1

Shiro WATAKABE

Assistant Sub Project Leader of COURSE50JFE Steel Corp.

Current Progress on COURSE50 Project

-- Recent Results on H2 Reduction including LKAB’s EBF Experiments and CO2 Capture --

5th November 2013at Tokyo Institute of Technology

IEAGHG/IETS Iron & Steel IndustryCCUS & Process Integration Workshop

2Contents

1. About COURSE50 Project

2. Current status of COURSE50

3. Test operation trial at experimental blast furnace

3Contents

1. About COURSE50 Project

2. Current status of COURSE50

3. Test operation trial at experimental blast furnace

4Drastic CO2 Emissions Reduction in Steel Industry

Alternative reducing agents Reduction in carbon

Steps for radical

reduction

(1) Utilization of hydrogen① Natural gas

② By-product gas

(1) CO2 capture

① CO2 capture from BFG

・ Chemical absorption

・ Physical adsorption

(2) Direct use of electricity

① Hydrometallurgy

(3) Use of C-Neutral agents

① Biomass

・Charcoal reduction, waste use

② CO2 capture from other reduction processes

・ Coal-based Smelting Reduction

・ Coal-based Direct reduction

Scenario 21)Maximum use of waste heat 2)Expanded use of waste heat through CO2

absorbent development 3)Utilization of external energy sources

Scenario 11)Further improvement of COG reforming efficiency by the use of waste heat

5Innovative Steelmaking Process -COURSE50-

COURSE50 : CO2 Ultimate Reduction in Steelmaking Process by Innovative Technology for Cool Earth 50

• Coal is used to reduce iron ore in steelmaking process.• Even with enhanced energy-saving, emission of CO2 is unavoidable.

• COURSE 50 aims at developing technologies to decrease CO2 emissions by approximately 30% through reduction of iron ore by hydrogen as well as capture – separation and recovery – of CO2 from blast furnace gas.

• The initiative targets establishing the technologies by ca. 2030 with the final goal of industrializing and transferring them by 2050, taking advantage of renewing blast furnaces and relevant facilities.

Outline of COURSE 50

1. Total budget: approximately 10 billion yen

2. Schedule:

3. R&D targets:

(1)Development of technologies to reduce CO2 emissions

from blast furnace

(2)Development of technologies to capture - separate and

recover - CO2 from blast furnace gas (BFG)

Phase1 Step1(2008～12）

Phase1 Step2(2013-17）

Phase 2 Industrialization & Transfer

2010 2020 2030 2040 2050

6Development of Technologies for Environmentally Harmonized Steelmaking Process

(1) Technologies to reduce CO2 emissions from blast furnace (2) Technologies for CO2 capture

・Chemical absorptionReduction of cokeIron ore

H2 amplification

H2

BOF

Electricity

High strength & high reactivity coke

Coking plant

Coke BFG

BF

Shaft furnace

・Physical adsorption

CO-rich gas

Regeneration Tower

Reboiler

Absorption Tower

Steam

Hot metal

Cold air

Hot air Sensible heat recovery from slag (example) Waste heat recovery boiler

CO2 storage technology

Kalina cycle

Power generation

Slag

Iron ore pre-reduction

technology Coke substitution reducing agent production technology CO2 capture

technology

Coke production technology for BF hydrogen reduction

for BF hydrogen reduction Reaction control technology

Technology for utilization of unused waste heat

Other project

COG reformer

(1)Technologies to reduce CO2 emissions from blast furnace (2)Technologies for CO2 capture

7Project Targets

(1)Development of technologies to reduce CO2 emissions from blast furnace

・ Develop technologies to control reactions for reducing iron ore with hydrogenous agents to decrease coke consumption in BF.

・ Develop technologies to reform coke oven gas (COG) aiming at amplifying hydrogen concentration by utilizing unused COG heat.

・ Develop technologies to produce high strength and high reactivity

coke for reduction with hydrogen.

(2)Development of technologies to capture - separate and recover - CO2 from blast furnace gas (BFG)

・ Develop techniques for chemical absorption and physical adsorption to capture CO2 from blast furnace gas.

・ Develop technologies to reduce energy to capture CO2 through enhanced utilization of unused waste heat.

