FIELD OF THE INVENTION
1. The present invention relates to a process for
utilization of coke oven gas for partial replacement of Syngas in GAS
based direct reduction (DR) plant to produce the desired quality of
DRI with maintaining the same productivity level.
2. The present invention relates to a methodology for
utilizing the coke oven gas (COG), which is a by-product of coke
making process and readily available at any integrated steel plant
which reduces the Syngas consumption by utilization of excess
coke oven gas.
BACKGROUND OF THE INVENTION
3. The reduction of CO2 emission is a significant
challenge to steel produces due to stringent environmental law. The
production of iron and its alloys is based on the iron and steel
metallurgy. The four main routes viz., i) BF-convertor (Basic oxygen
furnace); ii) smelting reduction; iii) direct reduction (electric arc
furnace); iv) scrap [electric arc furnace ) for molten steel production
is adopting worldwide.
4. The process reduces the iron ore or iron ore pellets
without melting it called the DRI process. The feed material in this
process is either iron ore pellets or iron ore 10-30 mm. The DRI
process can be classified according to the kind and source of
reducing gas or type of reactor used. Depending on the generation
of reducing gas, two different DR processes are commercially
available: gas-based and coal/oil. The gas- based DR process is
more energy-efficient (required less than half energy) and higher
metallization as compared to coal-based DR process.

5. The produced Syngas injected into the reduction
furnace which mixed with the recycling gas, coming from the CO2
removal. The reduced gas is passed through a humidifier tank,
where a small amount of water is added to the gas stream to
optimum control of the carburization process. The reducing gas is
heated up to 970°C in the process gas heater. Also, the oxygen gas
is injected in the transfer line.
6. Just before the reactor to increase the temperature of
the reducing gas to the required level for in-situ reforming and
reduction inside the reactor.
7. In this process, partial oxidation is carried out in the
transfer line and hence the reducing gas inlet temperature
increases. The partial oxidation and reforming reactions are as
follows:
CH4 + ⁄ 2 O2 → CO + 2H2
O2 + 2H2 → H2O
CH4 + H2O → CO + 3H2
CO2 + H2 → CO + H2O

8. In this process, the hot reducing gas is fed to the reactor reduction
zone and flows upward counter-currently to the Iron ore moving bed. The gas
distribution is uniform, and there is a high degree of direct contact between the
gas and solid. The exhaust reducing gas (top gas) leaves the reactor, at about
450 °C, and passes through the quenching/scrubbing system. In these units,
water produced during the reduction process is condensed and removed from
the gas stream, and hence most of the dust carried with the gas separated.
Scrubbed gas is then passed through the process gas recycle compressors, where
gas pressure is increased. The compressed gas (after being sent to the carbon
dioxide removal unit) is mixed with the syngas make-up, thus closing the
reducing gas circuit.
9. The steel production through DR route is costlier in JSPL, Angul
unit due to the higher cost of produced syngas. This higher cost of syngas is due
to lack of availability of the desired quality of Indian coals. Therefore, a team had
worked on another possible route to produced hot metal at economical cost. In
recent past effort has been made to utilize alternative fuel in this process. This
is necessary to use lower-cost fuel to produce optimal cost of hot metal. Based
on the several methodologies, the team found that the coke oven gas (COG) may
efficiently use in the existing DRI process with the comparatively lesser cost of
hot metal production. Since, JSPL, Angul unit having 1.90 MTPA recovery stamp
charged coke oven plant and therefore the generated coke oven gas during coke
making is surplus. This surplus quantity of coke oven gas had flared and
wastage, which is easily utilized in the present invention as an alternative fuel of
syngas in the DRI plant. It is well known that coke oven gas has high calorific
value as compared to syngas, and therefore it may not like to like use in the DRI
plant, but of course, it may partially replace the syngas which will reduce the
DRI cost significantly.

