Natural gas fired combined cycle power plant with CO2 capture

A natural gas (NG) fired power plant is designed with virtually zero emissions of pollutants, including CO₂. The plant operates in a gas turbine-steam turbine combined cycle mode. NG is fired in highly enriched oxygen (99.7%) and recycled CO₂ from the flue gas. Liquid oxygen (LOX) is supplied by an on-site air separation unit (ASU). By cross-integrating the ASU with the CO₂ capture unit, the energy consumption for CO₂ capture is significantly reduced. The exergy of LOX is used to liquefy CO₂ from the flue gas, thereby saving compression energy and also delivering product CO₂ in a saleable form. By applying a new technique, the gas turbine efficiency is increased by about 2.9%. The net thermal efficiency (electricity out/heat input) is estimated at 45%, compared to a plant without CO₂ capture of 54%. However, the relatively modest efficiency loss is amply compensated by producing saleable byproducts, and by the virtue that the plant is pollution free, including NO_x, SO₂ and particulate matter. In fact, the plant needs no smokestack. Besides electricity, the byproducts of the plant are condensed CO₂, NO₂ and Ar, and if operated in cogeneration mode, steam.     

集成小型堆和可再生能源的超临界CO2循环发电系统

  [目的]  小型模块化压水堆(小型堆)核电站由于温度参数低,其发电效率不到30%,为了提高小型堆的核能利用效率,可将小型堆与可再生能源组合,并以先进的超临界CO₂循环作为热能转换为电能的装置。  [方法]  基于简单回热模式的超临界CO₂循环,并在此基础上增加一次间冷和一次再热,将小型堆与太阳能、生物质能热源集成为新型混合发电系统,对其发电效率进行了分析。  [结果]  结果表明:对于高压透平入口温度390 ℃的系统,发电效率34.13%,对于高压透平入口温度550 ℃的系统,发电效率41.22%。此外,对系统的安全性分析表明:CO₂本身是具备核安全属性的工质,并且超临界CO₂循环还可以作为反应堆的非能动余热排出系统,确保在严重事故工况下,反应堆持续排出衰变热。  [结论]  集成小型堆和可再生能源的超临界CO₂循环发电系统具备良好的发电效率和核安全性。     

燃气-超临界CO2联合循环发电系统

  [目的]  燃气轮机排气温度高,可增加底循环,利用排气的余热发电,从而提高燃料总的能量利用率。鉴于超临界CO₂循环热效率高,并且具有系统简单、结构紧凑、运行灵活等潜在优势,可与燃气轮机组成新型的燃气-超临界CO₂联合循环。  [方法]  为了充分利用燃气轮机排气余热,提出在简单回热超临界CO₂循环的基础上,再嵌套一个简单回热循环的布置方式,并以PG9351(FA)型燃气轮机为例,对其热效率进行了计算分析。同时,在系统中增加余热利用装置,可将剩余热量用于供热、转换为冷量或发电。  [结果]  结果表明:对于选定的燃气轮机,超临界CO₂循环最高温度可达约600 ℃,循环发电效率约32%,获得余热温度为170 ℃以上,余热热量占燃气轮机排气热量9%,联合循环发电效率约54%。  [结论]  燃气-超临界CO₂联合循环发电系统具有较高的热效率,并且保留部分较高品位的余热,可进一步用于电厂运行。     

Effects of future fossil fuel use on CO2 levels in the atmosphere

A model based on fossil fuel use per capita and United Nations population predictions has been developed to predict global fossil fuel use and the resulting levels of CO₂ in the atmosphere. The results suggest levels of CO₂ will increase to between 415 and 421 ppm by 2025. Countries with energy-intensive economies will be responsible for the majority of CO₂ emissions, while nations with large populations but low energy consumption per capita will have less of an effect. A major increase in nuclear power generation will not have a significant impact on CO₂ levels over this time scale.     

Cost effective integration of hydrogen in energy systems with CO2 constraints

The integration of hydrogen in national energy systems is illustrated in four extreme scenarios, reflecting four technological mainstreams (energy conservation, renewables, nuclear and CO₂ removal) to reduce C emissions. Hydrogen is cost-effective in all scenarios with higher CO₂ reduction targets. Hydrogen would be produced from fossil fuels, or from water and electricity or heat, depending upon the scenario. Hydrogen would be used in the residential and commercial sectors and for transport vehicles, industry, and electricity generation in fuel cells. At severe (50–70%) CO₂ reduction targets, hydrogen would cost-effectively supply more than half of the total useful energy demands in three out of four scenarios. The marginal emission reduction costs in the CO₂ removal scenario at severe CO₂ reduction targets are DFL 200/tCO₂ (ca $ 100/t). In the nuclear, renewable and energy conservation scenarios these costs are much higher. Whilst the fossil fuel scenario would be less expensive than the other scenarios, the possibility of CO₂ storage in depleted gas reservoirs is a conditio sine qua non.     

