Development on Advanced High-Temperature Air Combustion … · 2018. 8. 22. · High-Temperature Air Combustion Technology for Steam Reforming Process ... (CH4 -> C+2H2) Gas temperature

2002 AMMONIA TECHNICAL MANUAL

Development on Advanced High-Temperature Air

Combustion Technology for Steam Reforming Process In 1999, a national project on the development of an advanced steam

reformer was initiated. The project�s objective is to break through design constraints experienced on conventional reformers. This paper

describes major results of the project up to March 2002.

Takaaki Mohri, Toshiaki Yoshioka, Yoshikazu Hozumi and Tetsu Shiozaki Chiyoda Corporation

Toshiaki Hasegawa and Susumu Mochida Nippon Furnace Kogyo Kaisha, Ltd

Shigenao Maruyama, Dr.Eng. Tohoku University

Introduction

evelopment on an advanced steam re-former incorporating high-temperature air combustion technology is one of the pro-

ject targets in the national project (officially called Hi-COT project) of Japan subsidized by the Ministry of Economy, Trade and Industry (METI), entrusted by New Energy and Industrial Technology Development Organization (NEDO), and re-entrusted by Energy Con-servation Center, Japan (ECCJ). The project is being carried out jointly by Chiyoda Corporation (Chiyoda) and Nippon Furnace Kogyo Kaisha, Ltd (NFK) from fiscal year 1999 to 2003.

The high-temperature air combustion technology is a combustion technology utilizing air preheated by recov-

ered heat from flue gas to temperatures of 800°C and higher, and holds great potential for realizing the energy efficient and ecological combustion systems of the future.

Figure 1 shows the concept of combustion-mode re-gions related to diluted air temperature and oxygen con-tent in the air. It was confirmed that when combustion air temperature is increased at lean oxygen content, sta-ble combustion is obtained. This combustion-mode zone is categorized inovated zone III as new combustion-mode region. It was also confirmed that this zone III gives innovated new combustion realizing super low NOx emission, even though the combustion air tempera-ture is extremely high as shown in Figure 2.

In addition, uniform temperature distribution was found in the combustion chamber as shown in Figure 3.

D

AMMONIA TECHNICAL MANUAL 2002

III. New Combustion Region(High-Temperature Air Combustion)

II. Hot flame region

Unstable Combustion Region

I. Ordinary Flame Region(Conventional Combustion)

Oxygen Concentration in Diluted Air [%]

Dilu

ted

Air

Tem

pera

ture

[deg

.C]

21 10.5

500

1000

Figure 1. Diluted Air Temperature and Combustion Region (Concept)

High-temperature AirCombustion

Conventional Combustion

Combustion Air Temperature [deg.C]

NO

x[pp

m](c

orre

cted

to 0

% O

2)

0

400

800

1200

1600

400 800 1200

Figure 2. NOx Emission of High Temperature Air Combustion

Figure 3. Measured Temperature Profile affected by Diluted Air Temperature and its O2 Concentration

In contrast with an ordinary combustion shown in Fig. 3(a), when increasing the air temperature up to 1,200°C at lean oxygen of 4%, the peak flame temperature mostly disappeared as shown in Figure 3(b).

The effectiveness of the advanced high-temperature air combustion technology for combustion performance, such as energy saving, CO2 reduction, and reduced emission of NOx, was recognized during earlier phase of the research and development of industrial furnace entrusted by NEDO(project completion was 1999). The purpose of the HiCOT project is to apply the advantages of the technology for industrial combustion equipment consuming large energy in various industrial fields.

Comprehensive studies are also being carried out on pulverized coal combustion boilers and the waste incin-eration process as well as the steam reforming process.

Steam Reforming Process

Process

The steam reforming process is applied in Hydro-gen, Ammonia, Methanol, Direct reduction and other Synthesis Gas plants.

The steam reformer is the heart of the plant and catalytically reforms feed gas consisting of hydrocarbon and steam to H2 and CO at high temperature condition

(a) Tair=35ºC, O2=21% (b) Tair=1200ºC, O2=4%


of around 900°C. The reforming heat duty requires large heat input and reaction tubes are directly heated by burners.

Structure of Steam Reformer and Carbon Formation

The feed gas of hydrocarbon and steam is supplied to the reaction tubes at 500°C~650°C and heated up to around 900 °C by the burners.

