U.S. patent number 3,671,402 [Application Number 05/032,891] was granted by the patent office on 1972-06-20 for fluidizing bed coking method of brown coal.
This patent grant is currently assigned to Rheinische Braunkohlenwerke AG. Invention is credited to Hans Penning, Werner Wenzel.
United States Patent |
3,671,402 |
Wenzel , et al. |
June 20, 1972 |
FLUIDIZING BED COKING METHOD OF BROWN COAL
Abstract
For the coking of brown coal, lignite or the like there is
provided a coking system which includes a coking apparatus and an
associated heater from which hot air is introduced into the coking
apparatus. One part of the fine grained portion of the charge mixed
with gases derived from the coking process is introduced from the
coking apparatus into the combustion chamber of said heater to
serve as fuel therefor.
Inventors: |
Wenzel; Werner (Aachen,
DT), Penning; Hans (Cologne Lindenthal,
DT) |
Assignee: |
Rheinische Braunkohlenwerke AG
(Koln, DT)
|
Family
ID: |
5732693 |
Appl.
No.: |
05/032,891 |
Filed: |
April 29, 1970 |
Foreign Application Priority Data
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Apr 29, 1969 [DT] |
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P 19 21 710.8 |
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Current U.S.
Class: |
201/15; 201/6;
201/31; 201/27; 201/42 |
Current CPC
Class: |
C10B
49/08 (20130101) |
Current International
Class: |
C10B
49/00 (20060101); C10B 49/08 (20060101); C10b
049/10 () |
Field of
Search: |
;201/27,13,14,15,16,31,42,32,36,37,38 ;110/28J,8 ;202/121 |
References Cited
[Referenced By]
U.S. Patent Documents
Primary Examiner: Yudkoff; Norman
Assistant Examiner: Edwards; David
Claims
What is claimed is
1. A method of coking brown coal or the like comprising the
following steps:
A. continuously charging a coking apparatus with said coal having a
grain size between 0 and approximately 30 mm,
B. introducing hot gas from a heater into said coking apparatus for
effecting coking therein,
C. introducing approximately 75-95 percent of the coal charge as
fine-grained coal with and by means of coking gases from said
coking apparatus into said heater,
D. burning the coal-gas mixture introduced in said heater to obtain
said hot gas,
E. converting the approximately 5-25 percent of the charge
remaining in the coking apparatus into coke having a grain size
approximately 5 - 20 mm, and
F. withdrawing said coke from said coking apparatus.
2. A method as defined in claim 1, wherein said charge is
introduced into said coking apparatus downwardly at the upper
portion thereof and said hot gas is introduced into said coking
apparatus upwardly through a base thereof to create a fluidized bed
containing said 5-25 percent of said charge and to cause said 75-95
percent of said charge to be carried into said heater.
3. A method as defined in claim 1, wherein said hot gas has a
temperature between approximately 250.degree. C- 450.degree. C.
4. A method as defined in claim 1, wherein the flow rate of said
charge and of said hot gas is so regulated that the temperature in
said coking apparatus is at a value between 600.degree. -
900.degree. C.
5. A method as defined in claim 1, including the step of
comminuting the coal taken out with said coking gases from said
coking apparatus prior to its introduction into said heater.
6. A method as defined in claim 5, wherein said comminuting step
effects a reduction of the coal taken from said coking apparatus to
powder size grains.
Description
BACKGROUND OF THE INVENTION
The economic feasibility of the manufacture of coke from
fossil-type fuels is affected to a significant extent by the costs
involving their preparatory treatment. Accordingly, it is a basic
desideratum to submit the coal, prior to coking, to as few
processes as possible to keep the entire coking operation simple
and economical.
In view of the above considerations, either raw brown coal, or a
coal little burdened by drying, comminuting or preforming (such as
pelletizing) should be used for coking fossil-type charges. Despite
advantageous prospects of coking raw coal, no coking processes of
this type for mass production have been developed. The reason for
this may probably be found in the difficult pyrometric conditions
required for the coking of raw coal.
The invention is based on a known process of and an apparatus for
coking brown coal, particularly brown coal having a relatively high
water content, whereby the coking is performed while the coal is in
a turbulent condition and the necessary heat is supplied by
injecting hot gases, preferably derived from a partial combustion
of the coal. The gases obtained during the coking process are
burned in a heater.