Decomposition analysis of CO2 emission intensity between oil-producing and non-oil-producing sub-Saharan African countries

The need to decompose CO₂ emission intensity is predicated upon the need for effective climate change mitigation and adaptation policies. Such analysis enables key variables that instigate CO₂ emission intensity to be identified while at the same time providing opportunities to verify the mitigation and adaptation capacities of countries. However, most CO₂ decomposition analysis has been conducted for the developed economies and little attention has been paid to sub-Saharan Africa. The need for such an analysis for SSA is overwhelming for several reasons. Firstly, the region is amongst the most vulnerable to climate change. Secondly, there are disparities in the amount and composition of energy consumption and the levels of economic growth and development in the region. Thus, a decomposition analysis of CO₂ emission intensity for SSA affords the opportunity to identify key influencing variables and to see how they compare among countries in the region. Also, attempts have been made to distinguish between oil and non-oil-producing SSA countries. To this effect a comparative static analysis of CO₂ emission intensity for oil-producing and non oil-producing SSA countries for the periods 1971–1998 has been undertaken, using the refined Laspeyres decomposition model. Our analysis confirms the findings for other regions that CO₂ emission intensity is attributable to energy consumption intensity, CO₂ emission coefficient of energy types and economic structure. Particularly, CO₂ emission coefficient of energy use was found to exercise the most influence on CO₂ emission intensity for both oil and non-oil-producing sub-Saharan African countries in the first sub-interval period of our investigation from 1971–1981. In the second subinterval of 1981–1991, energy intensity and structural effect were the two major influencing factors on emission intensity for the two groups of countries. However, energy intensity effect had the most pronounced impact on CO₂ emission intensity in non-oil-producing sub-Saharan African countries, while the structural effect explained most of the increase in CO₂ emission intensity among the oil-producing countries. Finally, for the period 1991–1998, structural effect accounted for much of the decrease in intensity among non-oil-producers, while CO₂ emission coefficient of energy use was the major force driving the decrease among oil-producing countries. The dynamic changes in the CO₂ emission intensity and energy intensity effects for the two groups of countries suggest that fuel switching had been predominantly towards more carbon-intensive production in oil-producing countries and less carbon-intensive production in non-oil-producing SSA countries. In addition to the decomposition analysis, the article discusses policy implications of the results. We hope that the information and analyses provided here would help inform national energy and climate policy makers in SSA of the relative weaknesses and possible areas of strategic emphasis in their planning processes for mitigating the effects of climate change.     

Thermo-economic analysis of a direct supercritical CO2 electric power generation system using geothermal heat

A comprehensive thermo-economic model combining a geothermal heat mining system and a direct supercritical CO₂ turbine expansion electric power generation system was proposed in this paper. Assisted by this integrated model, thermo-economic and optimization analyses for the key design parameters of the whole system including the geothermal well pattern and operational conditions were performed to obtain a minimal levelized cost of electricity (LCOE). Specifically, in geothermal heat extraction simulation, an integrated wellbore-reservoir system model (T2Well/ECO2N) was used to generate a database for creating a fast, predictive, and compatible geothermal heat mining model by employing a response surface methodology. A parametric study was conducted to demonstrate the impact of turbine discharge pressure, injection and production well distance, CO₂ injection flowrate, CO₂ injection temperature, and monitored production well bottom pressure on LCOE, system thermal efficiency, and capital cost. It was found that for a 100 MW_e power plant, a minimal LCOE of $0.177/kWh was achieved for a 20-year steady operation without considering CO₂ sequestration credit. In addition, when CO₂ sequestration credit is $1.00/t, an LCOE breakeven point compared to a conventional geothermal power plant is achieved and a breakpoint for generating electric power generation at no cost was achieved for a sequestration credit of $2.05/t.     

