STEAM-HYDROCARBON REFORMER FURNACE DESIGN
Introduction Direct-fired steam hydrocarbon reforming furnace is the “work-horse” of gas production processes. Steam reforming process is a well-established catalytic process tha t convert natural gas or light hydrocarbons in a mixture containing a major portion of Hydrogen. The Steam reforming process has gained more and more importance with the increasing demand of various type of syngases for the chemical and petrochemical industries. Its application are in the production of:
-
Ammonia Methanol OXO Alcool Hydrogen
In particular Hydrogen has become a very important product for the refinery desulphurisation and hydrocracking process units. The furnace may “stand alone”, or operate in conjunction with a pre reformer, post-reformer, or other schemes. I n the furnace, the reforming of steam-hydrocarbon mixtures is accomplished in catalyst-filled tubes. In hydrogen plants, in-tube fluid pressures are typically 25 ÷ 30 kg/cm2 with outlet temperatures up to 860°C (and even higher) depending on the process requirements. The reformer reaction process is endothermic, requiring high level heat input. A variety of catalyst (nickel-based) are available for a given feed and product requirement. Safe, reliable and efficient operation is needed to meet the user’s product demands.
Radiant section arrangement As the process requires high heat input l evels, the catalyst-filled tubes are placed vertically in the radiant firebox section of the furnace. The steamhydrocarbon mixture is typically preheated outside the radiant section to 500°C ÷ 650°C to minimize the radiant heat load and, therefore, the furnace fuels requirement. Excessive preheat will effect coke formation of
Page 1
the feed, resulting in carbon deposits on the catalyst causing degradation and/or pluggage, and also potential tube failure in the preheat section. Properly located combustion equipment (burners) assures heat input as the mixture passes through the catalyst tubes and is reformed to the required outlet conditions. The catalyst tube arrangement consists of a multiple of “once-through” parallel “passes”, typically with the preheated inlet mixture entering the top of each catalyst tube, and exiting at the bottom. Once the reformed gas exits the catalyst tubes, it is collected in a header system and cooled in an external process gas waste heat exchanger. The effluent from this equipment is t ypically cooled to 320°C ÷ 370°C to permit further reaction in downstream equipment. Safe and reliable operation of the reformer furnace depends on the disposition of the catalyst tubes and the burners that supply the heat to the catalyst tubes. In theory, complete control of heat input along the vertical catalyst tube length will maximize catalyst reactivity, minimize tube temperatures, and minimize tube or catalyst damage during operating upsets such as process steam interruption, or wide load swings. Such a design requires an excessive number of burners and be difficult to operate. Several well-proven configurations are available which, each in their own way, provide a practical approach towards meeting the requirements of this process. Two particular designs are considered. FIGURE 1
Page 2
Side Fired (Terrace Wall™) Foster Wheeler Fired Heater Division developed its patented Terrace Wall ™ reformer furnace in the early 1960’s and continuosly improves it to incorporate the desired process requirements and provide a safe, operable, and economic design. This design (Figure 1) typically locates a single, in-line row of catalyst tubes in the middle of the radiant firebox, and locates burners on both sides to provide uniform heat distribution around the catal yst tube circumference. The burners fire vertically upward along the refractorylined walls of the radiant section, essentially parallel to the catalyst t ubes, to assure flame stability and avoid flame impingement. The bur ners provide a flat-shaped flame and are suitably spaced along the length of the firebox, assuring uniform heat input to the catalyst tubes; essentially the refractory wall becomes a uniform heat radiating plane. (See figure 2) Operating flexibility is “built in” to allow trimming of burners in specific areas where minor hot spots may occur, since the burners “serve” a single row of tubes. With catalyst tubes typically 11 to 14 meters long, control of vertical heat distribution along the tube lengths is typically obtained by providing two (2) levels of burners. This permits controlled heat input as process conditions, catalyst activity or other factors varies during operation. As is the case with all fired process furnaces, the radiant section heat transfer is augmented by a convection component as hot flue gas es recirculate, drawn downwards by the relatively colder tubes. In this design, the recirculation is essentially “contained” by the sidewalls on both sides of the tubes, and “reheating” (as the gases return upwards along the sidewalls past the up-fired burners) is predictable, resulting in efficient overall heat transfer.
Page 3
The upflowing hot flue gases exhaust “naturally” at the top of the firebox, entering the heat recovery section where feed preheat, steam generation, air preheat or post-combustion Nox reduction (SCR’s) may be installed.