OBJECT AND SUMMARY OF THE INVENTION
It is an object of the invention to introduce an improved method
and an apparatus of the aforenoted type for providing a technically
and economically advantageous coking of brown coal, particularly
raw brown coal, lignite or similar fuel.
Briefly stated, according to the invention, the coking apparatus is
connected with a heater from which hot air is introduced into the
coking apparatus. One part of the fine grained portion of the
charge is carried by the gases derived from the coking process into
the heater to serve as fuel therefor.
The invention will be better understood and further objects and
advantages will become more apparent from the ensuing detailed
specification of a preferred, although exemplary embodiment of the
invention taken in conjunction with the sole figure schematically
illustrating the embodiment .
DESCRIPTION OF THE PREFERRED EMBODIMENT 0- comminuting
The coking system according to the invention includes a coking
apparatus 1 having an apertured, sieve-like base 2. The apparatus 1
is charged at the top at 4 with coking fuel such as brown coal
which preferably has a grain size of 0- 30 mm. The grain size
distribution is that which normally results from crushing raw brown
coal in a conventional communiting device.
The coking system according to the invention further includes a
heater 7 from which heated air for combustion is taken through
conduit 3 and introduced into the coking apparatus 1 at 3a through
the apertured base 2. By virtue of the upwardly directed air flow a
fluidized bed is formed which is supported by the apertured base
2.
The velocity of the gas through the fluidized bed is set to such a
value that the large size coal settles on or in the vicinity of the
base 2. In this range the coal is not exposed to the turbulent air
action proper; there is merely a relatively slight mixing caused by
the throughgoing gases. In an extreme case, the large-grained coal
supported on base 2 may form a stationary bed which, as the grain
size decreases upwardly, gradually changes into the fluidized bed
proper.
The velocity of the gas streaming through the coking apparatus is
further so regulated that a major, fine-grained portion of the coal
(approximately 75-95 percent of the charge) is carried by the
combustion gases derived from the coking through conduit 6 and
introduced into the heater 7. Approximately 5-25 percent of the
charge remains in the coking apparatus due to its grain size. In
the heater 7 the mixture of coal and coking gases is burned with
the aid of hot air taken from the heater 7 itself and introduced
into its firing chamber through conduit 3b. Exhaust gases resulting
from this combustion are discharged at 8.
The most advantageous velocities of the gas at different heights of
the fluidized bed may be regulated in a known manner by accordingly
varying the cross-sectional configuration of the fluidized bed.
Thus, for example, the cross section of the fluidized bed may be of
a smaller value at its base than at its upper surface.
The hot air furnished by the heater 7 to the coking apparatus at a
temperature of approximately 250.degree.-450.degree. C, burns
preponderantly with the fine-grained portion of the raw coal with
simultaneous heat generation. The ratio of hot air admitted through
base 2 to the raw brown coal charged at 4 is set to such a value
that an average temperature of 600.degree.- 900.degree. C prevails
in the coking apparatus. At such temperature, a rapid drying of the
fine-grained pieces of the raw brown coal takes place, so that the
latter may be carried out of the coking apparatus at 6 by the gases
in a substantially dried condition.
The coal pieces of large dimension which, as noted hereinbefore,
settle at the base 2 because of their weight and constitute about
5-25 percent of the charge, are dried and degassed, whereby the
degree of degasification and of conversion into coke are dependent
on the dwelling time of the respective coal pieces in the coking
bed and on the temperature prevailing in the coking apparatus.
The finished coke, which has a grain size of about 5- 20 mm, may be
taken out of the fluid bed at 5 by known removing means (e.g. an
auger mechanism) directly from above the perforated base 2.
In order to adapt the coal taken from the coking apparatus 1 to the
firing conditions of the adjoining heater 7, the coal may be
comminuted, preferably to powder form, prior to the introduction
thereof into the heater. For this purpose, known comminuting
apparatus such as an impact mill, may be used.
Several modifications may be effected in the afore-described
exemplary embodiment of the invention to adapt it to any particular
type of coal or heater. Thus, instead of a fluidized bed-type
coking apparatus a mobile grill-type coking apparatus may be used.
In such an apparatus a major part of the coal is combusted on the
grill for generating the heat necessary to operate the heater,
while a smaller part of the charge is carried out by the grill as
coke. Instead of hot air, hot gases may be blown through the coking
apparatus. These hot gases may be, for example, the exhaust gases
taken from the heater.
* * * * *