10. Please elaborate the problems in the prior arts also.
11. The present invention meets the long felt need by replacing syngas
with coke oven gas, which will minimize the use of coal in the gasification unit,
and thereby it will help to decrease the DRI production cost through the lesser
cost of fuel gas.
OBJECTS OF THE PRESENT INVENTION
12. It is therefore the primary object of the present invention to provide
a method of producing low cost DRI, for alternative fuel of syngas which has
lower in cost for DR process;
13. Another object of this invention is to propose a process for
developing a methodology for producing low cost DRI, which injects COG gas in
reducing gas heater through COG booster compressor.
14. Another object of this invention is to propose a process for
developing a methodology for producing low cost DRI, which utilizes the coke
oven gas in reducing heater through COG booster compressor for reducing the
cost.
15. Another object of this invention is to propose a process for producing
optimal cost DRI with maintaining productivity.
16. Still another object of this invention is to provide a process for
developing a methodology for producing low cost DRI , which reduces the
generation of less CO2 emission by saving the quantity of non-coking coals;

17. Further, the object of this invention is to provide the use of
alternative fuel for improving the process efficiency.
18. Another object of the present invention is to provide a process for
developing a methodology for producing low cost DRI, which is not only cost
effective, is rapid and does not causes any harm to the environment.
SUMMARY OF THE INVENTION
19. One or more drawbacks of conventional systems and process for a
method for high cost production of DRI, which overcome and additional
advantages are provided through the method as claimed in the present
disclosure. Additional features and advantages are realized through the
technicalities of the present disclosure. Other embodiments and aspects of the
disclosure are described in details herein and are considered to be part of the
claimed disclosure.
20. Various objects, features, aspects, and advantages of the inventive
subject matter will become more apparent from the following detailed description
of preferred embodiments, along with the accompanying drawing figures.
21. It is to be understood that the aspects and embodiments of the
disclosure described above may be used in any combination with each other.
Several of the aspects and embodiments may be combined to form a further
embodiment of the disclosure.
22. The foregoing summary is illustrative only and is not intended to be
in any way limiting. In addition to the illustrative aspects, embodiments, and
features described above, further aspects, embodiments, and features will

become apparent by reference to the drawings and the following detailed
description.
BRIEF DESCRIPTION OF THE ACCOMPANYING DRAWINGS
23. The illustrated embodiments of the subject matter will be best
understood by reference to the drawings, wherein like parts are designated by
like numerals throughout. The following description is intended only by way of
example, and simply illustrates certain selected embodiments of system
processes that are consistent with the subject matter as claimed herein, wherein:
24. Figure 1 illustrates the schematic layout of Syngas based DRI plant
for the production of DRI or sponge Iron.
25. Figure 2 illustrates the schematic layout of the proposed mixed gas
(Syngas + COG) DRI plant.
26. Figure 3 illustrates the schematic layout COG Booster Compressor
for the addition of COG to reducing gas heater.
27. Figure 4 illustrates the schematic layout of the proposed process for
the addition of COG in a reduction furnace.
28. Figure 5 illustrates the schematic layout for Ejector (side view) for
feeding the COG to reduction furnace in DRI plant.
29. Figure 6 illustrates the schematic layout for Ejector (front view) for
feeding the COG to reduction furnace in DRI plant.

000030. The figures depict embodiments of the disclosure for purposes of
illustration only. One skilled in the art will readily recognize from the following
description that alternative embodiments of the methods illustrated herein may
be employed without departing from the principles of the disclosure described
herein.
DETAILED DESCRIPTION OF THE PRESENT INVENTION
31. While the embodiments of the disclosure are subject to various
modifications and alternative forms, specific embodiment thereof have been
shown by way the figures and will be described below. It should be understood,
however, that it is not intended to limit the disclosure to the particular forms
disclosed, but on the contrary, the disclosure is to cover all modifications,
equivalents and alternative falling within the scope of the disclosure.
32. It is to be noted that a person skilled in the art would be motivated
from the present disclosure to arrive at a method for producing low cost DRI
in furnace. Such a method for evaluating the same may vary based on
configuration of one or more workpieces. However, such modifications should
be construed within the scope of the disclosure. Accordingly, the drawings
illustrate only those specific details that are pertinent to understand the
embodiments of the present disclosure, so as not to obscure the disclosure
with details that will be clear to those of ordinary skill in the art having benefit
of the description herein.
33. As used in the description herein and throughout the claims that
follow, the meaning of “a”, “an”, and “the” includes plural reference unless the
context clearly dictates otherwise. Also, as used in the description herein, the
meaning of “in” includes “in” and “on” unless the context clearly dictates
otherwise.