FIGURE 2
Flat-shaped flame configuration
The top of the firebox is the point of highest pressure (lowest negative pressure, or “draft”). This area must be controlled to be maintained at least 2.5 mm water column below atmospheric pressure to keep t he furnace at negative pressure throughout, avoiding hot flue gas leakage through the various openings (tube penetrations, sight doors, etc.) and to prevent hot flue gas from contacting the furnace casing plate. The Terrace Wall™ design can frequently utilize simply a natural draft stack. Where very high fuel efficiency is needed (e.g., air preheat) or an SCR is installed, the pressure loss through this equipment usually dictates the use of mechanical draft equipment (induced draft fan). With firing at more than one level to reduce the vertical heat flux variation, and with a uniform radiating plane effected by firing along the side walls, the catalyst tubes can be spaced typically at a 1.4 to 1.7 ratio (center-tocenter divided by outside diameter) to obtain an optimal distribution of heat around the tube, minimizing peak tube metal temperatures. (using the API RP-530 curve, the circumferential heat flux factor – or variation from average flux – for calculating tube temperature is 1.31 to 1.25; see Figure 3) .
Page 4
FIGURE 3
Ratio of maximum local to average heat flux. Single row of tubes with equal radiation from both sides. Source: API RP-530
Each catalyst tube is flanged on top to permit catalyst loading from walkways at the firebox roof (or arch). The firebox sidewalls are slopped at a small angle to optimize radiant heat transfer. This also creates a “terrace” shape, which provides a mounting space for the individual burner levels. Burner access for operation and maintenance is from essentially unrestricted platforms located along the sidewalls at each firing level. Burner noise plenums, ductwork supplying preheated combustion air or, in some cases, hot gas turbine exhaust, can be readily installed. Various fuels such as natural gas, refinery gas, or even liqui d fuels (and associated atomizing steam) can be readily piped to the burners. The off-gas from a PSA (Pr essure Swing Absorption) hydrogen purification system is used as fuel for the reformer furnace. This is low BTU fuel, and usually available at low pressures. When properly integr ated with hydrogen plant design itself, the PSA fuel can provide most – or all – of the fuel needed in the reformer furnace. Typically, the plant design prefers to limit the PSA off-gas to “base-load” at 90% or so of the total reformer fuel requirement, allowing the balance (refinery gas or natural gas) to be used for controlling the heat input.
Page 5
The burner arrangement on the Terrace Wall™ design (firing along the refractory sidewalls) allows stable burning 100% of PSA off-gas once the firebox is heated. Top Fired (“Downfired”) The down-fired design (Figure 4) locates from one to as many as ten or more rows (or “lanes”) of catalyst t ubes (in-line) in a single radiant firebox enclosure, with rows of burners located in the roof (or arch) of the firebox between the tube lanes. The burners fire downwards, parallel to t he hydrocarbon-steam mixture flow direction through the catalyst tubes. Burner flame and hot gas radiation provide heat input to the tubes. The combustion of low calorific value PSA gas produce long, lazy and uncontrollable flame patterns which will be creating down-flowing as well as side turning flames with impingement on catalyst tubes, since no hot refractory lining is present to retain the flame away from the cataly st tubes. FIGURE 4
Typical Downfired design
This arrangement effects somewhat higher heat fluxes at the top of the tube (coldest fluid).
Page 6
The concentration of heat flux at catalyst tube inlet might result in local overheating of both tubes and catalyst in particular when operating at partial loads. Each row of burners provides heat input affecting two rows of catalyst tubes. The two lateral rows are subject – in addition to flue gas radiation – also to the radiation of the hot unshielded wall facing the tubes. This fact results in an overheating of one side of the lateral catalyst tube with consequent heat maldistribution. Flue gases are collected at the bottom of the firebox i n refractory “tunnels”, properly sized and arranged to maintain a uniform flow pattern in the firebox. The flue gases exit the “tunnels” and are directed to the heat recovery section for process coil heating, steam generation services, and air preheating exchanger. To assure negative pressure at the firebox, mechanical draft equipment (induced draft fan) must be installed to overcome the “draft gain” in the firebox and the pressure losses in the various heat recovery coils and/or equipment. Having firing only at one level, there is no possibility of control of the heat input along the catalyst tubes, and the heat transfer mechanism more dependent on burner spacing (not by uniformly heated sidewalls). The catalyst tubes are spaced at a 2.0 to 2.5 ratio (center-to-c enter divided by outside diameter) to minimize peak tube metal temperatures. (Using the API RP-530 curve, the circumferential heat flux factor for calculating tube temperature is 1.20 to 1.15 at this spacing). Lane spacing (versus tube length) is established to assure proper heat transfer. Access for burner operating maintenance, is from the walkways located between the tube lanes and burner rows at the firebox arch.
