the charge.
9. The method of claim 7 wherein the venting is performed
periodically while heating the charge.
10. The method of claim 1 further comprising: rehydrating the
charge to a third moisture level higher than the second moisture
level but less than the first equilibrium moisture level of the
charge.
11. The method of claim 1 wherein the heating medium comprises
saturated steam.
12. The method of claim 11 wherein the charge is heated to between
a minimum temperature where structure of charge particles become
elastic and a maximum temperature where pyrolysis occurs.
13. The method of claim 12 wherein the minimum temperature is about
400.degree. F. and the maximum temperature is about 500.degree.
F.
14. The method of claim 13 wherein the charge is heated under
pressures of between about 247 psia and about 680 psia.
15. The method of claim 1 wherein the heating medium comprises
superheated steam.
16. The method of claim 11 wherein a portion of the heating medium
comprises compressed hot water condensed from the saturated
steam.
17. The method of claim 15 wherein a portion of the heating medium
comprises compressed hot water condensed from the superheated
steam.
18. The method of claim 1 wherein the charge is directly contacted
with the heating medium under pressure for a time period of about 5
minutes to about 1000 minutes.
19. The method of claim 1 wherein the charge is directly contacted
with the heating medium under pressure for a time period of about
15 minutes to about 60 minutes.
20. The method of claim 1 wherein the charge is directly contacted
with the heating medium under pressure for a time period of about
20 minutes to about 30 minutes.
21. The method of claim 1 wherein the second moisture level is
between about 20% and about 60% of the first equilibrium moisture
level.
22. The method of claim 10 wherein the third moisture level is
between about 101% and about 125% of the second moisture level.
23. The method of claim 10 wherein the third moisture level is
between about 110% and about 120% of the second moisture level.
24. The method of claim 10 wherein rehydrating is carried out in a
moisturizing chamber.
25. The method of claim 10 wherein rehydrating is carried out by
spraying the upgraded charge with water via at least one spray
nozzle.
26. The method of claim 10 wherein rehydrating is carried out by
blending an upgraded charge with non-upgraded carbonaceous
material.
27. A method for upgrading energy content of a charge of
carbonaceous material having a first equilibrium moisture level
comprising: directly contacting the charge with a heating medium
under pressure to heat the charge to drive moisture from the charge
to a second moisture level below the first equilibrium moisture
level and to lower an equilibrium moisture level of the charge to a
value between the first equilibrium moisture level and the second
equilibrium moisture level; separating driven moisture from the
charge; and adding a reactive gas to the heating medium in an
amount sufficient to cause mercury level in the charge to decrease.
Description
RELATED APPLICATIONS
[0001] This is a division of commonly assigned U.S. patent
application Ser. No. 11/486,349, filed Jul. 13, 2006, which is a
continuation of commonly assigned U.S. patent application Ser. No.
10/837,998 filed May 3, 2004, now U.S. Pat. No. 7,198,655 issued
Apr. 3, 2007.
BACKGROUND OF THE INVENTION
[0002] The invention generally relates to thermal upgrading of
carbonaceous materials, such as sub-bituminous rank and lignite
rank coals, peat and various forms of bio-mass fuels. More
particularly, the invention concerns thermal upgrading of
carbonaceous materials by direct contact with a heating medium and
by removing moisture from the charge as hot water.
[0003] U.S. Pat. No. 5,071,447 to Koppelman discloses methods and
apparatus for steam treating carbonaceous materials. Under the
system disclosed in the '447 patent, steam is injected at the top
of a processing vessel.
[0004] U.S. Pat. No. 5,769,908 to Koppelman relates to the
treatment of carbonaceous materials by injecting an inert gas into
the carbonaceous material under a vacuum or injecting steam into
the carbonaceous material either with or without the vacuum being
applied in a controlled manner to more consistently treat the
charge of carbonaceous material.
[0005] While the prior teachings in the two above cited Koppelman
patents are believed to have been advances in the art addressing
many problems in the area of thermal upgrading of materials, such
as coal, there remains a need in the art to more consistently
insure that all surfaces of the charge of carbonaceous material
reach the same final temperature, to minimize free moisture
accompanying the upgraded charge, and to accomplish improved
removal of unwanted byproducts from the charge.
SUMMARY OF THE INVENTION
[0006] Accordingly, a method for upgrading energy content of a
charge of carbonaceous material having a first equilibrium moisture
level begins with directly contacting the charge with a heating
medium under pressure to heat the charge to drive moisture from the
charge to a second moisture level below the first equilibrium
moisture level and to lower an equilibrium moisture level of the
charge to a value between the first equilibrium moisture level and
the second moisture level. Moisture driven from the charge is
separated therefrom.
[0007] In another aspect of the invention, a method for upgrading
energy content of a charge of carbonaceous material having a first
equilibrium moisture level begins with directly contacting the
charge with a heating medium under pressure to heat the charge to
drive moisture from the charge to a second moisture level below the
first equilibrium moisture level and to lower an equilibrium
moisture level of the charge to a value between the first
equilibrium moisture level and the second moisture level,
separating driven moisture from the charge, and adding a reactive
gas to the heating medium in an amount sufficient to cause mercury
level in the charge to decrease.
BRIEF DESCRIPTION OF THE DRAWINGS
[0008] The objects and features of the invention will become
apparent from a reading of a detailed description, taken in
conjunction with the drawings, in which:
[0009] FIG. 1 is a side elevation view showing the vertical
orientation of a feed lock hopper on top of the main process vessel
with a product discharge lock hopper under the process vessel, in
accordance with the principles of the present invention;
[0010] FIG. 2 is a side elevation view showing two feed lock
hoppers and two product discharge lock hoppers in combination with
the process vessel for providing continuous charge processing in
accordance with the principles of the invention;
[0011] FIG. 3 is a partial cross-sectional view of the process
vessel of FIG. 1 showing inlet and outlet nozzle arrangements in
accordance with the principles of the invention;
[0012] FIG. 4A is a cross-sectional view of the process vessel of
FIG. 1 showing inlet and outlet nozzle details in addition to
solid/water separation devices arranged in accordance with the
principles of the invention;
[0013] FIG. 4B is an enlarged view of perforated regions of the
separation surfaces of the devices of FIG. 4A;
[0014] FIGS. 4C, D and E are top plan views of the vessel of FIG.