8R&D Organization and Sub-Projects

1. Development of technologies to utilize hydrogen for iron ore reduction.2. Development of technologies to reform COG through the amplification of

hydrogen.3. Development of technologies to produce optimum coke for hydrogen

reduction of iron ore.4. Development of technologies to capture – separate and recover – CO2

from BFG.5. Development of technologies to recover unused sensible heat.6. Holistic evaluation of the total process.

NEDO*

Kobe Steel, Ltd.JFE Steel CorporationNippon Steel & Sumitomo Metal CorporationNippon Steel & Sumikin Engineering Co., Ltd.Nisshin Steel Co., Ltd.

Contract research

* NEDO New Energy and industrial technology Development Organization ** COURSE 50 Committee at the Japan Iron and Steel Federation (JISF) supports the five companies’ R&D activities.

COURSE 50 Committee**

Sub-Projects (Phase1 Step1)

9Contents

1. About COURSE50 Project

2. Current status of COURSE50

3. Test operation trial at experimental blast furnace

10Sub-Project 1

Identification of feeding conditions of preheated gas, aiming at constraining ore degradation by reduction associated with enhanced reduction by hydrogen.

Pre-heated gas (N2, etc.) Gas Flow

Development of high strength coke with feeding of reformed COG (sub-project 3).

Evaluation of balances of energy and CO2 for an entire steelworks.

Reformed COG

・Clarification of optimal injecting conditions of reformed COG (RCOG).

・Model experiments

・Simulation

・Operation design model for RCOG usage based on the heat and mass balance model.

・Reviewing previous knowledge regarding blast furnace operations with high hydrogen reduction.

• Quantification of results of reduction in carbon supply.

・Quantification of improved reducibility of iron ore when feeding reformed COG.

・Evaluation of effects of accompanying reactions under hydrogen-co-existent gas conditions.

Combustion simulation of tuyere raceways under hydrogen co-existence.

Temperature Decrease

Sinter Degradation

Reduction Promotion

<<Technologies to utilize hydrogen for iron ore reduction>>

11Blast Furnace Inner Reaction Simulator

Characteristics of BIS furnace

・ Pseudo-counter flow moving bed ・ Possible to simulate endothermic

reaction associated with gasification and hydrogen reduction, as well as heat exchange.

Evaluation of reaction in blast furnace

[ Adiabatic ]

Coke

Coke

Sinter

Sinter Normal Coke C50% + Iron-coke C50%

Adiabatic control

Coke

Coke

Sinter

Sinter

Coke

Coke

Sinter

Sinter

Bosh gasExperiment under bosh gas conditions adjusted to hydrogensupply conditions

Heating at 100℃ to prevent condensation of water

12BIS Experimental Results on Iron Ore Reduction

40

50

60

70

80

0 5 10 15

水素還元率 (%)

～ 1050 ℃

300Nm3/thm

Reduction rate up to 1050℃

increases by feeding reformed COG

into the shaft.

Possibilities are :

1)indirect H2 reduction rate

increased,

2)direct reduction rate by water gas

reaction (C+H2O=CO+H2) increased.

Increase in indirect reduction

indicates the possibility of the effect

of H2 reduction.

Increment by indirect reduction

Increment by direct reduction

Slope assumed for simple hydrogen reduction with reformed COG injection

Experimental results with BIS

Reformed COG feeding rate Nm³/t-hm 0 200 300 Solution loss (up to 1050°C) kg/t-hm 54.5 69.9 83.2 Total reduction rate (up to 1050°C) % 49 63.7 72.8

Direct reduction % 16.6 21.2 25.3Indirect reduction % 32.5 42.5 47.6

Tota

l R

eduction R

ate

(%)

Hydrogen Reduction Rate (%)

200Nm3/thm

13Observed Microstructures of Sintered Ore

Reduction degree of the high temperature part of the *sintered ore after reduction with the BIS furnace improved by injection of reformed COG.

* Reduction experiments stopped before completion.

Metal (white particles) Void (black area)Unreduced iron (gray area)

Peripheral area of sintered ore

Inner area of sintered ore

14Sub-Project 2

現行COG

炭化水素 (メタン等 )一酸化炭素、等

増幅水素（顕熱相当分）

水素増幅(ﾄﾞﾗｲｶﾞｽ化)

一酸化炭素

残存炭化水素、等

タール・軽油

COG 顕熱（水蒸気）

増幅水素（タール・軽油

転換分）

触媒化学反応場

水素 水素

水素H2 enrichment concept

H2 reduction process flow

Coke Oven Gas

H2 enrich. tech

Coke OvensCoke

Waste heat

Blast furnace

H2 reduction

of iron ore

Catalytic chemical reaction

H2

H2

H2

(Sensible heat)

Enriched H2(derived from sensible heat)

Hydrocarbons

(methane, etc.)