There are two carbon formation zones in the reaction tube, one is the BOUDOUARD REACTION ZONE

where carbon will be formed from CO at lower tempera-tures, and the other is METHANE DECOMPOSION ZONE at higher temperatures as shown in Figure 4. The process gas should be heated such that carbon formation along the tube length is prevented.

Figure 5 shows a typical steam reformer structure for each process licenser. Each structure type has same design concept with the reaction tubes installed in a single row of tubes in the radiant chamber and with the tubes heated from both side of the tubes. This is because that heating profile for the tubes should be uniform as much as possi-ble to avoid carbon formation inside of the tubes.

Boudouard Reaction Range (2CO -> C+CO2)

Hydrocarbon, Methane Decomposed Range (CH4 -> C+2H2)

Gas temperature

Rea

ctio

n tu

be

Inlet

Outlet

Ideal profile

Figure 4. Carbon Formation Zone in Reaction Tube

Figure 5. Typical Steam Reformer Structure

Down firing type Radiant wall type Terrace wall type Up firing type

Convection Section

Burner

Burner

Burner

Tubes

Tubes


Outline of Research and Development

Objective of the Research and Development

The research is expected to clarify the effect of high-temperature air combustion and heat transfer char-acteristics on a steam reformer. Essential design factors, in particular, burner location, tube pitch, and other as-pects of geometric design will be studied under high-temperature air combustion. In addition, acquired opera-tional data will be analyzed and accumulated in a data base and these essential design factors for those charac-teristics will be evaluated.

Based on technical study and evaluation of the data, a practical 3 Dimensional (3D) design simulator, together with performance control technology will be established.

Overall Schedule

Figure 6 shows the overall schedule of the research. The research was begun in fiscal year 1999 and the plan is to complete the research in fiscal year 2002.

The research program consists of two main issues. One is to design and construct a test facility for the re-search. The other is the development of a 3D design simulator for steam reformer.

Design, Construction, and Operation of the Test Facility. As for the test facility, basic and detailed en-gineering, and procurement of material for the test facil-ity was completed in fiscal year 2000, and the construc-tion begun in fiscal year 2001. All of the construction work was completed in November 2001.

Operation of the test facility was started in Decem-ber 2001, and the operating data will be obtained and analyzed in fiscal years 2002 and 2003.

Development of 3D Design Simulator. As the first step of the development work for the 3D design simulator, the existing 3D simulator and 2D reforming reaction simulator were integrated into phase-I 3D de-sign simulator(Phase I simulator) in fiscal year 1999. In fiscal year 2000, the Phase-I simulator was developed reflecting high-temperature air combustion technology after evaluating several combustion models grading jointly discussed by a technical committee organized in the HiCOT project. The up-grading of the Phase-I simu-lator to Phase II to incorporate high-temperature com-bustion air was approximately 90% complete on March 2002. The Phase II simulator will be proved and/or cor-rected through the analysis of acquired operational data in fiscal year 2002, and finalized in fiscal year 2003.

Interim Report (1999~2002)

Test Facility

Process Design. Figure 7 shows the process flow for the test facility.

The test facility consists of a desulfurization unit, a steam reforming unit, and a steam generation unit. The town gas is mixed with process steam after being desul-furized in the desulfurization unit and the mixed process gas is fed to the reaction tubes at about 500°C. The process gas is reformed in the reaction tubes to H2 and CO plus remaining the CH4 and H2O at 825°C. Re-formed gas is cooled down to 200°C by a heat ex-changer located down stream of the steam reformer, and exhausted to atmosphere through flare stack.

The test steam reformer has regenerative burners and high-temperature air combustion is performed. Combustion air is supplied for the regenerative burners by a forced draft fan (FDF) and heated up to around 1,000°C through heat accumulators installed inside of the burner body. The flue gas, after heat-recovery is ex-hausted by the induced draft fan (IDF) to atmosphere.

Regenerative Burner. Figure 8 shows continuos firing type regenerative burner to be mounted on the test reformer. The burner has 4 sets of heat accumulator cas-sette in the burner body. Fuel gas is supplied to a center gun. While 3 heat accumulator cassettes induce flue gas in the cassette for heating, the remaining heat accumula-tor cassette exhausts combustion air heated to around 1,000°C. The combustion air is switched to the next cassette at 5 seconds interval by means of a switching air valve provided for each heat accumulator cassette.

Preliminary Combustion Test

Objectives. The flame from high-temperature air combustion using gaseous fuel becomes mostly invisible and the flame volume where the combustion reaction is taking place expands in the combustion chamber, show-ing uniform temperature distribution.