4A taken respectively at locations A-A, B-B and C-C of FIG. 4A;
and
[0015] FIG. 5 is a schematic showing the orientation and placement
of typical rehydration equipment and associated input, internal and
output flow streams, arranged in accordance with the principles of
the invention.
DETAILED DESCRIPTION
[0016] Referring to FIG. 1, processing system 100 includes a feed
lock hopper 102 positioned at a top portion 104 of a process vessel
106, with a discharge lock hopper 108 positioned below a bottom
portion 110 of process vessel 106. At an input of each lock hopper
102 and 108 are valves 112 and 116, respectively, which seal their
respective lock hopper from atmospheric pressure up to an operating
pressure of process vessel 106. Likewise, there are output valves
114 and 118 at an output of respective lock hoppers 102, 108 which
serve the same purpose.
[0017] Carbonaceous charge material in conduit 150 is
intermittently fed into feed lock hopper 102 via valve 112 being in
an open position and bottom valve 114 in a closed position. Input
valve 112 is then closed, and lock hopper 102 is brought up to the
same operating pressure as in process vessel 106. Valve 114 is then
opened, and the charge material flows by gravity into the process
vessel 106. When feed lock hopper 102 is empty, output valve 114 is
closed, and the pressure in lock hopper 102 is lowered to
atmospheric conditions. Input valve 112 is then opened, and the
feed lock hopper 102 is ready to start another feed cycle via
conduit 150. The hourly feed rate of carbonaceous material, on an
average basis, is determined by the weight of material fed each
cycle and the number of cycles per hour, and the feed flow into the
process vessel 106 is thus intermittent.
[0018] With continued reference to FIG. 1, in a manner similar to
operation of feed lock hopper 102, discharge lock hopper 108
intermittently removes upgraded charge material from process vessel
106 via conduit 152. The simplified sequence of the cyclic
operational steps would be that the empty discharge lock hopper 108
has just discharged upgraded material to atmospheric conditions and
to further processing equipment via conduit 152. Output valve 118
is then closed, the pressure is equalized to that of process vessel
106, and output valve 116 is opened. After discharge lock hopper
108 is full, input valve 116 is closed and the pressure in the lock
hopper 108 is lowered to atmospheric conditions. Outlet valve 118
is then opened, and output lock hopper 108 intermittently
discharges upgraded charge material via conduit 152 to complete the
cycle. The lowering of pressure in lock hopper 108 also serves to
lower the temperature through evaporation of water from inner
portions of the carbonaceous charge.
[0019] Process vessel 106 could be operated in a batch mode without
using feed or discharge lock hoppers 102 or 108. An input valve 114
and an output valve 116 would be required, and then the sequence of
operation would be the same as for one of the lock hoppers
previously described--i.e., with the output valve 116 closed and
process vessel at atmospheric pressure, feed material flows into
process vessel 106 via open input valve 114. Valve 114 is then
closed after the process vessel 106 is full, process vessel 106 is
brought to operating pressure and temperature and, after a desired
processing time, process vessel 106 pressure is lowered to
atmospheric, output valve 116 is opened and the upgraded charge is
discharged. After process vessel is empty, output valve 116 is
closed and the batch cycle starts again. Using multiple batch
process vessels, and with the proper sequencing of cycles on each
vessel, it is possible to operate batch vessels in a manner that
overall feed and discharge to and from the multiple vessels
approaches continuous operation.
[0020] Using two feed lock hoppers and two discharge lock hoppers,
it is possible to achieve true continuous feed and discharge into
and out of process vessel 106. FIG. 2 shows an equipment
arrangement that would allow such a continuous process. Feed charge
material is fed from inlet duct 252 through a diverter valve 202
which directs the feed flow to either of the feed lock hoppers 204
or 206. For continuous feed, one of these lock hoppers is full and
ready to feed process vessel 106 before the other hopper is empty.
At the discharge end of the vessel, one of the discharge lock
hoppers 208, 210 is empty and ready to receive upgraded material
before the other discharge lock hopper is full. With this operation
the feed into process vessel 106 is continuous, and the discharge
out of process vessel 106 is continuous. Hence, process vessel 106
operates in a completely continuous mode. However, because of the
requirement that one of the feed lock hoppers is full and waiting
to feed and one of the discharge lock hoppers is empty and waiting
to receive discharge, the feed into the feed lock hoppers and the
discharge out of the discharge lock hoppers will not be continuous,
but will approach continuous operation.
[0021] With continued reference to FIG. 2 the sequence for
continuous operation of process vessel 106 is as follows. Feed lock
hopper 204 will be feeding process vessel 106 with input valve 212
in the closed position and output valve 214 in the open position.
The other feed lock hopper 206 will be sitting full of feed and
will be at process vessel pressure. Additionally, both input valve
216 and output valve 218 will be closed. As soon as feed lock
hopper 204 is empty, output valve 214 closes and simultaneously
output valve 218 on feed lock hopper 206 opens and feeds into the
process vessel 106 in a continuous and uninterrupted manner. The
pressure in feed lock hopper 204 is then lowered to atmospheric,
input valve 212 is opened, diverter valve 202 is positioned to feed
the charge material into feed lock hopper 204, and the feed
continues until feed lock hopper 204 is full. The flow of feed
charge material is stopped, input valve 212 on feed lock hopper 204
is closed, the pressure in feed lock hopper 204 is equalized to
process vessel 106 pressure, and the feed lock hopper 204 then sits
and waits for feed lock hopper 206 to empty. The cycle is then
ready to repeat.
[0022] Still referring to FIG. 2, the sequence for operation of
discharge lock hoppers 208 and 210 is the same as for feed lock
hoppers 204 and 206 described above, except that one of the
discharge lock hoppers 208 (or 210) has to be sitting empty at
process vessel pressure with input valve 220 open and bottom valve
222 closed, while the other discharge lock hopper 210 (or 208) is
filling. When discharge lock hopper 210 is full, diverter valve 224
directs process vessel discharge into discharge lock hopper 208.
Input valve 226 on discharge lock hopper 210 is closed, the
pressure in the discharge lock hopper 210 is lowered to
atmospheric, the output valve 228 on discharge lock hopper 210 is
opened, and upgraded charge is discharged to any necessary
collection and conveying equipment via outlet duct 250. When empty,
output valve 228 on discharge lock hopper 210 is closed, pressure
inside the discharge lock hopper 210 is equalized with that of the
process vessel 106, and input valve 226 is then opened. Discharge
lock hopper 210 then sits empty and pressurized until companion
discharge lock hopper 208 is full. The cycle then repeats.
