This paper presents the analysis of potential thermal cracking of light feedstocks in the SMR. Two different feedstocks, natural gas and light hydrocarbon (HC) feedstock at two different mixed feed inlet temperatures, are selected to study the HC thermal cracking. Effect of Crossover Piping Volume on feed thermal cracking is also discussed.
H2 can be produced from a variety of HC’s, ranging from natural gas (methane) to petroleum-based gases and liquids. In our previous paper (Part I), we had quantitatively discussed thermal cracking of Liquefied Natural Gas (LNG), C4 stream and naphtha feed stocks in the CPV of reformer [
Parameters that affect thermal cracking are HC feed composition and component structure, mixed feed (HC + Steam) reformer inlet temperature and pressure, Steam/C mole ratio and mixed feed residence time in the CPV, etc. [
Natural gas is an important feed stock for SMR, however it is not a commodity with uniform composition and it includes N2, CO2, CH4 and non-methane HC’s.
The objective of this study is to explore the parameters which will affect the undesired cracking of reformer feed stocks in the Mixed Feed Preheater (MFPH) coil and in the CPV. The parameters being considered are the mixed feed inlet temperature to the reformer and the residence time of mixed feed in the CPV. Also in this paper we introduce the concept of Temperature Index (TI) to indicate the thermal cracking potential of HC’s.
HC feed is mixed with process steam and this stream is called mixed feed. The mixed feed is preheated in the MFPH Coil located in the convection section, and the preheated mixed feed is sent to the catalyst tubes through crossover piping (
1) Scope
This paper analyses potential of thermal cracking in the MFPH Coil and crossover piping from MFPH coil outlet to the inlet of SMR.
2) MFPH Coil
MFPH Coil geometry and tube material are listed below (
3) Feed Composition
Case 1 feed (Natural Gas) has N2, CO2, CH4 and non-methane hydrocarbons as shown in
Case 2 is a light feed which is treated in the pre-reformer. It has more H2 and CO2, CH4 and no C2 + hydrocarbons as shown in
4) Crossover Piping Volume (CPV)
Assume CPV is an adiabatic zone with no heat loss. CPV is constant for all cases which is 24.7 m3 per SMR.
5) Pressure Drop
Assume 0.35 kg/cm2 drop through CPV.
The SMR feedstock cracking kinetics has been simulated using SPYRO® program which is widely used by the industry for prediction of hydrocarbon cracking.
SPYRO® is a unique program for prediction of cracking furnace effluent yields as well as overall performance of the furnace. SPYRO® is the only program which is based on the rigorous fundamental mathematical equations
MFPH # of Rows | Tube Size NPS | Hori/Vert Distance inch | Tubes per Row | No. of Passes | Tube Material |
---|---|---|---|---|---|
8 (outlet) | 3” Sch 80 | 8/6 | 14 | 28 | 800H |
7 | 3” Sch 80 | 8/6 | 14 | 28 | |
6 | 3” Sch 80 | 8/6 | 14 | 28 | |
5 | 3” Sch 40 | 8/6 | 14 | 28 | |
4 | 3” Sch 40 | 8/6 | 14 | 28 | |
3 | 3” Sch 40 | 8/6 | 14 | 28 | |
2 | 3” Sch 80 | 8/6 | 14 | 28 | |
1 (inlet) | 3” Sch 80 | 8/6 | 14 | 28 |
Note 1: Total 8 rows in MFPH coil. 2: Effective tube length 13.2 m for all tubes. 3: All tubes are bare. 4: Process gas and flue gas are in co-current flow.