It is essential for the development to establish an ac-curate flame detection method for effective combustion control in the steam reformer.

A preliminarily combustion test was programmed to develop a method and a probe for flame detection appli-cable to bench-scale flame and actual-scale flame re-spectively before installing the regenerative burners for the test steam reformer.

Bench Scale Test. A small sized flame, utilizing high-temperature air combustion was investigated to


E

Development of SecondarySimulator reflecting High-Temp. Air Combustion andInstalled in the PrimarySimulatorcombustion newly developed

Development of PrimarySimulator for DesignigSteam Reformer notreflecting High-Temp. Air Combustion

Simulation of Actual operationData and Modification of theSimulator, if necessary

Basic and Detail Design of TestOperation and Acquisition

of Data

Analysis of

Operation data

ConstructionFabrication andPurchasing Material

Preliminary Combustion Test

Finalizing Test Procedure,e.g., location of Burnerand tube pitch

Completion of Design Simulator

for Steam Reformer for High-Temp

Air Combustion

Design and Construction

of Commercial Scale

Reformer

1999 20032000 20022001

1) Design, Constuction and Operation of Test Unit

EProcess Design and

Equipment Design

ETechnical Study for

@Test Procedure

Purchase order equipment

and material

ERelation between Ion and High Temp. Air

@Combustion

ETest of sampling probe for Ion

2) Development of Simulator

ECombining exist'g reforming@program and combustion/@heat transfer programEInvestigation of High-Temp.@of the reaction Air@Combustion and kinetics

EStudy and program@High-Temp. Air CombustionEModifining of Radiative heat@transfer program under@collaboration agreement@with Tohoku Univ.

EHeat transfer simulation

EVerification of Simulator

Figure 6. 5 Year Plan for Development of Advanced High-Temperature Air Combustion Technology for Reforming Reaction Process

F.D.FanF.D.FanF.D.FanF.D.Fan

Test Reformer

Burner

H2

IW

HC

FG Valve

Steam

I.D.Fan

Heat exchanger

Boiler

Desulfurization unit

To Flare Stack

Flue gas escape duct Flue

gas duct

Reaction tubes

Figure 7. Process Flow for Test Facility


Figure 8. Continuous Fuel Feeding Type Regenerative Burner

L L P = 6 8 L

Preheated Air

235

130 45

Fuel Gas

Figure 9. Measurement Position of Ionization Probe in the Bench-Scale Combustion Chamber

confirm the performance of a probe which detects the existence of ions in the flame.

Figure 9 shows the measured points of ion on the bench scale combustion test.

Figure 12 shows the results of the measurements on ion detection in the flame, which were obtained for the combustion tests using room temperature air and pre-heated air of 1,000°C respectively. It was clearly con-firmed that the ionization probe can detect an existence of the flame as shown in Figure 12(b) in spite of the fact that the flame becomes invisible with the high-temperature air combustion.

Actual Scale Test. An actual flame formed by the regenerative burners, which will be installed for the real test steam reformer, was also investigated to establish the flame detection method. The burners were installed on the existing water cooled tubular furnace which was con-structed at the previous NEDO project in 1996.

Figure 11 shows the water cooled tubular furnace for the full scale test.

Figure 12 shows an over view of the combustion condition of the regenerative burner. Yellowish bright flame was found as shown in Fig. 12(a) at an air tem-perature of 600°C and air ratio of 2.0, and an almost in-

visible flame was observed as shown in Fig. 12(b) at the air temperature of 1,080°C and air ratio of 1.3.

The area shown in Figure 13 was measured with the ionization probe and a successful detection of ion in the flame was made.

The flue gas temperature distribution in the furnace as shown in Figure 14, was also measured for the same area as the ion detection was made.

It is understood that the flue gas temperature is uni-formly distributed, even though the upper portion shows a slightly higher temperature tendency. Summarizing the preliminary combustion test, it was confirmed that the ionization probe is effective for the detection of invisible high-temperature air combustion flames.

Development of 3D Design Simulator

Integration of the Simulator for Combustion, Heat Transfer and Reforming Reaction. The existing 3D simulator for analyzing the combustion reaction and heat transfer through flow dynamics was integrated with the chemical reforming reaction simulator. The inte-grated simulator can totally analyze heat transfer from the burner flame to the process fluid considering geo-

Preheated Air

Flue Gas

Flue Gas Air

Switching Valve

Fuel


Figure 10. Ion Measurement Result from (a) Normal Combustion and (b) High Temperature Air Combustion metrical condition such as location of burner, tube di-ameter, tube length, tube pitch and so on. The 3D simu-lator will be reviewed and revised to be able to analyze the combustion reaction and heat transfer under the high-temperature air combustion based on actual ex-perimental data. A prototype of the 3D simulator was completed by the end of fiscal year 2001 and the final simulator, after reflecting all of experimental data, will be completed in fiscal year 2002 or 2003.