[0023] FIG. 3 shows more detail for a single feed lock hopper
operation in a semi-continuous system. Input and output valves 112
and 114 operate on feed lock hopper 102 as described above. A
pressurization inlet 302 and depressurization outlet 304 are used
to control the pressure in feed lock hopper 102. After feed lock
hopper 102 has emptied its charge into process vessel 106, input
valve 112 is still closed, output valve 114 is still closed, but
feed lock hopper 102 is still at process vessel pressure and
contains a saturated steam environment. A valve on the
depressurization outlet 304 is opened, and the saturated steam
vapor flows out of the feed lock hopper 102 until atmospheric
pressure is achieved and the valve on the depressurization outlet
304 is closed. Input valve 112 on feed lock hopper 102 is then
opened, and the lock hopper is filled with charge material. When
full, input valve 112 is closed, and a valve on pressurization
inlet 302 is opened. A suitable pressurization medium, such as
saturated steam, super heated steam, air or another gas is used to
raised the internal pressure to match that of process vessel 106,
and the valve on pressurization inlet 302 is closed. Output valve
114 on feed lock hopper 102 is then opened, and material is fed
into the process vessel 106.
[0024] Non-condensable gases are continuously vented from process
vessel 106 using vents 306, 308 and 310 shown in FIG. 3.
Non-condensable gas arises from volatile organics released from the
carbonaceous charge material during upgrading, from air that enters
the upgrading process absorbed in the feed charge material, and
from any other gas introduced into the upgrading process.
Non-condensable gas is normally present at minor concentrations in
process vessel 106, with a majority volume constituent being
saturated steam vapor. Thus, when non-condensable gases are vented,
there is an accompanying steam flow that represents considerable
energy loss from the upgrading process. Some of this energy can be
recovered and reused by using all, or a portion, of process vessel
vent flows as the pressurization gas for both feed lock hopper 102
and discharge lock hopper 108 operation. The pressurization outlets
304 and 312 on feed and discharge lock hoppers 102 and 108,
respectively, vent gas that could be essentially almost pure
saturated steam from the process. This also comprises energy loss.
Using vent flows from process vessel 106 for lock hopper
pressurization does not result in any additional energy loss from
the upgrading process when vented a second time from lock hopper
depressurization outlets 304 and 312.
[0025] With continued reference to FIG. 3, the heating medium is
normally introduced into process vessel 106 through inlets 314 and
316 located on one side of process vessel 106, while process vessel
vents 306, 308 and 310 are on an opposite side of the vessel 106.
Both the inlets and vents can be at multiple elevational positions
on the vessel and may involve many more locations than shown in
FIG. 3. The vents are normally protected by associated diverter
shields 318a, b, c which prohibit water and solids from escaping in
the vent streams, but allow non-condensable gas and steam vapor to
escape. One requirement of the inlet and vent placement is to
prevent short circuiting of inlet flows directly to the vents.
Another requirement of the inlet and vent placement is to create
flow patterns across an interior volume of process vessel 106 in a
substantially horizontal direction, a down-flowing direction, or an
up-flowing direction to effectively control and remove
non-condensable gases from process vessel 106. For instance, heavy
non-condensable gases, such as carbon monoxide, will tend to
migrate to the bottom interior portion 320 of process vessel 106,
and they would not effectively be removed if all of the inlet and
vent flow was at the top interior portion 322 of process vessel
106. In such a case, inlet and vent flows would be controlled to
sweep the heavier non-condensable gas out of a lower vent location.
In an opposite case, light non-condensable gas such as hydrogen
will migrate to the top portion 322 of process vessel 106, and
appropriate flow patterns between the inlet and vent locations need
to be established to control concentration of light non-condensable
gas in a top portion 322 of process vessel 106. In some instances,
controlling both concentrations of heavy and light non-condensable
gases is effectively implemented with substantially horizontal flow
patterns between process vessel 106 inlets and vent locations.
[0026] In normal operation, the heating medium flow into process
vessel 106 is controlled by pressure in process vessel 106. If the
pressure drops below a desired operating set point, heating media
inlet 314 flow will increase to compensate. Conversely, if the
pressure rises above the desired operating set point, inlet flow
will decrease. Vent flow out of process vessel 106 is normally
controlled by measuring non-condensable gas concentration in
process vessel 106 and then adjusting an appropriate control valve
to achieve the desired mass flow of non-condensable gas (and
accompanying water vapor) out of process vessel 106 at each desired
vent location. Vent flow out of process vessel 106 can be a
significant variable in terms of impacting heating medium inlet
flow. Most of the heating medium inlet flow will be to provide
sensible heat to heat the feed charge to operating conditions,
provide energy for heat losses from the process, and provide energy
for heat of reaction requirements that occur in the thermal
upgrading process.
[0027] The preferred heating medium is either saturated steam or
super heated steam introduced to the process vessel 106 through the
upper and lower heating medium inlets 314 and 316, respectively, or
through any other inlets located on an exterior wall of vessel 106.
Likewise, the heating medium could be directed through internal
piping into interior 322 of vessel 106 and used to provide energy
to selected locations.
[0028] Compressed hot water may also be used as part of the heating
media. For instance, when relatively cold incoming charge material
is fed into the top of process vessel 106 through feed lock hopper
102, saturated steam will immediately start to condense and
transfer energy into the cold charge thermodynamically by latent
heat of condensation. The hot condensate, or compressed hot water,
at this location or other locations within process vessel 106, will
be hotter than the charge material and will also transfer heat into
the charge material. If a suitable source of compressed hot water
is available external to process vessel 106 at thermodynamic
conditions capable of supplying heat into the thermal upgrading
process, such compressed hot water could be introduced at multiple
locations and used as the entire energy supply to the process.
Alternatively, compressed hot water could be used as a partial
supplement to saturated or super heated steam heating media. One
benefit that comes from using saturated steam, or super heated
steam after it has been de-super heated, is that saturated steam
condenses isothermally, which means that steam will flow on its own
to any location within process vessel 106 that is colder than the
temperature of the saturated steam, provided that the porosity of
the bed of charge material is sufficient to allow passage of the
steam vapor to the cooler areas of the bed. Until it is de-super
heated, super heated steam flow must be directed to its point of
use.