CO, etc

CO, Residual

hydrocarbons

, etc.

COGsensible heat(water vapor)

H2 enrichment (dried gas)

Coke Oven Gas

Enriched H2(converted from tar and light oil)

Tar, light oilHot metal

Hydrogen concentration:55%→63~67%

H2 gas volume : to be doubled.

<<Technologies to reform COG through the amplification of hydrogen>>

15Development of Technologies to Dry and Hydrogen Enriched COG

Reaction rate was successfully doubled through the improvement of the catalyst.

Improvement of reaction rate

Methyl naphthalene 1st

generation Ni catalyst.Methyl naphthalene 2nd generation Ni catalyst.

Methyl naphthalene 3rd

generation Ni catalyst .

16Sub-Project 3

HPC (High Performance Caking Additive )Blended coal

CokingMelting

High strength coke

Experimentally produced coke with HPC (300 kg)

•Possible to increase coke strength without relying on blending coking.

•Enhanced compatibility with raw materials at the time when hydrogen reduction is put in practical use.

・HPC starts softening and melting at low temperatures below 300 oC.・HPC packs coal particles effectively by filling gaps in between.=> It is possible to produce a high strength coke with HPC.

<<Technologies to produce optimum coke for hydrogen reduction of iron ore>>

17Enhancement of Coke Strength with HPC

● Experimental results（Base-1 blending）

HPC additionBase-1 blendingCoal packing density > 800kg/m3

84

86

88

90

700 750

DI

(

%)

150

15

800 850

Packing density (kg/m3, d.b.)

HPC 0%

HPC 5% addition

Base -1

D

C

B

A

Base-1

D

C

B

A

HPC 5% addition

Base-1 + HPC

C

B

(15%)

(26%)

(34%)

(25%)

(29%)

(26%)

(15%)

(25%)

Target coke strength :DI150

15≧88% achieved.

Strongly-caking coal

Semi coking coal

Non or slightly-caking coal

Base-1: Coking coal rich (normal)

18Sub-Project 4

・Development of technology and equipment of a very large amount of CO2 capture (8 million ton-workshop → 3.2 million ton-CO2 generation)

・Utilization of low quality energy in workshop.

CO2 Emission CO2 Capture CO2 Storage

40~50% 50~60%

60~70% 30~40%

Cost CutEvaluation/Standard

Equipment

Storage Cost

Problem

<<Technologies to capture – separate and recover – CO2 from BFG>>

19Technical Subject of Chemical CO2 Capture

Relative Cost (%)

2.52.0

100

3.0

Recovery Heat of Chemical Absorbents （GJ/t-CO2）

Optimization of total process including steelmaking process

Increase in wasted heat usage

・High performance absorbent・Improvement of chemical absorption process

Conventional Method

Target of Development

Target Cost

90

80

70

60

50

40

30

20Collaboration Scheme to Develop New Chemical Absorbents

Development of new chemical absorbents

Quantum chemicalcalculations

Design new amine Compounds.

Synthesize new aminesDesign absorbentsEvaluate the performance

Suggest new amine compounds

ExperimentsChemoinformatics

Evaluation at Test Plants (NSSNG)

CAT1 (1t-CO2/d） CAT30 (30t-CO2/d）

Industrial application

StripperAbsorber

Reboiler

Evaluation of new absorbents Evaluation of chemical plant properties

21Developed Progress and Target

1.5

2

2.5

3

3.5

0.1 1 10 100 1000 10000

Heat Consumption(GJ/ton

-

CO2)

Plant Scale (ton/day)

CAT -1 CAT -30 Commercial3000

RITE-5C

RN-1

RN-3

RN-1

RN-3 RN-3

RN-1

Measured

COURSE50Target

Development until present work

Further development △=0.3

Target Line

Heat Consu

mption o

f Abso

rbent(

GJ/

t)

22Concept of Two-staged PSA for BFG

Selection of adsorbent

PSA lab. testsAdsorption simulation

Bench scale PSAoperation

・Operating conditions

・Design bench scale test equipment

・Cost reduction

・Establish adsorption model

・Compare with lab. tests

Utilitiessimulation

Concretize industrial processClarify & reduce recovery cost

Data accumulation for Scaling up

・Data matching

incorporation

Gas flowsimulation

Outline of technology developmentNon combustible gases

Combustible gases

View of ASCOA-3

23Test Operation Results in ASCOA-3

Process targets were achieved during test operation period.