Study of Combustion Model. The following com-bustion model was studied for the high-temperature air combustion.

• Mixed is Burnt Model (MIB). The model

is structured assuming that the reaction time is extremely short compaired with the mixing time of fuel and air, therefore the reaction rate of combustion is assumed to be infinitely fast when fuel and air is mixed, applying the PDF (Probability Den-sity Function) for the simulation.

However, it is uncertain whether PDF will apply for the high-temperature air combustion, since the PDF was experien-tially obtained based on normal combustion reaction.

• Eddy Break Up Model (EBU). This model is structured assuming that the com-

bustion reaction takes place at the boundary between fuel and air, and the boundary consist from small eddy and turbulent flow. So the combustion reaction rate will be de-cided by the disappearring rate of small ed-dies in the turbulent flow.

However, it is also believed that the theory is not applicable for the high-temperature air combustion, since the com-bustion rate for the high-temperature air combustion is decided only by turbulent flow conditions, with no effect from the temperature of the combustion.

• Jones 4 Step Chemical Reaction (J4C). Actual combustion reaction consists of more than hundred kinds of unit reaction. It is impossible to take all of the reactions into the simulator, and it is assumed that the reaction rate is effected by a typical 4 step simple combustion reaction. The com-bustion rate is decided by the formula of Arrhenius considering reaction temperature and concentration of reactants. It is consid-ered that J4C is the most applicable model for the high-temperature air combustion, because of these reasons.

x [m m ]20 400 60 80 100-20-40-60-80

h=235

h=130

h=45

h=0

ProbeOutput[m

V]

0

50

100

0

50

100

0

50

100

O2% in air: 21% Air Temp.: 20deg.C Fuel: LPG Firing Rate: 1.4kW

(a)

x [m m ]20 400 60 80 100-20-40-60-80

h=235

h=130

h=45

h=0

ProbeOutput[mV]

0

50

100

0

50

100

0

50

100

O2% in air: 3% Air Temp.:1000deg.C Fuel:LPG Firing Rate:1.4kW

(b)


Figure 11. Diagram of Water Cooled Tubular Furnace and Pictures of the Furnace

Comparison with Pre-Combustion Firing Test. Calculated results from the 3D simulator using the EBU model and J4C were compared with experimental data obtained at the pre-combustion test as shown in Figure 15 and 16. Figure 15 shows that the pre-combustion test was performed at preheated air tem-perature of 1,300K (1,027°C) and reducing the O2 from 21% to 4% in the air.

A peak flame temperature of 1588K (1,315°C) at 4% O2 is calculated by J4C model in contrast with 1,708K (1,435°C) from the EBU model. Also the ambi-ent temperature of the inside chamber calculated by J4C seems to be lower than what is predicted by the EBU model. In addition, when observing the intermediate product of H2 generated during combustion, the contour of the intermediate product of H2 by the J4C model is almost the same shape as the real flame.

Specification Dimensions: L2m x W1.8m x H2m Firing rate: Max. 600kW Volumetric heat release: 75kW/m3 Max. in furnace temp.: 1100deg.C Combustion control: Manual Heated object: Water-cooled tube 1.5in x 2m x 19 tubes


Figure 12. Flame picture of High Temperature Air Combustion, (a) Start-Up Condition, and (b) Operating Condition

Test Furnace

Firing Rate:290kW

Air Ratio:1.4

Fuel:Natural Gas

1000

300750

A

Figure 13. Measured Reaction Zone by Ionization Probe

Test Furnace

Firing Rate:290kWAir Ratio:1.4Fuel:Natural Gas

A

1000

300

750

Figure 14. Measured Temperature Distribution by Thermocouple

(a) 600 ℃ λ =2.0 Firing Rate:105 kW

(b) 1080℃ λ =1.3 Firing Rate:145kW


(Air preheating temperature to 1,300K [1,027°C])

Figure 15. Comparison of Burnt Models with Burnt Experiment

Oxygen 21vol% Oxygen 4vol%

Laboratory Experiment

Eddy break up Model Temperature Distribution[K]

Jones 4 Steps Model Temperature Distribution[K]

Jones 4 Steps Model Intermediate Product(H2) Mass Fraction[-]


The Flame Figure is varied by Air Preheating Temperature. (Mass Fraction of Intermediate Product (H2) at Jones 4 Steps Model [-])

Figure 16. Parameter Study of HiCOT Flame Figure 16 shows the variation of the calculated in-

termediate product contour of H2 when changing pre-heated air temperature from 1,000K (727°C) to 1,500K (1,227°C). It is found that there is tendency of the flame to lift at the preheated air temperatures of less than 1,100K (827°C). This phenomenon is also consistent with the real flame condition.