A coal-fired power plant integrated with biomass co-firing and CO2 capture for zero carbon emission

A promising scheme for coal-fired power plants in which biomass co-firing and carbon dioxide capture technologies are adopted and the low-temperature waste heat from the CO₂ capture process is recycled to heat the condensed water to achieve zero carbon emission is proposed in this paper. Based on a 660 MW supercritical coal-fired power plant, the thermal performance, emission performance, and economic performance of the proposed scheme are evaluated. In addition, a sensitivity analysis is conducted to show the effects of several key parameters on the performance of the proposed system. The results show that when the biomass mass mixing ratio is 15.40% and the CO₂ capture rate is 90%, the CO₂ emission of the coal-fired power plant can reach zero, indicating that the technical route proposed in this paper can indeed achieve zero carbon emission in coal-fired power plants. The net thermal efficiency decreases by 10.31%, due to the huge energy consumption of the CO₂ capture unit. Besides, the cost of electricity (COE) and the cost of CO₂ avoided (COA) of the proposed system are 80.37 $/MWh and 41.63 $/tCO₂, respectively. The sensitivity analysis demonstrates that with the energy consumption of the reboiler decreasing from 3.22 GJ/tCO₂ to 2.40 GJ/ tCO₂, the efficiency penalty is reduced to 8.67%. This paper may provide reference for promoting the early realization of carbon neutrality in the power generation industry.     

下吸式固定床的生物质O2/CO2分段气化流程模拟

建立干桦木屑在下吸式固定床气化炉中的Aspen Plus气化模型,该模型预测煤气组成和煤气热值,与文献试验结果吻合良好。利用灵敏度分析模块模拟了氧碳比、CO₂/C对气化结果的影响,并提出O₂/CO₂分段气化流程,对比常规的CO₂气化特征,分析了CO₂/C对气化结果的影响。结果表明,纯氧气化时可获得高H₂和CO浓度的气化气,但其净CO₂排放量较高,氧碳比增加使碳转化率逐渐增加、冷煤气效率先增加后降低;CO₂作为气化剂时,随着CO₂/C的增加,净CO₂排放量逐渐减少,但碳转化率及冷煤气效率大幅降低;与常规CO₂气化相比,O₂/CO₂分段气化在保持低CO₂排放量的同时,可有效增加气化过程中的碳转化率及冷煤气效率。     

水合物法分离CO2工艺研究进展

随着温室效应加剧,CO₂减排行动已迫在眉睫。水合物法分离CO₂工艺作为一种发展前景广阔的新型CO₂分离技术,为CO₂减排提供了一种解决思路。水合物法分离CO₂工艺相比于化学吸收、物理吸附、深冷分离和膜分离等技术具有分离效率高、过程简单无副产物、条件温和的优势,为减缓CO₂排放增加对环境造成的影响提供了一个中短期解决方案,以此为前提将允许人类继续使用化石燃料直至可再生能源技术广泛应用。本文综合分析了国内外的相关文献,介绍了水合物法分离CO₂工艺的基本原理,并比较了水合物法分离CO₂不同工艺的优劣之处,为进一步优化水合物法分离CO₂工艺提供指导。     

CO2 utilization options, part II: Assessment of dimethyl carbonate production

In this paper, the potential to reduce CO₂ emissions from dimethyl carbonate production by switching from the traditional phosgene-based production to a urea-based CO₂ utilization process is assessed. The total CO₂ emission for each process is estimated, including emissions related to the carbon content of the products, energy consumption in the production process, and energy consumption in the production processes of the required reactants. Implementation of the CO₂ utilization process probably will reduce total CO₂ emissions. However, in order to achieve substantially reduced CO₂ emissions, serious consideration must be given to the optimization and design of the CO₂ utilization process. Furthermore, the fuel-mix employed is one of the factors that influences the total CO₂ emission the most.     

下吸式固定床的生物质H2O/CO2气化数值模拟研究

利用Aspen Plus 软件建立干桦木屑在下吸式固定床气化炉中的气化模型,模拟值与文献实验值吻合良好。利用Aspen Plus的灵敏度分析模块模拟分别以水蒸气（H₂O）和二氧化碳（CO₂）为气化剂时气化剂/生物质碳比（GC值）对气化结果的影响,并结合H₂O、CO₂各自的特点研究其复合气化。结果表明,H₂O气化时可获得富氢煤气,但其净CO₂排放量较高;CO₂气化时碳转化率及冷煤气效率较低,但净CO₂排放量较低;H₂O、CO₂复合气化使碳转化率及冷煤气效率略有降低,但可有效减少气化系统中的净CO₂排放量。     

Sequestration of CO2 in geological media in response to climate change: capacity of deep saline aquifers to sequester CO2 in solution