0.0

0.5

1.0

1.5

2.0

2.5

3.0

3.5

4.0

4.5

5.0

3/8

3/11

3/11

3/14

3/15

3/16

3/17

3/18

3/22

3/23

3/24

CO

2Recove

ry (

t/day)

0

10

20

30

40

50

60

70

80

90

100

CO

2Purity

, Recove

ry R

atio(%)

Recovery target:3t/day

Purity target:90%

Recovery ratio target 80%

Recovery Ratio

Purity

Achieve 3 targets

Max. Recovery:4.3t/day

Max. Purity:99.5%

Recovery

24Sub-Project 5

COG sensible heat

Hot stove gas

BOF gas sensible heat

BF slag sensible heat Steelmaking slag sensible heat

Slag granulation tank waterCOG ammonia water

HDG NOF

HDG RF

CAPL NOF

Plate Mill RF

HRM RFMain exhaust gas after heat recovery

Main exhaust gasCooler exhaust gas

0

200

400

600

800

1000

1200

1400

1600

1800

Tem

pera

ture

(℃

)

Sintering process Coke plant BF Steelmaking Rolling exhaust gas

３０００２０００

Calorie (TJ/year) ４００

０

Unstable generation rate

Coke oven flue gas after heat recovery

CAPL RF

Model steelworks 8 million ton

Waste heat of from medium to low temperatures / molten materials at high temperatures difficult to recover economically currently unused

<<Technologies to recover unused sensible/wasted heat in steelworks>>

25Sensible Heat Recovery from Slag

Slag Plates

Apron Conveyer

Cooling Roll

Tilting Equipment

Slag Ladle

Hot Crusher

Cyclone

Blower

Bucket Elevator

Slag Heat Recovery Chamber

Mist Spray Nozzle

Slag after HeatRecovery

26Technology Development for Sensible Heat Recovery from Steelmaking Slag

ConveyerConveyer Cooling RollCooling RollTroughTrough

Slag LadleSlag Ladle

Target (after roll forming)for heat recovery ratio ≧ 30% Thickness of Slag = 7~8mmTemperature of Slag ≧1000℃

Target (after roll forming)for heat recovery ratio ≧ 30% Thickness of Slag = 7~8mmTemperature of Slag ≧1000℃

27Contents

1. About COURSE50 Project

2. Current status of COURSE50

3. Test operation trial at experimental blast furnace

28Experimental Blast Furnace Test

【Purpose】・ Comprehensive evaluation of COURSE50 hydrogen reduction.

【Targets】・ Evaluation of the potential in replacing coke and coal as

reducing agents in the blast furnace with high H2

containing gas as reformed COG (RCOG)and COG.

・ Evaluation of effects of hot top gas injection on temperature of upper part of the blast furnace and on sinterdisintegration.

29LKAB’s Experimental Blast Furnace

Figures are quoed from Swerea/MEFOS and LKAB brochure

30LKAB’s EBF Trial

【Probing, Sampling】

Basket Sample

Raceway

【Reformed COG Injection】

【COG Injection】

Upper Probe

Vertical Probe

【Operational Data, Analyzing】

Lower Probe

Inclined Probe

Ferrous Material：Sinter70%-Pellet 30%Coke、PC：from SSAB

【Hot Top Gas Injection】

Schedule：16th April ～11th May, 2012Schedule：16th April ～11th May, 2012

Blast Tuyere

Upper shaft Tuyere

Lower Shaft Tuyere

Figures are quoed from Swerea/MEFOS and LKAB brochure

31Operation Conditions (Gas Injection)

Synthetic COG and RCOG were mixed from pure gases to control constant and accurate gas composition through the trial operation for the main purpose of evaluating the effects of H2 reaction.

Synthetic COG and RCOG were mixed from pure gases to control constant and accurate gas composition through the trial operation for the main purpose of evaluating the effects of H2 reaction.