In view of these comparison results, it is understood that the J4C model is applicable for the high-temperature air combustion analysis.

Simulation for Test Steam Reformer. The 3D model was made by meshing each component as small as possible , and resulted in the same shape observed in the test reformer.

Calculated results of tube skin temperature, heat flux, and process gas temperature are shown in Figure 17, and of process gas contents such as H2 and CH4 are shown in Figure 18 by both MIB and J4C respectively.

Developing Technology Aspects

Advanced Steam Reformer

The critical feature of the high-temperature air com-bustion technology is considered to be uniform tempera-ture distribution in the combustion chamber under ex-panded flame combustion at lean oxygen combustion.

1,000K(727°C) 1,100K(827°C) 1,200K(927°C)

1,300K(1,027°C) 1,400K(1,127°C) 1,500K(1,227°C)

Air Preheating Temperature


Figure 17. Mean Tube Skin Temp. & Heat Flux of the Process Reaction Tube①①①①

Figure 18. Process Flow Mole Fraction in the Process Reaction Tube①①①①

From the technical view point, there is a possibility

to innovate the conventional design concept for both process configuration and steam reformer structure.

Figure 19 shows a conventional radiant wall type steam reformer for a 1000ton/day Ammonia plant. The reaction tubes are installed in the radiant cell in single row tube arrangement and uniformly heated by radiant wall burners from both side.

The flame of the burner is formed along the refrac-tory lining wall and no flame impingement occurs.

The waste heat recovery section is located on the top of the radiant section and the combustion flue gas is ex-hausted to atmosphere through the IDF.

As for the advanced steam reformer, it is found that no waste heat recovery section is required for the steam reformer, since the waste heat of the flue gas is heat-recovered by the heat accumulator installed in the burner body.

Also, as another feature of the advanced steam re-former, an innovative tube arrangement will be consid-ered under the uniform heat distribution of the flame of the regenerative burner.


31,6

00

15,4008,700

Waste Heat Recovery sect.

Radiant section

Figure 19 Conventional Radiant Wall Type Steam Reformer

These design feature can realize remarkable down sizing of the steam reformer, namely the new steam re-former is expected to take 30−40% less of the plot area and more than 50% less on the total material work vol-ume.

Advanced Hydrogen Plant

A technical study was performed for the design of a Hydrogen plant utilizing advanced steam reformer mounted regenerative burners;

Conventional Hydrogen Plant. A conventional Hydrogen plant applying Pressure Swing Ad-sorber(PSA) unit as the gas purification unit is shown in Figure 20, consisting of a de-sulfurization unit, a steam reformer, a CO converter unit, a PSA unit and a steam generation unit. The required heat for the reforming re-action is provided by the combustion of fuel gas. The available heat from the purge gas from the PSA unit, which is primary fuel of the steam reformer , is only 40% to 70% of the total required heat fired, and it is necessary to supply the remaining heat from the fuel gas from outside of battery limits.

The fuel efficiency of the radiant section is around 50%, and the exit flue gas at 950°C~1,050°C is intro-duced to the convection section to recover the waste heat for process gas preheat, steam generation, boiler feed water preheat and air preheat.

Advanced Hydrogen Plant. The design configu-ration of the advanced Hydrogen plant is shown in Figure 21.

Figure 20. Conventional Hydrogen Plant


Figure 21. Advanced Hydrogen Plant

The process units are basically the same as the con-

ventional one. However, since the regenerative burners are installed for the steam reformer, the waste heat of the exit flue gas from the radiant section is utilized only for preheating its combustion air for the regenerative burners and the convection section can be eliminated.

This new design concept makes it possible not to re-quire any additional fuel gas from outside of the battery limit, since the required heat for the reforming reaction can be supplied only by the purge gas from the PSA unit.

New Process Design for Advanced Hydrogen Plant. The advanced hydrogen plant was designed , studied, and compared with the conventional one at the design conditions of Butane feed and 4,000Nm3/h hy-drogen production as shown below. The calculation re-sults are shown in Table 1.

