Gasification combined cycle: Carbon dioxide recovery, transport, and disposal

Doctor, R.D.; Molburg, J.C.; Thimmapuram, P.; Berry, G.F.; Livengood, C.D.

doi:10.2172/10190542

Cited by 20 publications

(14 citation statements)

References 6 publications

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“…According to the designs in other studies [Doctor, 1994, 1996, Sciamanna, 1988, Black, 2000, a thumb rule of design is concluded here. If the pressure of CO 2 rich Selexol flow is larger than 240 psia, two power recovery turbines will be used.…”

Section: Power Recoverymentioning

confidence: 62%

“…Table 3. Approach temperatures used in Aspen Plus to characterize non-equilibrium ([Altafini, 2003;Zaimal, 2002, Zhu, 2003 Table 11: Water gas shift reactor cost data adjusted to the dollar value in 2000 [Doctor, 1996] Table 12: Gas-liquid heat exchanger cost data adjusted to the dollar value in 2000 [Doctor, 1996] Table 13: Gas-gas heat exchanger cost data adjusted to the dollar value in 2000 [Doctor, 1996] Table 16 Relative solubility of gases in Selexol solvent [Doctor, 1994] Table 21 Absorber cost data adjusted to the dollar values in 2000 [Doctor, 1996] Table 22 Power recovery turbine cost data adjusted to the dollar value in 2000 [Doctor, 1996] Table 23 Sump tank cost data adjusted to the dollar value in 2000 [Doctor, 1996] Table 24 Recycle compressor cost data adjusted to the dollar value in 2000 [Doctor, 1996] Table 25 Selexol pump cost data adjusted to the dollar value in 2000 [Doctor, 1996] …”

Section: Total Revenue Requiredmentioning

confidence: 99%

“…The reactor vessels are made of carbon steel. The process facility costs of the shift reactors are estimated based on the reactor volumes, which is assumed to be 1.2 times the catalyst volume [Doctor, 1994].…”

Section: Process Facility Costmentioning

confidence: 99%

“…For instance, as shown in Table 16, CO 2 is 75 times more soluble than H 2 , and H 2 S is 670 times more soluble than H 2 in Selexol. Table 16 Relative solubility of gases in Selexol solvent [Doctor, 1994] Table 17 shows the actual solubility of various gases at 25°C in the Selexol solvent. The solubility data in Table 17 are based on single component solubility.…”

Section: Solubility Of Acid Gasesmentioning

confidence: 99%

“…The ratio of the actual flow rate to the equilibrium flow rate of the solvent was regressed based on published data [Doctor, 1994, 1996, Sciamanna, 1988. The ratio is given in Equation (51):…”

Section: Figure 42 Simplified Selexol Processmentioning

confidence: 99%

See 4 more Smart Citations

Development and Application of Optimal Design Capability for Coal Gasification Systems

Rubin¹,

Rao²,

Berkenpas³

2007

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Section: Power Recoverymentioning

confidence: 62%

Section: Total Revenue Requiredmentioning

confidence: 99%

Section: Process Facility Costmentioning

confidence: 99%

Section: Solubility Of Acid Gasesmentioning

confidence: 99%

Section: Figure 42 Simplified Selexol Processmentioning

confidence: 99%

See 3 more Smart Citations

Development and Application of Optimal Design Capability for Coal Gasification Systems

Rubin¹,

Rao²,

Berkenpas³

2007

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Pre-combustion carbon-capture technologies for power generation: an engineering-economic assessment

Lorenzo

Barbera

Ruggieri

et al. 2013

Int. J. Energy Res.

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SUMMARY An engineering‐economic analysis of the behaviours of each of two pre‐combustion gas‐turbine combined cycles with CO2 capture (an Integrated Gasification Combined Cycle (IGCC) and an Integrated Reforming Combined Cycle (IRCC)) is described. Their economic performances have been evaluated in terms of the break‐even electricity selling price. The results show that the proposed pre‐combustion power plant efficiency values (37% and 43.7% for the IGCC and the IRCC respectively) are significantly lower compared to a conventional plant value (55.3%). The CO2 emissions of the latter are less than half those of the conventional plant. Introducing an hypothetical carbon tax equal to 50£/tCO2, the break‐even selling price (BESP) for the proposed IGCC and IRCC plants is 4.40 p/kWh and 4.10 p/kWh respectively, while for the conventional plant amounts to 4.73 p/kWh. A sensitivity analysis has been carried out by varying the most influential investment parameters. The analysis has revealed that, considering the uncertainties associated with these key parameters, a substantial risk that the BESP could exceed the first value obtained is so prominent in some cases to alter their ranking order with respect to the most competitive technology. The final part of the analysis is a Monte‐Carlo simulation to determine the impact of simultaneous variations of all the variables, subject to uncertainty, on the break‐even selling unit price for the generated electricity. From the simulation, it derives that the BESP value ranges from 3.13 p/kWh to over 6.00 p/kWh for the IGCC case with a 50% probability of exceeding the first value obtained (4.40 p/kWh). In the IRCC case, the range of possible value for the BESP is from 2.85 p/kWh to 6.10 p/kWh, and there is a 60% probability that the actual BESP would exceed the first value obtained (4.10 p/kWh). Copyright © 2013 John Wiley & Sons, Ltd.

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