[0029] It may be particularly advantageous to supply super heated
steam to the thermal upgrading process through heating medium inlet
316 located near the bottom of process vessel 106 to serve at least
two specific purposes. One would be to initially provide thermal
energy to the charge material in a "dry" form through loss of heat
from the super heated vapor or hot gas. This could be used to
remove excess free surface moisture from the charge material and
provide additional dewatering by converting free moisture to
saturated steam. The use of "dry" super heated steam near the
bottom of the process vessel would also provide a "dry" environment
around the charge material and provide a differential in partial
pressure between inherent moisture still contained in the charge
material and the relatively dry vapor space at an outer surface of
the charge material solid particles that would provide a thermal
dynamic driving force for liberation of additional inherent
moisture within the charge.
[0030] Pressurization of discharge lock hopper 108 through
pressurization inlet 324, and depressurization through
depressurization outlet 312 will be achieved and controlled in
exactly the same manner as described above for feed lock hopper
102. As previously described, vent gas from vents 306, 308 and 310
may be used as the pressurization gas for discharge lock hopper
108.
[0031] During upgrading of the charge, the processing vessel uses
temperatures ranging from a minimum temperature where the structure
of the charge's particles become elastic and a maximum temperature
where any substantial pyrolysis occurs. Preferably, the range is
400.degree. F. to 500.degree. F. with corresponding pressures of
247 psia to 680 psia, or pressures that substantially match the
temperature at saturated steam conditions. Due to the presence of
some amount of non-condensable gases that may be present in the
vessel environment, the actual temperature at any given total
process vessel pressure may be somewhat less than predicted by
saturated steam conditions. For example, if total process vessel
pressure is 500 psia and the concentration of non-condensable gases
is 10% by volume, the partial pressure of the non-condensable gas
will be 50 psia and the partial pressure of the saturated steam
will be 450 psia. Hence the temperature of both the non-condensable
gas and the saturated steam will be about 456.degree. F. compared
to a temperature of about 467.degree. F. if only saturated steam
were present.
[0032] In order for steam vapor to flow uniformly to colder regions
of the process vessel bed for isothermally condensing and to also
promote better draining and separation of moisture from the
upgraded charge, it is desirable to use a properly sized
carbonaceous feed material so that porosity is maintained in the
bed. This is achieved by crushing and screening oversize material
so that a maximum size of feed material is obtained. Likewise, some
fines need to be removed from the feed material so that the fines
do not pack into the void spaces between the larger particles and
create regions of low bed porosity within the process vessel. It is
recognized that because of mass to volume relationships, a given
weight of fine material will have a much larger surface area than
an equivalent weight of coarser material. Increasing the surface
area of the charge material, also increases the area for free
surface moisture to accumulate and makes dewatering of the upgraded
charge more difficult. Particle size distributions for the feed
material can range from 0.00 inch by minus 4 inch as an extreme,
with plus 0.125 inch by minus 3 inch being more desirable, and with
plus 0.25 inch by minus 2 inch being most desirable. In order for
these size ranges to be effective, the feed charge material should
be sized so that the distribution of sizes within the upper and
lower size limits should closely follow the Rosin-Rammler index
typically characteristic for the type of charge being upgraded.
[0033] Once in process vessel 106, the carbonaceous charge is
heated to operating temperature and pressure. The average retention
time of the charge in the process vessel 106 is determined by the
volume of the process vessel 106, the bulk density of the charge
material and the weight of the material fed. Retention times
between about 5 minutes and about 1000 minutes are believed useful,
with retention for about 15-60 minutes more preferable and about
20-30 minutes most preferable.
[0034] In a similar manner, the presence of super-heated steam can
increase the temperature in the process vessel above that predicted
by saturated steam conditions. Using the above example, if
super-heated steam were present in the vessel with about 11.degree.
F. of super heat in the vapor, then the steam partial pressure
would still be 450 psia, but the temperature of both the steam and
the non-condensable gas would increase to 467.degree. F., or the
temperature of pure saturated steam at 500 psia.
[0035] Within the temperature and pressure ranges on a weight basis
stated above, much more energy can be released from saturated steam
when it condenses compared to energy released when super-heated
steam cools down to saturated conditions or when compressed water
left after condensation cools down and transfers heat. Hence, the
use of saturated steam and the heat released when it isothermally
condenses is the preferred approach of supplying heat to the
process vessel.
[0036] As the charge reaches a desired temperature in the process
vessel, the charge becomes more elastic allowing for the release of
water with a minimum amount of charge particle fracturing.
[0037] Moisture present in the charge material is removed in
accordance with the invention by several mechanisms.
[0038] The first mechanism for moisture removal is volumetric
expansion of entrained water as the charge is heated up by the
surrounding environment. The water thermally expands at a rate
faster than the charge pore structure surrounding the water, and
the water has no place to go except to exit the charge.
[0039] A second mechanism squeezes additional water out of the
charge pores as the pores collapse in volume. The pores collapse in
volume due to water being removed and due to the external pressure
applied on the surface of the charge from the processing
environment.
[0040] A third mechanism involves differential pressure between
moisture and vapor form trapped in the charge which escapes to a
region of lower pressure in the process vessel vapor phase.
[0041] A fourth, less desirable mechanism is removal of ionic and
charge bonded water which is accomplished through thermal dynamic
equilibrium shifts as the processing temperature increases. Removal
of water from the charge via this mechanism is preferably minimized
by limiting the maximum temperature in the processing environment.
If only water were removed by the equilibrium shift, this would be
acceptable. However, at the elevated temperatures, volatile
organics contained in the carbonaceous charge are also released. As
the processing temperature goes up, the amount of volatiles
released starts to go up at an increased rate. The volatiles
released from the charge either combine with the water in a soluble
or entrained form or mix with the steam vapor as non-condensable
gases. Neither process is desirable, as organics mixed into or
soluble in the water add to the cost of water treatment prior to
reuse and/or disposal of the water and increase the concentration
of non-condensable gas in the process vessel vapor phase.
[0042] Indirect heating can also be utilized with the invention. As
an example, heat exchange tubes 350 (FIG. 3) could optionally be
placed anywhere in the process vessel where there would be contact
between the charge material and the indirect heating surface of
tube 350. As long as the indirect surface is at a higher
temperature than the charge, there will be heat transferred into
the charge. This may be particularly advantageous at a bottom of
the process vessel as shown in FIG. 3 where an indirect heat
surface serves to evaporate excess surface moisture from the charge
prior to discharge. A source of indirect heating medium (not shown)
would be coupled to element(s) 350 via ports 352 and 354.