Design condition: • Process gas feed : Butane • Steam carbon ratio : 3.4 • Hydrogen product : 4,000Nm3/h • Hydrogen purity : 99.99 % • Efficiency of PSA : 82%

Case 1 shows the results of the study applying the regenerative burner for the Hydrogen plant as one ex-ample of advanced Case, Case 2 shows the conventional Hydrogen plant case without an air pre-heater for the steam reformer, and Case 3 shows the conventional Case applying an air pre-heater for the steam reformer.

The total consumption rate of the feed gas and Bu-tane as the fuel gas for Case 1 is minimized compared with Case 2 and Case 3 as shown in Table 1.

This is due to the fact that the required heat for Case 1 can be reduced by increasing the combustion air tem-perature to around 900°C, use of the regenerative burner and maximizing the fuel efficiency of the radiant sec-tion. The fuel consumption rate for Case 1 is approxi-mately 53% lower than that of Case 2.

As for the amount of steam generation for each case, Case 1 becomes the minimum case for steam generation due to the minimized export steam. Case 2 and Case 3 recover the waste heat from the exit flue gas from the radiant section to generate steam in the convection sec-tion. For Case 1, the required process steam is generated at the process waste heat boiler provided downstream of the steam reformer furnace.


Table.1. Comparison of New Process Design with Conventional Design for Hydrogen Plants Case-1 Case-2 Case-3 Unit Example w/o APH w/APH

Process condition Product H2 capacity Nm3/hr 4,000 4,000 4,000 Product H2 purity mol% 99.99 99.99 99.99 Product H2 pressure kPaG 1,471 1,471 1,471 Product H2 temperature °C 35.0 35.0 35.0 Feed C4LPG C4LPG C4LPG PSA H2 recovery % 82.0 82.0 82.0 Flue gas exit temperature °C 200 200 200 Combustion air temperature °C 900 15 400 Consumption figure Feed LPG kg/hr 1,291 1,164 1,164 Fuel LPG kg/hr 0 486 299 Feed+Fuel LPG kg/hr 1,291 1,650 1,463 Reforming duty MW 4.48 4.66 4.66 Reformer firing duty MW 5.12 11.00 8.63 Thermal efficiency of Radiant section % 87.5 42.4 54.0 Steam Generation kg/hr 7,026 12,008 8,954 Process steam kg/hr 5,440 4,907 4,907 Export steam kg/hr 1,586 7,101 4,047 CW Ton/hr 74.4 69.1 69.1

The advanced Hydrogen plant gives us the follow-

ing advantages: • No requirement for additional fuel gas sup-

ply from outside of battery limit • Minimized export steam • High fuel efficiency of the steam reformer

without a convection section • Minimum investment cost and smaller plot

area

Conclusion

The development of advanced high-temperature air combustion technology for the steam reforming process has progressed from 1999 to 2002, and will be contin-ued until 2003, the expected project termination.

The results of the development work for the three years are summarized below:

1) A 3D design simulator was developed by

integrating the existing 3D simulator for

conventional combustion, and radiant heat transfer with a chemical reforming reaction simulator.

2) It was confirmed that an ionization probe is effective for the detection of invisible high-temperature air combustion flames.

3) It was also confirmed that Johns 4 step chemical reaction model is adequate for the high-temperature combustion phenomena installed in the 3D design simulator.

4) The developed 3D simulator can analyze the temperature distribution of the tube skin, flue gas, and process gas, together with chemical components of the process gas.

The new technology concept give us the possibility

of a technical break-through for the steam reforming process, not only for steam reformer design, but also for hydrogen plant design as shown below.

1) The advanced steam reformer is expected

to reduce the plot area by 30-40% less and


the material work volume by approximately 50%.

2) The advanced hydrogen plant is expected to realize the following targets: a) Reduction of fuel consumption by

more than 50% b) Reduction of green house gasses( CO2)

by more than 50% c) Reduction of NOx emission by more

than 30% Prevention of warming the earth, reduction of en-

ergy consumption, and zero-emission are our urgent re-quirement from the environmental view point. We should consider and apply new technology for the steam reforming process at the earliest time when the consider-ing economical growth in the world.

Documents

Development on Advanced High-Temperature Air Combustion … · 2018. 8. 22. · High-Temperature Air Combustion Technology for Steam Reforming Process ... (CH4 -> C+2H2) Gas temperature