Composition | MW | Mixed Feed | |
---|---|---|---|
Mol % | Wt % | ||
H2 | 2.0159 | 0.85 | 0.097 |
N2 | 28.014 | 0.55 | 0.874 |
CO2 | 44.01 | 0.49 | 1.224 |
CH4 | 16.043 | 26.00 | 23.669 |
C2H6 | 30.07 | 0.38 | 0.648 |
C3H8 | 44.097 | 0.05 | 0.125 |
iC4H10 | 58.124 | 0.01 | 0.033 |
nC4H10 | 58.124 | 0.01 | 0.033 |
nC6H14 | 86.177 | 0.01 | 0.049 |
H2O | 18.015 | 71.65 | 73.247 |
Total | 100.00 | 100.000 | |
MW | Kg/Mol | 17.623 | |
Steam/C | Mol/Mol | 2.65 |
Composition | MW | Mixed Feed | |
---|---|---|---|
Mol % | Wt % | ||
H2 | 2.0159 | 7.25 | 0.86 |
N2 | 28.014 | 0.57 | 0.94 |
CO | 28.01 | 0.04 | 0.07 |
CO2 | 44.01 | 2.22 | 5.75 |
CH4 | 16.043 | 26.23 | 24.79 |
H2O | 18.015 | 63.69 | 67.59 |
Total | 100.00 | 100.000 | |
MW | Kg/Mol | 16.976 | |
Steam/C | Mol/Mol | 2.42 |
Units | Case 1 | Case 2 | |||
---|---|---|---|---|---|
MFPH Inlet Stream | |||||
Pressure | Kg/cm2-a | 39.4 | 39.3 | ||
Temp. | °C | 368.4 | 456.4 | ||
Flow | Kmol/h | 7,212 | 6,557 | ||
MFPH Outlet and Reformer Inlet Streams | |||||
MFPH Outlet | SMR Inlet | MFPH Outlet | SMR Inlet | ||
Pressure | Kg/cm2-a | 38.4 | 38.0 | 38.3 | 37.9 |
Temp. | ˚C | 593.5 | 593.3 | 649.3 | 648.9 |
Resid.Time in CPV | Sec | 6.4 | 6.6 |
Units | Case 1 | Case 2 | |
---|---|---|---|
Flue Gas | |||
Pressure | Kg/cm2-a | 1.0 | 1.0 |
Temperature | ˚C | 1003 | 1001 |
Flow | Kmol/h | 10,540 | 9310 |
Composition | Mol % | ||
CO2 | 19.15 | 20.54 | |
Ar | 0.73 | 0.71 | |
O2 | 1.63 | 1.45 | |
N2 | 61.59 | 59.84 | |
H2O | 16.90 | 17.46 | |
Total | 100.00 | 100.00 |
representing reaction kinetics of almost all chemical, thermo-chemical reactions in the pyrolysis furnace.
SPYRO® is now used by more than 85% of the ethylene producing industry worldwide. The latest program version and kinetic model SPYRO®-7 covers all hydrocarbon species from C2 to C42 and more than 7000 reactions. This version also allows better flexibility in establishing the furnace and heat recovery flowsheet.
For the sake of completeness, we are recapping the fundamentals of thermal cracking from paper Part I (1) in this section [
1) Bond Energy
Bond energy is a measure of bond strength in a chemical bond. The larger the bond energy, the stronger the bond and hence the higher temperature required to break it. The bond energy is essentially the average enthalpy change for a gas reaction to break all the similar bonds. For the methane molecule, CH3-H, 104 kcal is required to break the first single C-H bond for a mole of methane, but breaking all four C-H bonds for a mole of methane requires 397 kcal. Thus, the average bond energy is (397/4) 99 (not 104) kcal/mol.
2) Bond Length
Distance between centers of bounded atoms is called bond length. There is a general trend in that the shorter the bond length, the higher the bond energy. Some typical bond lengths and bond energies are given below to illustrate a general trend (
Bond Type | Bond Length Picometer (pm), 1 pm = 10−12 m | Bond Energy Kcal/mol |
---|---|---|
H-H | 74 | 104 |
H-C | 109 | 99 |
C-C | 154 | 83 |
C=C | 134 | 147 |
C≡C | 120 | 200 |
Atom or Group | H | CH3 | C2H5 | (CH3)2CH | (CH3)3C | C6H5 | C6H5CH2 |
---|---|---|---|---|---|---|---|
H | 104 | 103 | 98 | 95 | 93 | 110 | 85 |
CH3 | 103 | 88 | 85 | 84 | 81 | 101 | 73 |
C2H5 | 98 | 85 | 82 | 81 | 78 | 99 | 71 |
(CH3)2CH | 95 | 84 | 81 | 79 | 74 | 97 | 70 |
(CH3)3C | 93 | 81 | 78 | 74 | 68 | 94 | 67 |
C6H5 | 110 | 101 | 99 | 97 | 94 | 110 | 83 |
C6H5CH2 | 85 | 73 | 71 | 70 | 67 | 83 | 59 |
CH3: -methyl: C2H5: -ethyl:(CH3)2CH: i-propyl (CH3)3C: -t-butyl C6H5: -phenyl C6H5CH2: -benzyl.