Geological sequestration is a means of reducing anthropogenic atmospheric emissions of CO₂ that is immediately available and technologically feasible. Among various options, CO₂ can be sequestered in deep aquifers by dissolution in the formation water. The ultimate CO₂ sequestration capacity in solution (UCSCS) of an aquifer is the difference between the total capacity for CO₂ at saturation and the total inorganic carbon currently in solution in that aquifer, and depends on the pressure, temperature and salinity of the formation water. Assuming non-reactive aquifer conditions, the current carbon content is calculated using standard chemical analyses of the formation waters collected by the energy industry on the basis of the concentration of carbonate and bicarbonate ions. Formation water analyses performed at laboratory conditions are brought to in situ conditions using a geochemical speciation model to account for dissolved gasses that are lost from the water sample. To account for the decrease in CO₂ solubility with increasing water salinity, the maximum CO₂ content in formation water is calculated by applying an empirical correction to the CO₂ content at saturation in pure water. The UCSCS in an aquifer is calculated by considering the effect of dissolved CO₂ on the formation water density, the aquifer thickness and porosity to account for the volume of water in the aquifer pore space and for the mass of CO₂ dissolved in the water currently and at saturation. The methodology developed for estimating the ultimate CO₂ sequestration capacity in solution in aquifers has been applied to the Viking aquifer in the Alberta basin in western Canada. Considering only the region where the injected CO₂ would be a dense fluid, the capacity of the Viking aquifer to sequester CO₂ in solution in the formation water is calculated to be 100 Gt. Simple estimates then indicate that the capacity of the Alberta basin to sequester CO₂ dissolved in the formation waters at depths greater than 1000 m is on the order of 4000 Gt CO₂. The results also show that using geochemical models to bring the analyses of the formation waters to in situ conditions is not warranted when the current total inorganic carbon (TIC) in the aquifer water is very small by comparison with the CO₂ solubility at saturation. Furthermore, in such cases, the current TIC may even be neglected.     

Pilot scale autothermal gasification of coconut shell with CO2-O2 mixture

This paper explored the feasibility and benefit of CO₂ utilization as gasifying agent in the autothermal gasification process. The effects of CO₂ injection on reaction temperature and producer gas composition were examined in a pilot scale downdraft gasifier by varying the CO₂/C ratio from 0.6 to 1.6. O₂ was injected at an equivalence ratio of approximately 0.33–0.38 for supplying heat through partial combustion. The results were also compared with those of air gasification. In general, the increase in CO₂ injection resulted in the shift of combustion zone to the downstream of the gasifier. However, compared with that of air gasification, the long and distributed high temperature zones were obtained in CO₂-O₂ gasification with a CO₂/C ratio of 0.6–1.2. The progress of the expected CO₂ to CO conversion can be implied from the relatively insignificant decrease in CO fraction as the CO₂/C ratio increased. The producer gas heating value of CO₂-O₂ gasification was consistently higher than that of air gasification. These results show the potential of CO₂-O₂ gasification for producing high quality producer gas in an efficient manner, and the necessity for more work to deeply imply the observation.     

Multi-objective optimization of an advanced combined cycle power plant including CO2 separation options

This paper illustrates a methodology developed to facilitate the analysis of complex systems characterized by a large number of technical, economical and environmental parameters. Thermo-economic modeling of a natural gas combined cycle including CO₂ separation options has been coupled within a multi-objective evolutionary algorithm to characterize the economic and environmental performances of such complex systems within various contexts.

The method has been applied to a case of power generation in Germany. The optimum options for system integration under different boundary conditions are revealed by the Pareto Optimal Frontiers. Results show the influence of the configuration and technical parameters on the electrical efficiencies of the Pareto optimal plants and their sub-systems. The results provide information on the relationship between power generation cost and CO₂ emissions, and allow sensitivity analyses of important economical parameters like natural gas and electricity prices. Such a tool is of interest for power generation technology suppliers, for utility owners or for project investors, and for policy makers in the context of CO₂ mitigation schemes including emission trading.     

Basic experimental results of liquid CO2 injection intothe deep ocean

CO₂ disposal in the deep ocean is expected to be an effective option for mitigating the increase in CO₂ on the earth. The authors have investigated the behaviour of liquid CO₂ using test facilities which can simulate the pressure and temperature of the deep ocean. Phase equilibrium data of the CO₂ -seawater system and the conditions of CO₂ clathrate formation were confirmed. In addition, the authors measured the pH value of seawater saturated with CO₂ at high pressure. The data presented in this paper are considered indispensable for evaluating the possibility of CO₂ disposal in the deep ocean     

Solar energy in photosynthesis

Solar energy provides the reducing power within green leaves to convert CO₂ and H₂O into sugars. The CO₂ is supplied by the atmosphere and enters the leaf by diffusion. Factors affecting the rate of photosynthesis must either change the CO₂ diffusive resistances or the CO₂ concentration gradient along the diffusion pathways. Therefore, these effects can be described in terms of diffusive control mechanisms.