[0043] High moisture content carbonaceous materials, such as
sub-bituminous coal, contain up to 30% by weight inherent or
entrained moisture. As mined, the inherent moisture content is very
close to the equilibrium moisture content of the material, which is
generally defined as that moisture level to which the coal will
re-equilibrate if exposed to a new environment and then re-exposed
to its original environment, unless the material has been either
structurally and/or chemically altered when exposed to the new
environment. As an example, coal mined from the seam at 30%
moisture and allowed to air dry in a low humidity environment to,
for example, 20% inherent moisture, will still have an equilibrium
moisture value of about 30% and will eventually return or
re-equilibrate to about 30% inherent moisture if exposed to a high
humidity environment over time.
[0044] Most normal upgrading processes attempt to lower the
inherent moisture level of the charge to a level much below the
equilibrium moisture level reached during such processing. When
shipped and stored, such material will attempt to equilibrate to
its equilibrium moisture level by absorbing moisture from the
environment. If this absorption occurs too rapidly, the charge may
overheat and even undergo spontaneous combustion in storage or in
transit.
[0045] It is believed that careful control of the processing
conditions relative to the charge material that is to be upgraded
in accordance with this invention will result in production of a
thermally upgraded product that is stable and safe to ship as
produced. However, with sub-bituminous charge material containing
20 to 30% inherent moisture, the resultant upgraded product in
accordance with this invention will have an equilibrium moisture
level between about 8 and about 16% by weight. Based on experience,
coal with an inherent moisture level of about 7% cannot be safely
shipped and stored as is, if the equilibrium moisture level is much
higher, for example at 15%. Depending on the charge, if it is
rehydrated back up to 10 to 14% inherent moisture it can be safely
shipped and stored. Rehydration may be achieved in a controlled
environment where moisture originally removed from the coal is
added back to the coal or high moisture, non-upgraded or partially
upgraded coal is blended with the low moisture upgraded charge.
[0046] Injection of air or other gas containing reactive oxygen
into the process vessel is desirable for a number of reasons, each
making use of desirable, highly exothermic reactions between oxygen
and some form of fuel in the charge or process vessel. With oxygen
injection, at least a portion of organic based volatiles expelled
from the upgraded charge may be oxidized. Excess surface moisture
can be burned off. Additionally, it is believed that unwanted
byproducts such as mercury, can be more easily separated from the
charge when subjected to oxidation reactions. Finally, selective
oxidation of portions of an upgraded charge may render it more
stable in storage.
[0047] One undesirable oxidation reaction is formation of excessive
amounts of non-condensable gas that may have to be vented from the
process vessel as discussed previously to control the impact of
non-condensable gas on saturated steam temperature. Heat generated
in any oxidation reaction approximately balances out energy loss
due to venting the non-condensables and accompanying steam vapor.
Conversely, if more non-condensable gas is desired in the process
vessel, then air would be the preferred source of oxygen for the
oxidation reaction, because of the high nitrogen (a non-condensable
gas) content of the air and the fact that any oxidation reactions
involving oxygen in the air form a non-condensable combustion
product.
[0048] The purpose of adding air or other gas containing reactive
oxygen is believed fulfilled when about 0.00005 pounds of reactive
oxygen per pound of upgraded charge (dry basis) to about 0.05
pounds of reactive oxygen per pound of upgraded charge (dry basis)
is added. About 0.00001 to about 0.025 pounds of added reactive
oxygen per pound of upgraded charge (dry basis) is more preferable,
with about 0.005-0.01 pounds of added reactive oxygen per pound of
upgraded charge (dry basis) being most preferable.
[0049] FIG. 4A shows details of how the charge material within
process vessel 106 is separated from water expelled therefrom. Both
moisture eliminated from the charge material and steam condensate
from the heating medium have to be continuously removed from vessel
106 as hot process water. This can be a difficult task, since both
the charge material and the hot water tend to flow downwardly
through the process vessel 106 due to gravity. Additionally, it is
necessary to separate the two flows of the charge and the moisture,
such that essentially dry upgraded charge material is removed from
process vessel 106 in one stream, and hot water is removed in
another totally separate stream or streams.
[0050] There are at least five different equipment arrangements
usable for separating hot water from the charge material moving
downwardly through process vessel 106. Examples are 1) outward
sloping separation cone 402, 2) vertical perforated drainage tubes
404a, b, c, located in an interior volume of process vessel 106, 3)
vertical perforated drainage tube 406 located on a wall of vessel
106, 4) inward sloping separation cone 408, and 5) at least one
rotatable horizontal separation table 410.
[0051] These various separation units can be used in a variety of
combinations with multiple placements within vessel 106 to effect
the desired degree of water/solid separation. Furthermore, although
the view of openings in the separation surface areas shows round
holes 450 in FIG. 4B, these openings in the various separation
areas alternatively could comprise slots, square openings, screens,
grates, baskets, perforated tubes or any other device enabling hot
water to pass through openings in the separation device while
blocking flow of the solid charge. The size of the openings is
selected to ensure good drainage while minimizing escape of fine
solid materials. In addition, it is preferable to taper each
opening so that the opening on the water collection side is
slightly larger than the opening on the charge side. In this
manner, solid particles which may become lodged in the openings
have a better chance of being dislodged and passing through the
opening.
[0052] Outward sloping separation cone 402 allows hot water to pass
substantially downwardly through separation openings in the surface
of cone 402, while the solid charge material is directed radially
outwardly toward the wall of process vessel 106. Hot water passing
through the openings in cone 402 is collected in a collection pan
412, or a header serving a similar function, and hot water exits
process vessel 106 via an internal drain 414 which is coupled to
hot water discharge 416.
[0053] As solid charge material is directed radially outwards, the
material flow can pass around and past internal drainage tubes such
as 404a, b, c which allow hot water to separate from the solid
charge through perforated holes in each tube. View A-A in FIG. 4D
is a plan view looking down the interior volume of the process
vessel 106 and shows that the internal drainage tubes 404 can be
arranged in concentric circles which would provide multiple
opportunities for hot water to be separated from the solid charge.