3) Temperature Index
Temperature Index (TI) represents the mixed feed temperature reduction due to the thermal cracking and chemical reaction in the adiabatic zone i.e. crossover piping volume (CPV).
4) General Cracking Rules
a) Bond energy comparison between different atoms
H-H > C-H > C-C (C-C is easier to break)
b) Dehydrogenation ability of HC depends upon its structure and is in the order of:
Tertiary H > Secondary H > Primary H
c) For carbon-carbon bonds, the order of bond energy:
Triple Bond > Double Bond > Single Bond
d) Order of heat stability for paraffin is:
CH4 > C2H6 > C3H8 > C4H10 >
e) For HC with same C atoms, heat stability order is:
Aromatics > Naphthene > Di-Olefin > Olefin > Paraffin
1) Effect of feed composition and mixed feed inlet temperature on the thermal cracking and MFPH coil material selection.
Data in
a) Steam-HC reforming reactions which are irreversible reactions at normal condition.
b) Methane reacts with water steam to form carbon monoxide and hydrogen (the mixture of CO and H2 is known as syngas), which is a reversible chemical reaction,
c) Water-gas shift reaction (WGSR) is a reversible chemical reaction in which carbon monoxide reacts with water vapor to form carbon dioxide and hydrogen,
However, Reverse Water-Gas Shift (RWGS) reaction,
Location | Mixed Feed to MFPH | MFPH Outlet | Outlet of Cross Over Piping |
---|---|---|---|
Mixed FeedFlow, Kg/h | 127,097 | 127,097 | 127,097 |
Composition mol% (wet) | |||
Hydrogen | 0.8500 | 0.8499758 | 0.8512 |
Methane | 26.0000 | 25.9999995 | 25.9998 |
Ethylene | - | 0.0000045 | 0.0031 |
Ethane | 0.3800 | 0.3799983 | 0.3791 |
Propylene | - | 0.0000020 | 0.0015 |
Propane | 0.0500 | 0.0499983 | 0.0487 |
Butenes | - | 0.0000008 | 0.0004 |
Butanes | 0.0200 | 0.0199987 | 0.0190 |
n-Hexane | 0.0100 | 0.0099988 | 0.0092 |
1-Pentene | - | 0.0000001 | 0.0001 |
Carbon Monoxide | - | 0.0000286 | 0.0017 |
Carbon Dioxide | 0.4900 | 0.4899714 | 0.4883 |
Nitrogen | 0.5500 | 0.5500000 | 0.5500 |
Water | 71.6500 | 71.6500230 | 71.6478 |
Total | 100.0000 | 99.9999998 | 100.0000 |
Total Olefins | - | 0.0000074 | 0.0051 |
Temperature ˚C | 368.4 | 593.5 | 593.3 |
Location | Mixed Feed to MFPH | MFPH Outlet | Outlet of Cross Over Piping |
---|---|---|---|
Mixed FeedFlow, Kg/h | 111,312 | 111,312 | 111,312 |
Composition mol% (wet) | |||
Hydrogen | 7.25 | 7.2464 | 7.1864 |
Methane | 26.23 | 26.2300 | 26.2300 |
Carbon Monoxide | 0.04 | 0.0436 | 0.1036 |
Carbon Dioxide | 2.22 | 2.2164 | 2.1564 |
Nitrogen | 0.57 | 0.5700 | 0.5700 |
Water | 63.69 | 63.6936 | 63.7536 |
Total | 100.00 | 100.0000 | 100.0000 |
Temperature ˚C | 456.4 | 649.3 | 648.9 |
2) Effect of crossover piping volume on cracking
The effect of SMR crossover piping volume on the mixed feed thermal cracking is shown in
No. of Rows | Case 1 | ||||
---|---|---|---|---|---|
Mixed Feed Temp, ˚C | Flue Gas Temp. ˚C | Simulation MTT, ˚C | Design Temp, ˚C | Material | |
Row 8 | 593.5 (outlet) | 821.7 (outlet) | 646.7 | 743.9 | 800H Sch 80 |