Page 7
Also in case of a generous lane spacing particularly with multiple fuel headers and/or hot ducting to the burners, this area, which is very hot during natural operation, might be dangerous for operator. In case of failure of the induced draft flue gas fan, hot flue gases will be trapped at the top of the down fired radiant box since no draft is available and therefore the excessive heat concentration and the possibility to have slight positive pressure at the top of the downfired reformer is a risk of injury for operating personnel, present on top of radiant section under the penthouse. The downfired arrangement is more difficult to be operated since a n uneven heat flux distribution caused by a maldistribution of the heat fired on the various lane of burners might effect heavily tube life. In addition during start-up and warm-up of steam reformer all the heat liberated by the downfiring burners will remain at the top determining a very hot area at arch level since the remaining radiant zone, still in cold condition and without vertical walls, are not suitable to provide the heat downwards. This can result in uncontrolled flame and detrimental after burning conditions between the catalyst tubes arranged in parallel lanes.
Catalyst Tubes At a specified design point, a comparison can be shown (between the two design configurations) of the in-tube fluid and tube metal temperature profiles along a catalyst tube (Figure 5). The comparative profiles for typical hydrogen reformer conditions indicate the higher heat flux at the top of the tube on the downfired design, as evidenced from a steeper fluid temperature profile (and relatively hotter tube metal temperature). The Terrace Wall™ design has the advantage that with a proper split of firing between the two burner level the fluid/metal temperature profile can be modified and optimized in accordance with the actual o perating condition while in the Downfiring design the temperature profile is only a consequence of the operating conditions. Operational upsets such as interruption of process steam or unexpected impurities in the hydrocarbon feed tends to result in greater cata lyst temperature with possibility of tubes damages in the higher flux inlet zone of the downfired unit.
FIGURE 5
Page 8
Temperature profile vs. catalyst tube length Terrace Wall™ against Downfired design
Outlet Header System The reformed gas outlet from the bottom of each catalyst tube is directed to the outlet collector header system, and then to the process gas heat exchange train (typically a waste heat boiler which generates steam). In the Terrace Wall™ design, each catalyst tube outlet is connected by an Incoloy 800H outlet pigtail, which is then connected to the outlet header. The outlet header is Incoloy 800H (or centrifugally cast equivalent material). This system is fully contained in an insulated enclosure to minimize heat loss and provide for expansion (see Figure 6). The outlet header is directly connected to the process gas waste heat boiler inlet channel in most cases. This arrangement also permits “pinching” of the individual pigtails (top inlet and bottom outlet) to isolate a failed tube without shutting down the whole unit. Experts skilled in this procedure have the equipment and know-how to safely pinch-off the tubes.
Page 9
FIGURE 6
Outlet pigtail and hot outlet header
Mechanical Features Proper installation and support systems for the catalyst tubes are critical to the successful long-term operation of the reformer furnace. Much work has been done over the years in learning the “do’s” and “don’ts” of the systems. Experience is the best teacher, and use of that experience in today’s reformer furnaces assures the most reliable product. In the Terrace Wall™ design with outlet pigtails and hot outlet header (Figure 6), the system provides full load top support (catalyst tube weight plus catalyst weight) with expansion of the catalyst tube upwards through the arch (typically 200 ÷ 250 mm). Top support is provided with a simple, positive counterweights system, which allows for the necessary variation in expansion between adjacent tubes. (Figure 7). The hot outlet header expands along the furnace length, “pulling” the outlet pigtails and the catalyst tubes with practically no stress since all the weight is supported from the top.
Page 10
Although a single row of tubes fired equally from both sides should have little – if any – temperature difference from one side to the other, the outlet pigtail does provide flexibility to reduce any bending stresses which might develop due to tube bowing.