000034. The terms “comprises”, “comprising”, or any other variations
thereof used in the disclosure, are intended to cover a non-exclusive inclusion,
such that a method, system that comprises a list of components does not
include only those components but may include other components not
expressly listed or inherent to such method, or assembly, or method.
000035. The full form of some abbreviation are given below:
BF : blast furnace
CGP : coal gasification plant
DRI : direct reduction of iron
Gcal : giga calories
h : hours
kcal : kilo calories
PGC : process gas compressor
t : ton
TGS : top gas scrubber
TPH : ton per hour
BT : bustle temperature
NCV : net calorific value
Nm3 : normal cubic meter
RG : reducing gas
000036. In other words, one or more elements in a system or device
proceeded by “comprises…..a” does not, without more constraints, preclude the

existence of other elements or additional elements in the system, apparatus or
device.
37. The present subject matter relates to to a process for utilization of
coke oven gas for partial replacement of Syngas in GAS based direct reduction
(DR) plant to produce the desired quality of DRI with maintaining the same
productivity level.
38. The production cost of direct reduced iron (DRI) is directly depends
on the fuel cost i.e. Syngas cost. The production cost of Syngas through coal
gasification is significantly depends on the type/grade of which used coal in the
gasifier. Since JSPL, Angul is not having own coal mine and hence fully depends
on the coal available in the market. In general, Indian reserve coal is having
peculiar characteristic viz., higher in ash content and lower in GCV which is not
suitable for fixed bed gasifier.
39. The present novel methodology has been developed for a partial
replacement of Syngas from clean coke oven gas to produce the optimum cost of
hot metal. In the present invention, Syngas coming from the coal gasification
process is enriched by the mixing of clean coke oven gas before entering the
reduction furnace and hence the requirement of Syngas consumption reduces
and thereby reduces the coal requirement in coal. This reduction of coal also
helps for reducing the CO2 emission.
40. In the present invention, iron ore pellets and iron ore lump used as
feed material. The coke oven gas and syngas was used as a fuel for reducing the
feed material for making sponge iron or DRI. The used syngas produces from
coal gasification plant where the non-coking coal was used as raw material while
the coke oven gas is a by-product of the coke making process.

41. The properties of non-coking coal used in coal gasification plant are
presented in Table 1 - 4.
42. Table 1 presents the typical size analysis of raw of mine (ROM) coal
from 0 -75 mm size. This size analysis comprises +75 mm (19.19%), -75mm to
+50mm (12.08%), - 50mm to +30mm (9.48%), -30mm to +20mm (11.82%), -
20mm to +15mm (5.38%), -15mm to +10mm (8.88%), -10mm to +8 mm (2.14%),
-8mm to +5 mm (4.8%) and -5 to 0 mm (26.23%).
Table 1: Typical size analysis of ROM coal (unwashed coal)

Size,
mm +75 -75 to
50 -50 to
30 -30 to
20 -20 to
15 -15 to
10 -10 to -8 to
8 5 -5 to 0
Feed
Value,
% 19.19 12.08 9.48 11.82 5.38 8.88 2.14 4.80 26.23
43. Table 2 depicts the properties of ROM coal like total moisture
(13.38%), inherent moisture (6.11%), ash (52.58%), volatile matter (20.45%),
fixed carbon (20.58%), and GCV (2481 kcal/kg) during the feed into coal washery
plant.
44. Table 3 shows the properties of washed coal like total moisture
(11.9%), inherent moisture (6.11%), ash (32.33%), volatile matter (24.05%), fixed
carbon (31.36%), and GCV (4030 kcal/kg) during the feed into coal gasification
plant.

Table 2: Typical properties of ROM coal (unwashed coal)

Total
Moisture, % Inherent
Moisture, % Ash, % Volatile
Matter, % Fixed
Carbon, % GCV,
kcal/kg
13.38 6.11 52.58 20.45 20.58 2481
Table 3: Typical properties of feed coal in coal gasifier (after
beneficiation)

Total
Moisture, % Inherent
Moisture, % Ash, % Volatile
Matter, % Fixed
Carbon, % NCV,
kcal/ Nm3
11.9 3.11 32.33 24.05 31.36 4030
000045. Table 4 depicts the desired size fraction and actual feed size into the
gasifier at coal gasification plant.
Table 4: Typical size analysis of feed coal in coal gasifier

Size, mm -70 to
50 -50 to
33 -33 to
22 -22 to
15 -15 to
10 -10 to 7 -7 to 5 -5.0
<3.0
1.5 <15
--
25.5
Desired
Value, % <3.0 16.0 29.0 21.0 18.0 7.0 3.0