200Nm3/thm (300Nm3/h)

77.9%H2-10%CO-12.1%N2

(78ppmH2S)

Composition Injection Position Injection RateInjection

Temperature

COG57%H2+31.3%CH4+11.7

%N2

Blast Tuyers (3)100Nm3/thm (150Nm3/h)

RT

RCOG

77.9%H2-22.1%N2

Lower Shaft Tuyeres (3)

150Nm3/thm (225Nm3/h)

200Nm3/thm (300Nm3/h) 770℃

HTGCombusted BFG

（CO/(CO+CO2)>0.05）

Upper Shaft Tuyeres (3)

100Nm3/t 800℃

32RCOG Heating Apparatus

RCOG out（925℃）

Hot Gas in （1000℃）

Hot Gas out（824℃）

COG out（760℃）

Pre-Heater

EBF

Main-Heater

Tube Basket

Bustle Pipe

COG in（RT）

RCOG was heated up to 800°C through a counter-current heat exchanger and injected to EBF.

RCOG was heated up to 800°C through a counter-current heat exchanger and injected to EBF.

33RCOG Heating Apparatus

EBF

COG Heating App.

Lower Tuyere

RCOG Outlet

Pre-Heater

Main-Heater

34Hot Top Gas Injection Apparatus

Gas Cleaner

CompressorBFG

Oxygen and Nitrogen Supply

Top Gas

Oxygen Enriched Air+ Nitrogen

Upper Tuyeres

Burners

Figures are quoed from Swerea/MEFOS and LKAB brochure

35Overview of Operation Trial

480500520

540

560

050100150200250

InputC COG RCOG

CR+PCR(kg/t)CR(kg/t)

Top Gas Temp.(℃）

Blast Volume(Nm3/hr)

ηCO(%)

4/164/184/204/224/244/264/284/30 5/2 5/4 5/6 5/8 5/105/12

150200250

300

350TGTCalculated TGT

0500

1000

1500

2000

050100

150

200

BVO2 Enrc.

3034384246

ηCO

400450500550600650

0

50

100

150

CR+PCR CR PCR

O2

Enrichment(Nm3/hr)

PCR(kg/t)

Start COG Inj. Start

RCOG Inj.Start

InputC(kg/t)

COGRCOG

(Nm3/t)

HTG Inj. start

HTG Inj. start

36Summary of EBF Trial

41.540.742.2%ηCO

34.642.238.2%ηH2

9729821057Nm3/thmBlast Air Volume

145114141446℃Hot Metal Temperature

224322022218℃Theoretical Flame Temp.

23.224.023.4g/Nm3Blast Moisture

112411261129℃Blast Temperature

6.97.85.9%O2 Enrichment

14900kg/thmRCOG injection

0990kg/thmCOG injection

563555580kg/thmRAR (CR+PCR)

128123130kg/thmPC Rate

435432450kg/thmCoke Rate

36.336.536.0t/dProduction

RCOG Inj.COG Inj.Base

37Reduction under COG and RCOG Injection

・ H2 reduction increased while C direct reduction and CO reduction decreased in both injection periods because of the fast reaction rate of H2 reduction

・ Decrease in C direct reduction, which is a huge endothermic reaction is the main reason of reduction in carbon input.

・ H2 reduction increased while C direct reduction and CO reduction decreased in both injection periods because of the fast reaction rate of H2 reduction

・ Decrease in C direct reduction, which is a huge endothermic reaction is the main reason of reduction in carbon input.

0

50

100

Base COGInjection

RCOGInjection

Fra

ction（%）

CO Indirect Reduction

H2 Indirect Reduction

Carbon Direct Reduction

-1500

-1000

-500

0

500

Heat of Reduction （

MJ/

t）

Base COGInjection

RCOGInjection

Exothermic

Endothermic

38H2 Concentration Distribution during COG/RCOG Injection

RCOG

COG

Lower Probe

・ Hydrogen concentration distribution during COG injection period was uniformly higher than the base period. => Gas from blast tuyere goes into the furnace through raceway

・ Hydrogen concentration only near the shaft tuyere was high duringRCOG injection period.=> Gas from shaft immediately reduces iron ore, small penetration depth

・ Hydrogen concentration distribution during COG injection period was uniformly higher than the base period. => Gas from blast tuyere goes into the furnace through raceway

・ Hydrogen concentration only near the shaft tuyere was high duringRCOG injection period.=> Gas from shaft immediately reduces iron ore, small penetration depth