FIGURE 7
Top supporting system
Heat Recovery Arrangement With the Terrace Wall™ reformer, the flue gas heat recovery section (convection section) is placed on top of radiant firebox. This minimizes the plot requirements, and provides continued upflow of the flue gases. The convection coils are horizontally mounted with all the services: mixed feed preheat, prereformer preheat, feed gas preheat, steam superheater and steam generation, feedwater preheater in a proper sequence to optimize the heat recovery. Steam generation coils are designed fo r forced circulation to assure positive flow throughout start-up and off-load operation. The steam drum is mounted on the reformer.
Page 11
Combustion air preheat exchanger can be mounted either on top of the upflow convection section, or mounted alongside the reformer furnace. Figure 8 shows a typical 2-cell Terrace Wall™ reformer with the closecoupled process gas waste heat boiler, steam drum, and hot air ducts to the burners. On the downfired reformer design, the hot flue gas exiting the radiant section “tunnels” can be directed to a grade-mounted heat reco very section with either vertical or horizontal flue gas flow depending on coil services and auxiliary equipment. FIGURE 8
Typical Terrace-Wall design
Page 12
Miscellaneous
Refractories Radiant section linings are exposed to firebox temperatures of 1000°C and higher, and therefore necessitating high quality insulating refra ctory materials to withstand the environment and reduce the heat loss (lower the casing temperature). Insulating firebricks backed by lightweight insulating blanket is used. Convection sections are lined with insulating castable.
Assembly Where shipping clearance is adequate, the Terrace Wall™ radiant section design lends itself to full modularization (steel and linings, catalyst tubes and outlet collectors, shop installed). (See figure 9). This feature is not possible with the Downfired design. Convection section is usually fully modularized with steel, linings and coils shop installed. FIGURE 9
Environmental
Page 13
Burner Nox levels can be effectively reduced using current low Nox burner designs. The low calorific value of PSA gas and the staged air design effectively reduces the Nox generated by the burner. This design is possible in the Terrace Wall™ reformer since the shape of the flames is controlled by the sloped wall design.
Conclusion The steam-hydrocarbon reformer furnace can be designed to meet the specific needs of a hydrogen plant. Optimal design configurations are available; one will provide the best solution for a particular purpose. Based on the consideration mentioned above it is clear the Terrace Wall™ design has several advantages if compared with the Downfiring design for what concerns safety, reliability and operability, along wit h design experience and quality. These are important factors to be considered when selecting this important c omponent in a hydrogen plant.