Feed
Value % 5.9 30.2 26.1 12.1 18.2 3.1 2.7

000046. In the present invention, mixed gas (syngas + COG) used as a fuel.
The coke oven gas (COG) utilized for two different applications like reducing gas

heater and reduction furnace in the DRI process. The COG partially replace to
syngas. The replacement ratio of COG in both applications is 1:1.18.
000047. Table 5 present the typical composition of syngas like H2 (52.9%),
CO2 (1.6%), O2 (0%), N2 (0.2%), CO (32.3%), CH4 (12.3%), CnHm (0.75%), H2O
(0%), H2S (0.01%) and NCV (3500 kcal/Nm3). Similarly Table 5 contains the
typical value of coke oven gas (COG) like H2 (52.8%), CO2 (2.9%), O2 (0.5%), N2
(5.8%), CO (5.8%), CH4 (25.0%), CnHm (3.3%), H2O (4.0%), H2S (0.0%) and net
calorific value (4182 kcal/Nm3).
Table 5: Typical composition of syngas

H2, % CO2,
% O2, % N2,
%
0.2 CO, % CH4,
% CnHm,
% H2O,
% H2S,
% GCV,
kcal/Nm3
52.9 1.6 0.0
32.3 12.3 0.75 0.0 0.01 3500
000048. The typical composition of mixed gas presented in Table 7. This gas
contain like H2 (59.1%), CO2 (2.26%), O2 (0.0%), N2 (2.92%), CO (25.58%), CH4
(6.42%), CnHm (0.28%), H2O (3.42%) and H2S (22 ppm).
Table 6: Typical composition of coke oven gas (COG)

H2, % CO2, % O2, % N2, % CO,
% CH4,
% CnHm,
% H2O,
% H2S,
% GCV,
kcal/Nm3
52.8 2.9 0.5 5.8 5.8 25.0 3.3 4.0 0.0 4182

Table 7: Typical Composition of Ejector Mixed-gas to RG Duct

H2, % CO2, % O2, % N2, % CO, % CH4, % OHC, % H2O, % H2S, ppmv
59.10 2.26 0.0 2.92 25.58 6.42 0.28 3.42 22
000049. Table 8 represents the essential operating parameter of gas-based
DRI plant.

000050. The process for producing low cost DRI comprises the steps of:
taking iron ore lump and pellet as the feed of DRI plant;
production of DRI or sponge iron at DRI plant;

feeding fuel gas through reducing gas heater and COG gas ejector to eject low
pressure COG;
mixing of low pressure COG with syngas through ejector and injected without
any booster at two locations;
heating of fuel gas before charging into reducing furnace;
wherein the said COG is partially replaced the existing syngas in gas heater
through COG BOOSTER COMPRESSOR with the replacement ratio of 1:1.19.
51. At DRI battery limit COG is available at 60 mbar. COG booster
compressor will compress low-pressure COG gas to >0.5 bar which is compatible
to use COG as fuel and enrichment to top gas fuel in burner. COG has 1.2 times
more calorific value compared to Syngas which effectively replaces Syngas as a
fuel. The COG is mixed with the top gas fuel in the reducing gas heater. Since
COG has two times more calorific value as compared to furnace top gas, and
therefore it has the potential to save the furnace top gas. This furnace top gas
can save by recirculated as process gas which ultimately increases feed gas to
the heater and therefore requires less Syngas addition into the feed gas. Thus,
the addition of COG in the existing DRI process reduces the consumption of
Syngas. A total of 11 kNm3/h COG utilized as a fuel in reducing gas heater in
place of syngas. Therefore, practically it saves 13.2 kNm3/h Syngas with the
same productivity.
52. The primary function of COG ejector is to eject low-pressure COG by
using high- pressure Syngas. Since the COG line pressure at DRI is ~ 60 mbar
and therefore ejector need motive fluid to eject the low-pressure COG gas
through the ejector. High-pressure syngas is available in DRI plant 24 bars and
works as motive fluid for the ejector. Low-pressure COG is mixed with Syngas
through Ejector and developed the mixed gas pressure at ejector outlet above the