Collection headers at a bottom of each tube collects the hot water
and directs it to an internal drain 420 which then allows hot water
to discharge from process vessel 106 through one or more hot water
outlets 422.
[0054] Also shown in view A-A of FIG. 4D is an arrangement where
the internal perforated tube 406 could be split in half and
attached to a wall of process vessel 106 in a circular array in
water tight manner such that hot water can be removed from the
charge material immediately adjacent the vessel wall. Hot water
collected in the tubes would be collected in a header at the bottom
and passed out of the process vessel 106 as hot water to discharge
418. A portion or all of the perforated tube array could be
replaced by a concentric wall with separation openings secured to
process vessel 106's wall at the top in a water tight manner and
with a collection header at the bottom to collect and pass the hot
water to discharge through at least outlets 418 and 422.
[0055] Part of the function of outwardly sloping separation cone
402 is to direct solid flow radially outward. Part of the function
of the inwardly sloping separation cone 408 is to direct solid flow
radially inwardly, while providing an opportunity for hot water to
separate from the solid charge material by flowing downwardly
through openings in separation cone 408. View B-B of FIG. 4C looks
downward on the inward sloping separation cone 408 in plan view and
shows that the cone is concentric and attached to an outer wall of
process vessel 106. The cone extends in an arc through the entire
circumference of process vessel 106. Cone 408 could also be
installed in segments and be discontinuous. Hot water passing
through cone 408 openings 409 is collected in a concentric annular
collection pan 424 which passes the hot water discharge through at
least one or more outlets in process vessel 106. Two outlets, 426a
and 426b, are shown in FIG. 4A as an example.
[0056] With continued reference to FIG. 4A, separation devices 402,
404a-c, 406 and 408 could be installed in multiple locations such
that solid charge material flowing substantially downwardly in the
process vessel 106 would alternate in a radially outward flow to a
radially inward flow pattern to provide multiple opportunities for
charge solids to pass over or around surfaces of the separation
devices.
[0057] View C-C in FIG. 4E is a downward looking plan view
depicting a substantially horizontal separation table 410 with
perforated openings 411 allowing hot water to pass downwardly, be
collected in a collection pan 428 and directed out of process
vessel 106 through an internal drain 430 in fluid communication
with water discharge outlet 432. Although separation table 410 is
shown as a single table and as a complete circle in both plan and
elevation views in FIGS. 4A and 4E, it would be possible to use
multiple concentric tables of increasing diameter, each stacked
underneath a smaller table above it such that solids would flow
both downwardly and outwardly while cascading from one table to the
next. Depending on placement and diameter of separation table or
tables 410, solid charge material will flow off an outer edge of
each table due to its angle of repose while the hot water will flow
substantially downwardly through the table's perforations. Outward
flow of charge solids can be substantially improved if separation
table 410 is rotatable. This will effectively lower the angle of
repose of material referenced to horizontal and improve outward
flow of such material. It should also be possible to position
stationary plows or similar structural members above rotating
tables, such as 410, to improve the outward flow of solids and
direct the solid charge material outwardly off an edge of the table
or tables.
[0058] Although not specifically shown in FIG. 4A, it would be
possible to place another inward sloping separation cone or
concentric perforated wall inside and above the lower discharge
conical portion 434 of process vessel 106 to separate additional
hot water from charge material just prior to the charge material's
exit from process vessel 106 into discharge lock hopper 108 (FIG.
3). It would also be possible to install any of the separation
devices described above in discharge lock hopper 108 to provide
additional opportunity for separation of hot water from upgraded
charge material.
[0059] If the separation surfaces of the various separation devices
of FIG. 4A were solid instead of perforated, such surfaces would
form internal chambers or tubes within process vessel 106. If each
such chamber had a separate inlet and outlet, then heating medium
could be introduced into the inlets, thermal energy transferred
through the chamber or tube via conduction, and thermal energy
provided to process vessel 106 charge material in an indirect
manner via the principles of conduction, convection and radiation
heat transfer. Spent heating medium would then be conveyed out of
the chambers or tubes through process vessel 106 to supplement
direct forms of energy that are introduced through heating medium
inlets 314 and 316 (FIG. 3).
[0060] As a converse to putting energy into the process vessel 106,
energy could also be removed from process vessel 106 as just
described by substituting a cooling medium for a heating
medium.
[0061] Referring again to FIG. 4A, if air or other suitable
oxygen-containing gas is introduced into the process vessel 106 for
purposes of thermally oxidizing a portion of volatiles expelled
from the charge, lowering required input energy, or for rendering
the upgraded charge more stable in storage, it may be desired to
premix the air or oxygen-containing gas with the heating medium
prior to introduction into process vessel 106 through inlets 314
and 316. Although this may be the preferred approach, the air or
oxygen-containing gas could also be introduced into process vessel
106 in any other inlet position. If premixed, the air or
oxygen-containing gas would be substantially in an inert form and
not capable of reacting with the heating medium while in the piping
leading to, or in the heating medium inlets 314 and 316. Likewise,
the air or oxygen-containing gas would be incapable of reacting
with materials of construction in the piping and inlets. Once in
process vessel 106, the air or other oxygen-containing gas would be
free to expand, mix and react with various organic fuels present in
the process vessel and serve its intended purpose. If the air or
oxygen-containing gas were put into the process vessel through a
dedicated inlet, without inert heating media being present,
oxidation reactions could occur near to or within the inlet nozzle
locations and damage the structural integrity thereof due to
excessive overheating from localized, highly exothermic oxidation
reactions with the various organic based fuels being upgraded.
[0062] FIG. 5 is a schematic drawing showing a general equipment
arrangement 500 with input, internal, and output stream details for
alternative approaches to rehydrating the upgraded charge material
exiting process vessel 106 prior to storage and shipment. Two
equipment configurations can be used for rehydrating an upgraded
charge in conduit 504. These are use of equipment to provide a
blender-mixer function 506 or equipment for rehydration 512, or
both. The arrangement in FIG. 5 shows the blender-mixer 506
preceding the rehydration equipment 512, but the arrangement could
also be reversed. Upgraded charge material in conduit 504 as
discharged from discharge lock hopper 108 of FIG. 3 may be unstable
if the inherent moisture level in the material is excessively lower
than the equilibrium moisture level of the material. If this is the
case, rehydration moisture must be added back to the material to
increase the inherent moisture level to a safe differential limit
below that of the material equilibrium moisture level.
