Simulation of hydrogen production from thermal decomposition of hydrogen sulfide in sulfur recovery units

Adewale, Rasheed; Salem, Dalia J.; Berrouk, Abdallah S.; Dara, Satyadileep

doi:10.1016/j.jclepro.2015.08.021

Cited by 41 publications

(16 citation statements)

References 11 publications

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“…Although the first configuration is definitely more cost-effective than the second one, none of them could be, in terms of hydrogen price, the rival of the conventional SMR process [195]. Adewale et al [196] studied hydrogen production from the thermal decomposition of hydrogen sulfide in a commercial sulfur recovery unit and then analyzed the economic benefits obtaining by retrofitting a Claus burner for this purpose. Although an early reduction in the sulfur recovery of the unit was observed, economic analyses showed that the return of capital investment is feasible within less than four years.…”

Section: Pyrolysis Of Hydrogen Sulfide: Energy Delivery and Decontamimentioning

confidence: 99%

Hydrogen Production Through Pyrolysis

Bakhtyari

Makarem

Rahimpour

2017

Encyclopedia of Sustainability Science and Technology

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Hydrogen Production Through Pyrolysis, Table 1 Properties of hydrogen (Adopted from [12, 14, 15]) Property Quantity Unit Critical point Critical temperature 33.24 K Critical pressure 1.297 Mpa Critical density 30.77 Kg.m À3 Compressibility factor 0.304-Gaseous Density 1.33 Kg.m À3 Compressibility factor 0.906-Enthalpy 1447.4 J.mol À1 Entropy 78.94 J.mol À1 .K À1 Constant pressure heat capacity 24.6 J.mol À1 .K À1 Constant volume heat capacity 13.2 J.mol À1 .K À1 Viscosity 1.11 Â 10 À3 mPa.s Thermal conductivity 16.5 Â 10 À3 W.m À1 .K À1 Liquid Normal boiling point 20 K Heat of vaporization 891.2 J.mol À1 Density 70.96 Kg.m À3 Compressibility factor 0.017-Enthalpy 548.3 J.mol À1 Entropy 34.92 J.mol À1 .K À1 Constant pressure heat capacity 19.7 J.mol À1 .K À1 Constant volume heat capacity 11.6 J.mol À1 .K À1 Viscosity 13.3 Â 10 À3 mPa.s Thermal conductivity 100 Â 10 À3 W.m À1 .K À1 Combustion Autoignition temperature 858 K Low heating value 119.9 kJ.g À1 High heating value 141.8 kJ.g À1 Diffusion coefficient in air at STP 0.61 cm 2 .s À1 Detonability limits in air 18.3-59 Volume % Limiting oxygen index 5 Volume % Flammability limits in air 4-75 Volume % Minimum energy of ignition in air 20 kJ Flame temperature in air 2318 K

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Section: Pyrolysis Of Hydrogen Sulfide: Energy Delivery and Decontamimentioning

confidence: 99%

Hydrogen Production Through Pyrolysis

Bakhtyari

Makarem

Rahimpour

2017

Encyclopedia of Sustainability Science and Technology

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“…There have been theoretical and experimental studies of SRU thermal reactors. Adewale et al [1] studied the thermal decomposition of H 2 S into hydrogen and sulfur using a process simulator. Using the net fraction of the acid gas feed to the cracking coils as the controlling parameter, its effect on hydrogen production, the thermal reactor's energy requirement, the stability of the burner flame, steam production, the temperature of a Claus reactor and sulfur recovery of the primary SRU was studied.…”

Section: Nh3 + So2 → N2 + H2s + 2h2omentioning

confidence: 99%

The Effect of Fuel Mass Fraction on the Combustion and Fluid Flow in a Sulfur Recovery Unit Thermal Reactor