reducing gas pressure which is injected easily without any boosters at two
different locations of the furnace in Bustle and Reheat Line. Hence, total 13
kNm3/h COG utilized with the help of ejector into the DRI process. By the
implementing of the present invention, COG can replace Syngas to 1.18 times.
This 13 kNm3/h COG is replacing 15.3 kNm3/h Syngas for maintaining the same
productivity.
53. The overall process flow sheet of the gas-based DRI process is
mentioned in Figure 1. The process equipment used raw material (iron
ore/pellet), gas scrubber, gas compressor, reducing gas heater, CO2 removal
system, turbo expander, feeding line of syngas gas and coke oven gas (COG).
54. The overall process flow sheet of the proposed process is mentioned
in Figure 2. The process equipment used raw material (iron ore/pellet gas
scrubber, COG booster compressor to feed the COG to gas heater, gas
compressor, reducing gas heater, CO2 removal system, turbo expander, feeding
line of syngas gas and coke oven gas (COG).
55. The COG booster compressor used for the addition of COG into the
reducing gas heater in the proposed invention is presented in Figure 3, whereas,
Figure 4 shows the process flow diagram of ejector for feeding the COG to
reduction furnace (main furnace). Figure 4 and 5 shows the side view and front
view of the ejector which is essential methodology of the present invention.
56. At DRI battery limit COG is available at 60 bar. COG booster
compressor will compress low-pressure COG gas to >0.5 bar which is compatible
to use COG as fuel and enrichment to top gas fuel in burner. COG has 1.2 times
more calorific value compared to Syngas which effectively replaces Syngas as a
fuel. The COG is mixed with the top gas fuel in the reducing gas heater. Since

COG has two times more calorific value as compared to furnace top gas, and
therefore it has the potential to save the furnace top gas. This furnace top gas
can save by recirculated as process gas which ultimately increases feed gas to
the heater and therefore requires less Syngas addition into the feed gas. Thus,
the addition of COG in the existing DRI process reduces the consumption of
Syngas. A total of 11 kNm3/h COG utilized as a fuel in reducing gas heater in
place of syngas. Therefore, practically it saves 13.2 kNm3/h Syngas with the
same productivity.
000057. BASIC ASSUMPTIONS FOR COMPARISON OF THE POTENTIAL
OF SYNGASAND (SYNGAS +COG) AS FUEL

Production of DRI : 200 TPH
Bustle gas Temperature : 1000 °C
Moisture content in Pellet : 1.5 %
Feed Rate of Pellet : 225MT/
NCV of Coke Oven Gas, h : 4182 kcal/Nm3
NCV of Syngas : 3500 kcal/ Nm3
Enthalpy of Syn Gas : 3525 kcal/Nm3
Temperature at reducing gas heater : 950 °C
Bed temperature of reduction furnace : ~780-800 °C
Metallization : >92 %
000058. In the present invention, COG is replaced the syngas 1.18 times i.e.,
13 kNm3/h COG is replacing 15.3 kNm3/h syngas for the same productivity of
DRI. Therefor syngas requirement reduces significantly in the DRI and hence

reduce the coal gas requirement for making 2.25 time costlier syngas in coal
gasification plant. This reduction in coal consumption in coal gasification plant
also help for reducing the CO2 emission by 55 kg/MT DRI production. Hence,
by adopting the said process, 1,46,540 INR/h i.e., 651 INR/MT of DRI production
saved. By the implementing the said process the productivity and resultant
quality of DRI remain constant.
000059. The non-limiting advantages of the present invention given as
follows:
1. In the present invention, wherein the said COG is 2.25 times cheaper as
compared to produced syngas through coal gasification plant.
2. The COG replaced the syngas 1.18 times, i.e., 13 kNm3/h COG is replacing
15.3 kNm3/h syngas for the same productivity of the DRI.
3. The total cost of the process reduced by 67,100 INR/h, i.e., 298 INR/MT
in the utilization of COG in the gas heater.
4. The total cost of the process reduced by 79,440 INR/h, i.e., 353 INR/MT
in the utilization of COG in reduction furnace for producing the sponge iron or
DRI.
5. The total cost of the process reduced by 1,46,540 INR/h, i.e., 651 INR/MT
of DRI production.
6. In the present process, the requirement of production of Syngas
production is ~26,180 Nm3/h i.e., 131 Nm3/MT less and thereby requirement of
the non-coking coal is ~40 MT/h, i.e., 0.2 MT/ton production of DRI by
utilization of COG in DRI and thereby reducing the CO2 emission by 11 MT/h,
i.e., 55 kg/MT DRI production.
7. In the process, the productivity and resultant quality of DRI or sponge iron