[0063] One method of rehydrating an upgraded charge is to add wet
partial upgraded or non-upgraded charge material in conduit 502 to
upgraded charge material in conduit 504, such that the blended
mixture has a desired average inherent moisture content. The final
blend must be fairly homogenous, so appropriate equipment is
required such as a blender or mixer 506. The blend could also be
made on a belt conveyor or other conveying device, if the blending
was complete and uniform.
[0064] One of the materials that could be used as wet partially
upgraded or non-upgraded charge material in conduit 502 is fines
that exit process vessel 106 in the various hot water discharges.
Another source of such material used in the blend could be feed
charge material containing free surface moisture, particularly
fines that are screened out of the carbonaceous material as
described earlier to prepare a properly sized feed charge to
process vessel 106.
[0065] If blending of solid charge materials to effect the desired
degree of rehydration is not sufficient, then water can be added
directly to upgraded charge material in the form of vapor or liquid
water in a rehydration media input stream 510, for example via
spray nozzles in equipment 512. The rehydration equipment 512 can
be a moisturizing chamber, blender, mixer, or other device
providing intimate and uniform contact between the rehydration
media in 510 and the feed charge material to the rehydration
equipment in conduit 508, such that the rehydrated upgraded charge
material in conduit 514 contains the desired amount of inherent
moisture.
EXAMPLES
[0066] For each of the following examples, the total moisture in
feed coal and the inherent moisture in process coal are both
measured by ASTM method D3302, while equilibrium moisture is
measured by ASTM method D1412-93.
Example 1
[0067] Run-Of-Mine (ROM) sub-bituminous coal from the Black Thunder
Mine near Wright, Wyo. was sized at minus 11/2 inches by plus 16
mesh. The sized coal had a moisture content of 25.2 weight percent
(w %), an equilibrium moisture content of 24.5% w % and a higher
heating value (HHV) of 9010 Btu per pound. The coal was thermally
upgraded in a batch-type autoclave of about 4 liter interior
volume. The autoclave was a vertically oriented cylinder with about
1/16 inch mesh screen removable basket in the top section into
which about 350 grams of feed coal is charged. The autoclave was
sealed and saturated steam used to raise the pressure and
corresponding saturated steam temperature to the targeted test
condition. As the steam condensed, heat was released and the
resultant condensate along with moisture released from the coal
drained and collected in the bottom of the autoclave, beneath the
coal basket. At the end of the targeted processing time, steam was
vented out of the autoclave and the pressure lowered to ambient, at
which time the basket containing the thermally upgraded coal was
removed and the processed coal submitted for analysis. Out of many
tests that were conducted, two serve to exhibit the impact of
temperature on upgraded coal properties. One was at a saturated
steam temperature of 430.degree. F. and the other at 460.degree.
F., which corresponds to respective saturated steam pressures of
about 344 pounds per square inch absolute (psia) and 467 psia.
Gauge pressures at the elevation of the test facility are about
12.5 psi lower than the absolute pressures stated. The processing
time from start of steam addition to start of venting was about 52
minutes for each test. When processed at 430.degree. F., the
upgraded coal had an inherent moisture level of 7.81 w %, an
equilibrium moisture level of 16.1 w % and a HHV of 11,397 Btu/lb.
When processed at the higher temperature of 460.degree. F., the
upgraded coal had a lower inherent moisture level of 6.0 w %, a
lower equilibrium moisture level of 14.1 w %, and a HHV of 11,674
Btu/lb. These two tests demonstrate the beneficial impact of
increasing the processing temperature (and pressure), particularly
in terms of higher temperatures lowering the equilibrium moisture
level in the upgraded product.
[0068] Note: factors other than inherent moisture impact the HHV,
such as volatile content, ash content and sulfur content. Since
different feed samples were used in these examples, the
relationship between inherent moisture and HHV is not constant.
Example 2
[0069] The same type of feed coal used in Example 1 was tested at
17 minutes total processing time at a temperature of 460.degree.
F., and when analyzed the inherent moisture level in the processed
coal was still very low at 6.3 w %, while the HHV was still
relatively high at 11,598 Btu/lb, showing that processing times
less than 20 minutes still yield very acceptable results comparable
to processing times of 52 minutes. The effect of processing time
was further demonstrated using another sample of coal with a
starting inherent moisture level of 24.1 w %, which was processed
at a temperature of 460.degree. F. Processing times of 19, 32 and
52 minutes yielded respective inherent moisture levels in the
upgraded product of 8.8 w %, 8.4 w % and 8.7 w %, and while the
final inherent moisture levels were high as a group because of
using a different sample of feed coal, there was basically no
difference in final moisture level among the three tests that can
be attributed to processing time, at least within the range of 19
to 52 minutes. Using a different batch autoclave apparatus capable
of processing about 10 pounds of coal per batch, another sample of
the Black Thunder coal similar to that described in Example No. 1
was processed at 467.degree. F. at over a very long time period of
540 minutes. The inherent moisture level in the processed coal was
6.2 w %, showing that excessively long processing time does not
impact the final moisture levels. Equilibrium moisture levels were
not measured in the samples processed at shorter and longer time
periods compared to the base cases at 52 minutes, but experience
tells us that the equilibrium moisture levels are directly
curvilinearly proportional to the inherent moisture levels.
Example 3
[0070] In two different tests with the same type of feed coal
described in Example 1, feed coal containing about 0.085 microgram
per gram (.mu.g/g) concentration of mercury, expressed on a dry
basis, was tested where air was added to one test and not to the
other. With air addition, 72.1 w % of the mercury was removed from
the processed coal and in the test without air addition, only 51.6
w % of the mercury was removed. This demonstrates that air addition
during processing improves mercury removal. The air addition was
made at the start of the test, before steam was added, and did not
flow continually into the batch autoclave during the tests, but it
is recognized that the air could have been added on a
semi-continuous or continuous basis as long as the autoclave was
vented to control the partial pressure of non-condensable gas
within the autoclave as explained in the following discussion.