EBF figure iquoted from Swerea/MEFOS and LKAB brochure

RCOG

COG

39Vertical Distribution of Reduction Degree

0

50

100

2.0 3.0 4.0 5.0 6.0

Distance from Stock Level (m)

Reduction D

egre

e (

%)

Blast TuyereLower Shaft Tuyere

Reference (no injection)

This study (RCOG)

←furnace top

40Change in Ratio of Indirect, Direct and H2 Reduction with BF Operation Conditions

100

20

40

50

80

Indire

ct C

O red

uctio

n ra

tio (

%)

0

70

90 10

30

0102030

Direct reduction ratio (%)

Hydrogen reduction ratio (%

)

H2 Reduction (BF)

COG injection (BF)

TGR(N2 free BF)

CO ReductionPromotion

(BF)

60

504050

Base

41Effect of HTG Injection on Upper Part Temperature

Hot Top Gas (800℃)

Vertical Probe

COG Injection

Dis

tance fro

mSto

ck

Leve

l (m

)

-4.0

-3.0

-2.0

-1.0

0

400 600 800 1000 1200

Detected Temperature by Vertical Probe (℃)

Before HTG Injection

After HTG Injection

290

270

250

230

210

190

170

150

Top G

as

Tem

pera

ture

(℃

)

280

240

200

160

120

80

40

00 2 4 6 8 10

HTG Inje

ction V

olu

me

(Nm

3/th

m)

Time (hr)

EBF figure quoted from Swerea/MEFOS and LKAB brochure

HTG Started

42Change in Sinter Particle Fraction in Shaft

Base

RCOGInjection

RCOG Injection

COG Injection + HTG

RCOG Injection + HTG

COGInjection

-6.3mm fraction at Ore Bin-6.3mm fraction at Ore Bin

COGInjection

-5mm fraction (%)-5mm fraction (%)

Dis

tance fro

m S

tock

Leve

l (m

)

Dis

tance fro

m S

tock

Leve

l (m

)

43Summary

1) Improvement of the reduction of iron ore by hydrogen injection has been

verified by experimental BF test with hydrogen enriched reformed COG

shaft injection and COG injection from ordinary tuyere.

2) Bench scale test results of COG reforming technologies (hydrogen

enrichment) indicate the possibility of making hydrogen content double.

3) Technology of producing high-strength coke stably by adding HPC

(High Performance Caking additive) has been prospective.

4) The results of both chemical absorption and physical adsorption bench

scale test indicate the world’s lowest level of energy consumption to

capture CO2.

5) The results of studies on various promising waste heat recovery

technologies as well as an inventory of unused waste heat indicate the

possibility of satisfying the energy demand for CO2 capture.

44Timetable for Industrialization

2000 2002 2004 2006 2008 2010 2012 2015 2020 2030 2050 2100

Post Post -- COURSE50COURSE50

Green electricity & Green hydrogen production technologies

CO2 Storage & Monitoring

COCS Project **(2001-2008)

JHFC Project *(2001-)

COG H2 enrichment Project

(2003-2006)

Partial substitution of carbon by hydrogen

CO2 capturefrom BFG

Hydrogen

Steelmaking

Intern’l collaboration

Development of fundamental technologies

Establishment of infrastructure

PhasePhaseⅠⅠ（Step 1）

Industrialization

PhasePhaseⅠⅠ（Step 2）

PhasePhaseⅡⅡ

Mini

exp. BF

EBF + PartiallyIndustrial

Matching between capture equipment and mini exp. BF

Integrated operation of semi-industrial capture equipment (several hundred t-CO2/D) with exp. BFULCOS (2004-)

1st industrialization by ca. 2030 <Prerequisite> CO2 storage available Economic reasonability

* Japan Hydrogen & Fuel Cell Demo. Project. * *Cost-saving CO2 Capture System

Verification

Hydrogen reduction

CO2 capture

Industrialization

Reduction fundamentalsOptimized gas injectionBench-scale H2

enrichment

Process evaluation plantTotal evaluation

incorporating mid - low temperature waste heat recovery

45

Acknowledgement

This study was carried out as a national project for development of technologies for environmentally harmonized steelmaking process, ‘COURSE50’supported by the New Energy and industrial Technology Development Organization (NEDO).

46

THANK YOU FOR YOUR ATTENTION !