Foster Wheeler Experience The attached pages show Foster Wheeler experience in the steam reformer heater design and the photos of some steam reformer heaters are herewith attached.
Page 14
Page 15
Partial list of Hydrogen Steam Reformers built by Foster Wheeler
JOB
YEAR
CLIENT CONTRACTOR
OWNER
COUNTRY
SIZE (MMSCFD)
2-BE-0024A
WINTER 2005
AO MOZYR
AO MOZYR
BELARUS
22
2-BE-0023A
AUTUMN 2005
KBR/SNAM
EGTL
NIGERIA
27
2-BE-0022A
AUTUMN 2005
KOCH GLITSCH
PNCHZ
KAZAKHSTAN
15
2-BE-0020A
SUMMER 2005
AO MOZYR
AO MOZYR
BELARUS
22
2-BE-0013A
SPRING 2004
TECHNIP ITALY
ARAMCO
SAUDI ARABIA
20
NA
SUMMER 2003
PETROM
PETROM
ROMANIA
22
2-BE-0008A
SUMMER 2002
FWI/ESSO
ESSO
GERMANY
10
2-21-20070
SUMMER 2001
FW/BOC
HUNTSMAN
ENGLAND
37
2-BE-0002A
SPRING 2000
TECHNIP ITALY
REFINERIA ISLA
NETH. ANTILLES
22
NA
1997
FW
LAGOVEN
VENEZUELA
50
2-21-1830
WINTER 1996
CHIYODA
THAIOIL
THAILAND
35
2-21-1800
FALL 1996
CHIYODA
MRC
MALAYSIA
15
2-21-1780
SUMMER 1996
SNAMPROGETTI
PEMEX
MEXICO
85
2-21-1775
SUMMER 1995
ESSO
ESSO
SINGAPORE
15
2-21-20035
SPRING 1995
FWEL
PERTAMINA
INDONESIA
75
RAYTHEON
PETROTRIN
TRINIDAD
40
NA 5-16-1130
1994
FW
CENEX
MINNESOTA
12
5-16-1094
SPRING 1989
FW
NEWGRADE ENERGY
CANADA
60
FW
NEWFOUNDLAND
CANADA
42
NA
Page 16
NOTES
COMPLETE MODULE
TOP FIRED
2-21-1760
SUMMER 1996
SNAMPROGETTI
TUPRAS
TURKEY
52
2-21-1705
FALL 1993
SNAMPROGETTI
TUPRAS
TURKEY
44
2-21-1655
FALL 1993
JGC
NIOC
IRAN
50
2-21-1640
SUMMER 1996
SNAMPROGETTI
NIOC
IRAN
50
2-21-1585
SUMMER 1987
C.F. BRAUN
KNPC
KUWAIT
50
3 UNITS
ARAMCO
ARAMCO
SAUDI ARABIA
50
2 UNITS
5-16-1069 2-21-1570
SUMMER 1985
SNAMPROGETTI
ADNOC
ABU DHABI
65
5-16-1049
SUMMER 1984
FW
UNOCAL
ILLINOIS
14
FW
PETROSAR
CANADA
5-16-1034 5-16-1033
FALL 1984
PBS
SHELL
CANADA
35
2 UNITS - TOP FIRED
2-21-1565
SUMMER 1984
JGC
KNPC (FUC)
KUWAIT
42
2 UNITS
5-16-1030
SPRING 1984
FE
SNC / SUNCOR
CANADA
41
2-21-1540
SUMMER 1983
JGC
KNPC (RMP)
KUWAIT
42
5-16-1026
FALL 1983
BECHTEL
PETROCANADA
CA NADA
36
5-16-1020
SPRING 1983
FLUOR
PHILLIPS
TEXAS
60
5-16-1010
FALL 1982
FLUOR
POWERINE OIL
CALIFORNIA
19
5-16-1003 (GTE)
SUMMER 1983
FW
CHEVRON
MINNESOTA
95
2-21-1455
WINTER 1980
CHIYODA
ARAMCO
SAUDI ARABIA
66
2-21-1405
SUMMER 1980
SNIA
TECHMASHIMPOR T
RUSSIA
8,5
5-16-964
WINTER 1979
FW
KIPCO
KOREA
17,7
5-16-956
WINTER 1979
FW
PGW
PENNSILVANIA
CONFID.
2-21-1385
SUMMER 1978
SNAMPROGETTI
NIOC
IRAN
34
5-16-940
SUMMER 1977
P ROCON
AMOCO
ALABAMA
16
5-16-935
SUMMER 1978
KNPC
KNPC
KUWAIT
70
Page 17
2 UNITS
2 UNITS
5-16-926
1978
FW
PETROCANADA
CANADA
17
5-16-903
FW
MOBIL
NEW JERSEY
21
5-16-886
FLUOR
TUCSON O & G
ARIZONA
6
5-16-883
FLUOR
BP
OHIO
42
NEVER ERECTED
5-16-863
FW
CHEVRON
NEW JERSEY
7
NEVER ERECTED
2-21-60107
1976
FWL
BP
ENGLAND
48
PRH 2940
1976
FWF
RHONE POULENC
FRANCE
7,6
5-16-853
SUMMER 1976
MCKEE
VENEZUELA
29
2-21-1370
1975
FWI
SIR
ITALY
34
2-21-60095
1975
FWEL
NIOC
IRAN
32
5-16-851
WINTER 1975
PROCON
AMOCO
TEXAS
1
FLUOR
N.W. NAT GAS
OREGON
5
BADGER
BORCO