Light affects CO₂ diffusion by initiating photosynthesis, which removes CO₂ at the chloroplast and establishes a diffusion gradient. Light also triggers stomatal opening, thereby sharply decreasing the diffusive resistance. However, intense radiation can cause desiccation of stomatal guard cells, a mechanism whereby the diffusive resistance increases.

During illumination, leaf cells have both a source (respiration) and sink (photosynthesis) for CO₂. Respiration in some species appears to be greatly stimulated by light. This additional internal CO₂ flux is a possible reason for a lower efficiency of energy utilization than in species whose respiration is not enhanced by light.

Physiological growth responses or movements often occur that position leaves in the light. Plants lacking this capability are often excluded in ecological succession in nature.     

Atmospheric stabilization of CO2 emissions: Near-term reductions and absolute versus intensity-based targets

This study analyzes CO₂ emissions reduction targets for various countries and geopolitical regions by the year 2030 to stabilize atmospheric concentrations of CO₂ at 450 ppm (550 ppm including non-CO₂ greenhouse gases) level. It also determines CO₂ intensity cuts that would be required in those countries and regions if the emission reductions were to be achieved through intensity-based targets without curtailing their expected economic growth. Considering that the stabilization of CO₂ concentrations at 450 ppm requires the global trend of CO₂ emissions to be reversed before 2030, this study develops two scenarios: reversing the global CO₂ trend in (i) 2020 and (ii) 2025. The study shows that global CO₂ emissions would be limited at 42 percent above 1990 level in 2030 if the increasing trend of global CO₂ emissions were to be reversed by 2020. If reversing the trend is delayed by 5 years, global CO₂ emissions in 2030 would be 52 percent higher than the 1990 level. The study also finds that to achieve these targets while maintaining expected economic growth, the global average CO₂ intensity would require a 68 percent drop from the 1990 level or a 60 percent drop from the 2004 level by 2030.     

A comparison of electricity and hydrogen production systems with CO2 capture and storage—Part B: Chain analysis of promising CCS options

Promising electricity and hydrogen production chains with CO₂ capture, transport and storage (CCS) and energy carrier transmission, distribution and end-use are analysed to assess (avoided) CO₂ emissions, energy production costs and CO₂ mitigation costs. For electricity chains, the performance is dominated by the impact of CO₂ capture, increasing electricity production costs with 10–40% up to 4.5–6.5 €ct/kWh. CO₂ transport and storage in depleted gas fields or aquifers typically add another 0.1–1 €ct/kWh for transport distances between 0 and 200 km. The impact of CCS on hydrogen costs is small. Production and supply costs range from circa 8 €/GJ for the minimal infrastructure variant in which hydrogen is delivered to CHP units, up to 20 €/GJ for supply to households. Hydrogen costs for the transport sector are between 14 and 16 €/GJ for advanced large-scale coal gasification units and reformers, and over 20 €/GJ for decentralised membrane reformers. Although the CO₂ price required to induce CCS in hydrogen production is low in comparison to most electricity production options, electricity production with CCS generally deserves preference as CO₂ mitigation option. Replacing natural gas or gasoline for hydrogen produced with CCS results in mitigation costs over 100 €/t CO₂, whereas CO₂ in the power sector could be reduced for costs below 60 €/t CO₂ avoided.     

CO2 utilization options, Part I: An emission assessment framework

The utilization of CO₂ in various products and services must be carefully assessed in order to achieve reduced CO₂ emissions and simultaneously to add to the net economic benefit of society. In this paper, a framework for the assessment of CO₂ utilization options in the chemical industry is outlined in which the total CO₂ emission is estimated in four steps. First, the processes under study are surveyed to establish the consumption of different raw materials (reactants). Second, the CO₂ emission due to the content of fossil carbon in the reactants is determined, i.e. the material-related emission. Third, the CO₂ emission related to energy consumption in the studied processes is estimated, i.e. the direct energy-related emission. Fourth, the CO₂ emission related to energy consumption in the reactant production processes is estimated, i.e. the indirect energy-related emission.