[0071] In these two tests, the temperatures were the same, but the
pressures were different. When air is added to the process, it
occupies part of the total pressure with steam vapor occupying the
other part. For example, if the total pressure in the processing
vessel is 466 psia and air occupies 20 percent of the volume (v %)
and steam the other 80 v %, the partial pressure of steam is only
373 psia, which corresponds to a saturated steam temperature of
about 437.degree. F., not 460.degree. F. that would be expected if
the processing environment were 100 v % steam. As oxygen in the air
is consumed during processing due to oxidation reactions, the
reaction products equal the volume of oxygen consumed, so there is
no change in temperature because of any change in steam partial
pressure. The amount of air added during this particular test was
about 0.06 weight fraction per one unit of feed coal, keeping in
mind that the air was added on a batch basis at the beginning of
the test. The same reasoning used to show the impact of air volume
relative to steam volume on steam temperature can also be expanded
to explain the impact of non-condensable gas volume or
concentration, as the oxygen and nitrogen in air are both
non-condensable gases, as are oxidation products such as carbon
dioxide and carbon monoxide. Although carbon dioxide and carbon
monoxide are both non-condensable, only the oxygen in carbon
monoxide is reactive under the processing conditions practiced in
this invention. Other volatiles released from the charge during
processing can also be non-condensable gases such as methane,
propane, hydrogen sulfide, sulfur dioxide and etc.
Example 4
[0072] In another set of two different tests with the same type of
feed coal described in Example 1, air was added to one test on a
continuous basis and was not added to the other test. As explained
in Example 3, the process vessel was also vented on a continuous
basis. Processing conditions were essentially equal in both tests
with the same processing temperatures and times. When the liquid
collected in the two tests resulting from moisture released from
the coal, steam condensate, and soluble volatile organics was
analyzed, the test with air addition had a lower concentration of
Total Organic Carbon in the liquid, about 278 milligrams per liter
(mg/l), than the test without air addition, or about 620 mg/l,
indicating that oxygen in the air was reacting with the organics
released from the coal either before, or while it was in contact
with the water. This was also evident by less colorization in the
water from soluble organics in the test where air was added. When
organics are selectively oxidized while in the process vessel, the
overall beneficial impact is to lower the cost of water treatment
and clean-up. The amount of air added during this particular test
was about 0.002 weight fraction per unit of unit of feed coal,
keeping in mind that it was added continuously over the length of
the test.
Example 5
[0073] Referring back to Example 1, there are thermocouples in both
the upper and lower sections of the autoclave. Since steam
condenses isothermally at the saturation temperature after the coal
charge is heated up to processing temperature, one would expect
both thermocouples to indicate the same temperature as the thermal
upgrading process continues, but that is not the case. Based on
volatile assay of the coal before and after processing, 1 w % to 5
w % of the coal feed weight is lost as volatiles, on a MAF basis
(moisture and ash free). Of this amount, analysis of the
non-condensable gas generated in the up-grading process based on
tests without air addition, indicates that about 95 v % of the
volatiles that are lost are carbon dioxide gas. In the autoclave
tests, any non-condensable gas that is generated is not normally
vented out of the process until the test is over. If the carbon
dioxide non-condensable gas was mixed uniformly with the steam
vapor, we would expect both thermocouples in the upper and lower
portions of the autoclave to read the same temperature, but at a
slightly lower temperature than would be predicted by the saturated
steam pressure (see Example 3) if some non-condensable gas were
present. In all autoclave tests where liquid is not removed from
the bottom portion of the autoclave during the test, the bottom
thermocouple initially indicates the same temperature as the top
thermocouple, but as the test proceeds, the bottom thermocouple
starts to drop in temperature and has reached at least 35.degree.
F. lower temperature than the top thermocouple. Based on volumetric
measurements, it is known that when the lower thermocouple drops in
temperature it is still located in vapor space and not immersed in
liquid, but is just slightly above the liquid layer. During one
test it was decided to drain liquid out of the bottom section
before the test was over and immediately the bottom thermocouple
reading increased to match the top thermocouple, and then started
decreasing again until more liquid was drained. This observation
and procedure has been repeated without fail a number of times, and
with different processing equipment arrangements. It is now
realized that high molecular weight gases, such as carbon monoxide
with molecular weight (MW) 44 does not mix uniformly with steam
water vapor with MW 18, but instead stratifies in a lower layer.
When the carbon dioxide layer concentrated as the test progressed,
the saturated steam temperature as measured by the thermocouple
progressively lowered due to partial pressure decrease of the steam
vapor concentration (see Example No. 3 for discussion on
non-condensable gas affecting the saturated steam temperature) as
carbon dioxide concentrated in a stratified layer just above the
liquid interface. When the liquid interface was lowered due to
removal of liquid, the carbon dioxide was not removed, but the
layer level lowered and allowed the set position thermocouple to
measure gas temperature that was substantially steam vapor rather
than a mixed high concentration carbon dioxide and steam vapor
concentration. Special procedures must be employed in the
processing equipment to insure that high molecular weight
non-condensable gases are effectively removed from the process
vessel. By reasoning, the converse also holds true for
non-condensable gases that are lower in molecular weight than steam
vapor, such as hydrogen with MW 2.
Example 6
[0074] Coal was also thermally upgraded in a semi-continuously fed
and discharged process vessel consisting of about a 6 inch interior
diameter by 60 inch high cylindrical pressure vessel orientated
vertically, equipped with a feed lock hopper and a discharge lock
hopper with appropriate lock hopper valves. The unit is fed about
12 lbs of feed coal every 12-14 minutes which allows for a
processing time of about 50 to 55 minutes. The process vessel is
also discharged about every 12-14 minutes to maintain level
control. Two tests point out the benefit of adequate draining and
dewatering of the upgraded charge before discharge from the process
vessel. Black Thunder ROM coal sized at minus 1 inch by plus 8 mesh
was used as the feed coal with a moisture content of 25.8% and a
HHV of 9076 Btu/lb. Saturated steam at 459.degree. F. and 462.5
psia was used as the heating media. When liquid representing
moisture removed from the coal plus steam condensate was
continuously drained out of the bottom of the process vessel
chamber and vented to atmosphere prior to transferring the upgraded
charge to the discharge lock hopper, the inherent moisture level in
the upgraded coal when discharged was 5.0 w % with a HHV of 11,554
Btu/lb. When liquid was not properly drained out of the bottom of
the process vessel chamber, and the upgraded coal was allowed to be
discharged with accompanying volumes of free liquid, the inherent
moisture level in the upgraded charge was much higher at 12.6 w %
with a HHV of 10,791 Btu/lb.
[0075] The invention has been described with reference to a
detailed description only for the sake of example. The scope and
spirit of the invention are to be derived from the appropriately
interpreted appended claims.
* * * * *