BAHAMAS
35
FLUOR
TRANSCO
PENNSILVANYA
10,5 9,5
5-16-847 5-16-824
SUMMER 1975
5-16-818 5-16-802
SPRING 1975
FW
PUBLIC SERVICE G&E
NEW JERSEY
2-21-1320
SPRING 1975
FWI
ISAB
ITALY
2-21-1275
SUMMER 1973
SNAMPROGETTI
NIOC
IRAN
17
2-21-60052
1973
FWL
IRVING OIL
CANADA
40
PRH 1805
SUMMER 1973
FWF
BP LAVERA
FRANCE
29
5-16-801
SPRING 1973
FW
PUBLIC SERVICE G&E
NEW JERSEY
1
2-21-60030
1972
FWL
NIOC
IRAN
30
5-16-779
FALL 1972
IHI
TOKAI DENKA
JAPAN
1,9
2-21-1295
FALL 1972
FLOUR
ESSO CREOLE
VENEZUELA
5-16-762
SPRING 1972
IHI
SHOWA YOKKAICHI
JAPAN
Page 18
NEVER ERECTED
2 UNITS
ESSO DESIGN
ESSO DESIGN 31,1
5-16-751
SUMMER 1972
LUMMUS
CANADA PETROFINA
CANADA
45,8
5-16-705
SPRING 1971
FW
PENNZOIL
PENSYLVANYA
1,65
5-16-672 (GTE)
SPRING 1971
BECHTEL
CHEVRON
MINNESOTA
80
5-16-670
SUMMER 1972
BECHTEL
PEMEX
MEXICO
52,5
5-16-648
SPRING 1972
IDEMITSU-KOSAN
IDEMITSU-KOSAN
JAPAN
17
5-16-645
SPRING 1971
KELLOGG
SHELL
TEXAS
CONFIDENTIAL
2-21-10273
19 70
FWL
SAO PAULO
BRAZIL
4
5-16-625
WINTER 1970
BECHTEL
MARATHON
ILLINOIS
26,5
5-16-622
1967
NOHON KIHATSUYU
NOHON KIHATSUYU
JAPAN
28
5-16-611
FALL 1970
PROCON
SHELL
CANADA
35
5-16-608
SUMMER 1969
PRITCHARD
MOBIL
LOUISIANA
26
5-16-604
FALL 1968
DAIKYOWA
DAIKYOWA
JAPAN
12
5-16-555
FALL 1968
JGC
KNPC
KUWAIT
39
5-16-535
SPRING 1969
FW
MOBIL
TEXAS
60
2-21-10253
1968
FWL
NATREF
SOUTH AFRICA
22
2-21-10239
1968
FWL
PETROBRAS
BRAZIL
220
2-21-10238
1968
FWL
BP
ENGLAND
80
5-16-501
WINTER 1970
AG MCKEE
SHELL
ILLINOIS
55
5-16-488
SUMMER 1968
FLUOR
KNPC
KUWAIT
70
5-16-479
SUMMER 1968
FLUOR
NIOC
IRAN
33
2-21-1075
SPRING 1968
FWI
MONTESUD
ITALY
2,2
2-21-10212
1967
FWL
NTGB
ENGLAND
50
5-16-451
SPRING 1967
FLUOR
ATLANTIC REFINING
PENNSYLVANYA
50
2-21-10197
1966
FWL
GULF OIL
WALES
12
Page 19
3 UNITS
2 UNITS
2-21-10186
1966
FWL
NIOC
IRAN
30
5-16-444
WINTER 1966
PARSONS
MOBIL
CALIFORNIA
50
5-16-437
FALL 1966
PARSONS
ARCO
CALIFORNIA
55
5-16-397
SUMMER 1966
FLUOR
BP
OHIO
26,9
5-16-388
WINTER 1965
FW
CHEVRON
CALIFORNIA
67,5
5-16-328
WINTER 1964
FW
KETONA CHEMICAL
5-16-315
SPRING 1964
FW
AMERICAN CYNAMID
NEW JERSEY
2
FWL
ESSO FAWLEY
ENGLAND
1,6
5-16-290
ALABAMA
2,3
5-16-248
WINTER 1963
PARSONS
LINDE NASA
CALIFORNIA
26
5-16-242
WINTER 1962
FWL
BRITISH AMERICAN
CANADA
11
WINTER 1962
FLUOR
CHEVRON
MINNESOTA
20
Page 20
2 UNITS
Hydrogen SteamReformer for ISLA Refinery – Curacao – N.A. Capacity 26000 Nm3/h – Single Cell Design
Page 21
Hydrogen Steam Reformer for PEMEX - Mexico Capacity 90,000 Nm3/h – Double Cell Design
Page 22
Hydrogen Steam Reformer for AO Mozyr - Belarus Capacity 12,000 Nm3/h – Single Cell Design
Page 23
Hydrogen Steam Reformer for NIOC - Iran Capacity 50,000 Nm3/h – Double Cell Design
Page 24
Hydrogen Steam Reformer for KNPC - Kuwait Capacity 55,000 Nm3/h –Double Cell Design Air preheaters and fans mounted on top of the heaters Seven Units supplied in three Refineries
Page 25
Hydrogen Steam Reformer for TUPRAS - Turkey Capacity 45,000 Nm3/h –Double Cell Design
Page 26