Row 7 | 633.9 | ||||
Row 6 | 616.1 | ||||
Row 5 | 643.3 | 693.9 | 800H Sch 40 | ||
Row 4 | 596.1 | ||||
Row 3 | 556.1 | ||||
Row 2 | 614.4 | 743.9 | 800H Sch 80 | ||
Row 1 | 368.4 (inlet) | 1003.3 (inlet) | 612.2 |
No. of Rows | Case 2 | ||||
---|---|---|---|---|---|
Mixed Feed Temp, ˚C | Flue Gas Temp. ˚C | Simulation MTT, ˚C | Design Temp, ˚C | Material | |
Row 8 | 649.3 (outlet) | 842.2 (outlet) | 689.4 | 743.9 | 800H Sch 80 |
Row 7 | 678.3 | ||||
Row 6 | 663.3 | ||||
Row 5 | 640.0 | 693.9 | 800H Sch 40 | ||
Row 4 | 645.0 | ||||
Row 3 | 611.7 | ||||
Row 2 | 661.1 | 743.9 | 800H Sch 80 | ||
Row 1 | 456.4 (inlet) | 1001.1 (inlet) | 661.7 |
For constant mixed feed flowrate, the residence time of mixed feed in the crossover piping is decided by the crossover piping volume, which depends on the crossover piping dimension and the distance from convection section outlet (Point A in
Mixed feed flowrate, kg/h | 127,090 (Case 1) | ||||
---|---|---|---|---|---|
Crossover Piping Volume (CPV), m3 | 0.0 | 24.7 | 49.4 | 74.1 | 98.8 |
MFPH outlet temperature, ˚C | 648.9 | 649.9 | 650.5 | 650.9 | 651.2 |
Residence time in CPV, sec | 0.0 | 6.0 | 12.0 | 18.0 | 24.0 |
Mixed feed T drop in CPV, ˚C | 0.0 | −1.0 | −1.6 | −2.0 | −2.27 |
Mixed feed T at SMR inlet, ˚C | 648.9 | 648.9 | 648.9 | 648.9 | 648.9 |
C2H4 + C3H6 at MFPH outlet, wt% (dry) | 7.90E−4 | 8.22E−4 | 8.42E−4 | 8.55E−4 | 8.65E−4 |
C2H4 + C3H6 formed in CPV, wt% (dry) | 0.0 | 0.239 | 0.389 | 0.479 | 0.539 |
C2H4 + C3H6 at SMR inlet, wt% (dry) | 7.90E−4 | 0.24 | 0.39 | 0.48 | 0.54 |
Therefore, it is better to keep the CPV as small as possible to avoid higher light olefins entering into the reformer.
The mixed feed temperature at the reformer inlet is equal to the MFPH feed outlet temperature minus the mixed feed temperature drop in the crossover piping volume.
1) There is not only thermal cracking but also chemical reaction in the MFPH coil and crossover piping volume which is an adiabatic zone.
2) There is a slight thermal cracking and chemical reactions in both MFPH coil and crossover volume for Case 1 and Temperature Index (TI) is 0.2˚C.
3) There is no thermal cracking for Case 2 feed because of non-methane hydrocarbons in the feed. However, Reverse Water-Gas Shift (RWGS) reaction, which is an endothermic reaction, can be involved in both MFPH coil and crossover volume. Hydrogen reacts with carbon dioxide to form carbon monoxide and water vapor and TI is 0.4˚C.
4) Larger Crossover Piping Volume results in a higher temperature reduction in the adiabatic zone and therefore, more light olefins to the reformer and easy to form coke in reformer tubes.
5) Maximum tubewall temperature profiles for MFPH coil are useful to select the correct tube material.
Guotai Zhang,Sanjeev Sekhri, (2015) Potential Cracking in Hydrogen Plant with Light Feedstocks (Part II). World Journal of Engineering and Technology,03,18-25. doi: 10.4236/wjet.2015.33C003