8. The process efficiency of DRI claims improves by utilization of COG in both
gas heater and reduction furnace in DRI.
9. Each of the appended claims defines a separate invention, which for
infringement purposes is recognized as including equivalents to the various
elements or limitations specified in the claims. Depending on the context, all
references below to the “invention” may in some cases refer to certain specific
embodiments only. In other cases, it will be recognized that references to the
“invention” will refer to subject matter recited in one or more, but not necessarily
all, of the claims.
10. Groupings of alternative elements or embodiments of the invention
disclosed herein are not to be construed as limitations. Each group member can
be referred to and claimed individually or in any combination with other
members of the group or other elements found herein. One or more members of
a group can be included in, or deleted from, a group for reasons of convenience
and/or patentability. When any such inclusion or deletion occurs, the
specification is herein deemed to contain the group as modified thus fulfilling
the written description of all groups used in the appended claims.
Equivalents:
60. With respect to the use of substantially any plural and/or singular
terms herein, those having skill in the art can translate from the plural to the
singular and/or from the singular to the plural as is appropriate to the context
and/or application. The various singular/plural permutations may be expressly
set forth herein for sake of clarity.
61. It will be understood by those within the art that, in general, terms

used herein, and especially in the appended claims (e.g., bodies of the appended
claims) are generally intended as “open” terms (e.g., the term “including” should
be interpreted as “including but not limited to”, the term “having” should be
interpreted as “having at least”, the term “includes” should be interpreted as
“includes but is not limited to”, etc.). It will be further understood by those within
the art that if a specific number of an introduced claim recitation is intended,
such an intent will be explicitly recited in the claim, and in the absence of such
recitation no such intent is present.
62. The above description does not provide specific details of
manufacture or design of the various components. Those of skill in the art are
familiar with such details, and unless departures from those techniques are set
out, techniques, known, related art or later developed designs and materials
should be employed. Those in the art are capable of choosing suitable
manufacturing and design details.
63. The terminology used herein is for the purpose of describing
particular embodiments only and is not intended to be limiting of the present
disclosure. It will be appreciated that several of the above-disclosed and other
features and functions, or alternatives thereof, may be combined into other
systems or applications. Various presently unforeseen or unanticipated
alternatives, modifications, variations, or improvements therein may
subsequently be made by those skilled in the art without departing from the
scope of the present disclosure as encompassed by the following claims.
64. The claims, as originally presented and as they may be amended,
encompass variations, alternatives, modifications, improvements, equivalents,
and substantial equivalents of the embodiments and teachings disclosed herein,

including those that are presently unforeseen or unappreciated, and that, for
example, may arise from applicants/patentees and others.
000065. While various aspects and embodiments have been disclosed herein,
other aspects and embodiments will be apparent to those skilled in the art. The
various aspects and embodiments disclosed herein are for purposes of
illustration and are not intended to be limiting, with the true scope and spirit
being indicated by the following claims.

We claim:
1. A process for producing low cost DRI comprises the steps of:
taking iron ore lump and pellet as the feed of DRI plant;
production of DRI or sponge iron at DRI plant;
feeding fuel gas through reducing gas heater and coke oven gas (COG)
ejector to eject low pressure COG;
mixing of low pressure COG with syngas through ejector and injected
without any booster at two locations;
heating of fuel gas before charging into reducing furnace;
wherein the said COG is partially replaced the existing syngas in gas
heater through cog booster compressor with the replacement ratio of
1:1.19.
2. The process as claimed in claim 1, wherein said feed fuel gas is heated at
a temperature of 970 °C.
3. The process as claimed in claim 1, wherein the said COG replaced the
syngas 1.18 times, i.e., 13 kNm3/h COG is replacing 15.3 kNm3/h syngas
for the same productivity of the DRI.
4. The process as claimed in claim 1, wherein the COG line pressure at DRI
is at ~ 60 mbar (give definite value or range) and therefore ejector need
motive fluid to eject the low-pressure COG gas through the ejector.

5. The process as claimed in claim 1, wherein the requirement of production
of Syngas production is ~26,180 Nm3/h i.e., 131 Nm3/MT less and thereby
requirement of the non-coking coal is ~40 MT/h, i.e., 0.2 MT/ton
production of DRI by utilization of COG in DRI and thereby reducing the
CO2 emission by 11 MT/h, i.e., 55 kg/MT DRI production.