Yeh

2016

Applied Sciences

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Sulfur recovery unit (SRU) thermal reactors are negatively affected by high temperature operation. In this paper, the effect of the fuel mass fraction on the combustion and fluid flow in a SRU thermal reactor is investigated numerically. Practical operating conditions for a petrochemical corporation in Taiwan are used as the design conditions for the discussion. The simulation results show that the present design condition is a fuel-rich (or air-lean) condition and gives acceptable sulfur recovery, hydrogen sulfide (H2S) destruction, sulfur dioxide (SO2) emissions and thermal reactor temperature for an oxygen-normal operation. However, for an oxygen-rich operation, the local maximum temperature exceeds the suggested maximum service temperature, although the average temperature is acceptable. The high temperature region must be inspected very carefully during the annual maintenance period if there are oxygen-rich operations. If the fuel mass fraction to the zone ahead of the choke ring (zone 1) is 0.0625 or 0.125, the average temperature in the zone behind the choke ring (zone 2) is higher than the zone 1 average temperature, which can damage the downstream heat exchanger tubes. If the zone 1 fuel mass fraction is reduced to ensure a lower zone 1 temperature, the temperature in zone 2 and the heat exchanger section must be monitored closely and the zone 2 wall and heat exchanger tubes must be inspected very carefully during the annual maintenance period. To determine a suitable fuel mass fraction for operation, a detailed numerical simulation should be performed first to find the stoichiometric fuel mass fraction which produces the most complete combustion and the highest temperature. This stoichiometric fuel mass fraction should be avoided because the high temperature could damage the zone 1 corner or the choke ring. A higher fuel mass fraction (i.e., fuel-rich or air-lean condition) is more suitable because it can avoid deteriorations of both zone 1 and heat exchanger tubes. Although a lower fuel mass fraction (i.e., fuel-lean or air-rich condition) can avoid deterioration of zone 1, the heat exchanger tubes may be damaged. This paper provides a guideline for adjusting the fuel mass fraction to reduce the high temperature inside the thermal reactor and to ensure an acceptable sulfur recovery.

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“…Catalytic pathway for thermally decomposing H 2 S has shown great efficiency, while providing an opportunity to recover the produced hydrogen [10]. Other methods including thermochemical process, photocatalytic approach, electrolysis, hydrolysis and reactive adsorption have also been attempted, showing great potentials for hydrogen recovery and high sulfur recovery rate, but they are all still in their infancy [9,[11][12][13]]. Yet, the Claus process is still the leading pathway for converting hydrogen sulfide to elemental sulfur, owing to its maturity developed over several years of research and operation.…”

Section: Introductionmentioning

confidence: 99%

Investigating efficiency improvement in sulfur recovery unit using process simulation and numerical modeling

Fazlollahi

Asadizadeh

Khoshooei

et al. 2021

Oil Gas Sci. Technol. – Rev. IFP Energies nouvelles

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Hydrogen sulfide exists mostly as a detrimental byproduct in the gas processing units as well as refineries, and it must be eliminated from natural gas streams. In a Sulfur Recovery Unit (SRU), hydrogen sulfide is converted into the elemental sulfur during the modified Claus process. Efficiency of sulfur recovery units significantly depends on the reaction furnace temperature. In this work, the effect of oxygen and acid gas enrichment on the reaction furnace temperature and accordingly on sulfur recovery is studied, using both numerical modeling and process simulation. Then, simulation and numerical model are benchmarked against the experimental data of an SRU unit. The validated model provides spotlight on optimizing the upstream sulfur removal unit as well as the oxygen purification process. Two cases of acid gas streams with low and high H2S content, 30% and 50%, are studied to investigate the effect of operating parameters on the overall recovery. Finally, average errors of the models are presented. According to the absolute difference with experimental values, the developed numerical model shows great potential for accurately estimating overall efficiency of the recovery unit.

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Simulation of hydrogen production from thermal decomposition of hydrogen sulfide in sulfur recovery units

Cited by 41 publications

References 11 publications

Hydrogen Production Through Pyrolysis

Hydrogen Production Through Pyrolysis

The Effect of Fuel Mass Fraction on the Combustion and Fluid Flow in a Sulfur Recovery Unit Thermal Reactor

Investigating efficiency improvement in sulfur recovery unit using process simulation and numerical modeling

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