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Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy.

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Presentation on theme: "Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy."— Presentation transcript:

1 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Advanced energy systems Studio, modellizzazione e analisi di componenti e sistemi innovativi a bassa emissione di CO 2 per la conversione termomeccanica dell’energia Marco Gambini, Michela Vellini Dipartimento di Ingegneria Industriale Università di Roma “Tor Vergata”

2 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Introduction Environmental situation Increasing amounts of gases, such as CO 2, in the earth's atmosphere bring the risk of enhancing the natural greenhouse effect, leading to changes in the climate. Actual energy policy The size of climate changes and their impact are not fully understood. Nevertheless, it is generally accepted that the level of greenhouse gases in the atmosphere must be stabilised in order to prevent dangerous anthropogenic interference with the climate system. Power generation sector Fossil fuels are likely to play a major role in global energy supply and especially in power energy sector in the near-medium term future. But fossil fuel are also major source of anthropogenic CO 2 emission into the atmosphere. A strong abatement of these emissions must be achieved in these and in the next few years CO 2 mitigation options in power generation A broad range of options is available for reducing carbon dioxide emissions to the atmosphere. They are: improving the efficiency of energy use switching to less carbon-intensive fuel (e.g. from coal to natural gas) increasing the application of renewable energy sources and the nuclear power removal of CO 2 from fossil fuel power plants

3 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems CO 2 CAPTURE AND STORAGE It’s the most important option to reduce substantially carbon dioxide emissions. Capture and storage of CO 2 is now technically feasible. Carbon dioxide removal techniques The methodologies proposed up to now are: CO 2 removal process treating the products of combustion from conventional fossil fuel power plants or the process gases (option A) using semi-closed cycles where the working fluid is prevalently CO 2 ; the excess CO 2 produced in the combustion process is totally captured (option B) Fossil fuel decarbonization (option C)

4 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems G.I.ST. Cycle Study and proposal of new advanced power plants able to attain high performance and low ambient impact. G.I.ST. (Gas Injection Steam) is a new mixed cycle where there is a topping heating of steam by means of an internal combustion pressure drop during mixing steam and exhaust gases (process A-B) topping temperature of the cycle very high (point B) final point of expansion (point C) is superheated steam (together with incondesable gases) de-superheating of mixuture steam and incondensable gases after expansio (process C-D) condensation (separation and recovery of the water) not isothermal (process D-E).

5 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems G.I.ST. Cycle Efficiency: 38.3%  boiler /  tot : 74% m steam /m tot : 67% (by weight at SEP inlet) Conventional high pressure steam turbine Regenerative re-heating Bottoming cycle “bottoming cycle”, fed by heat of the mixture steam and incondensable gases at the exit of the medium pressure turbine

6 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems G.I.ST. Cycle Ciclo termodinamico del vapore (diagramma T,s)

7 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems G.I.ST. Cycle Profili di temperatura nel separatore

8 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems G.I.ST. Cycle (AMC) Efficiency: 57.0% m steam /(m air + m steam ): 25% (by weight) Gas-turbine with reheating and steam injection in the first combustion chamber Conventional high pressure steam turbine HRSG for steam production Atmospheric SEP for water recovery

9 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems G.I.ST. Cycle Ciclo termodinamico del vapore (diagramma T,s)

10 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems G.I.ST. Cycle Profili di temperatura nel separatore

11 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Study of unconventional components SEPARATOR Study of the thermodynamic process (cooling of wet gas), development of a proper numerical model

12 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Study of unconventional components for AMC WET GAS EXPANSION Study of the thermodynamic process (wet gas expansion), development of a proper numerical model

13 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Study of advanced components In questo caso l’ossigeno separato viene consegnato a 84 bar e temperatura ambiente ossia in condizioni supercritiche (p cO2 =50,4 bar e T cO2 =-118,6°C) e l’azoto a 21 bar e temperatura ambiente (p cN2 =33,9 bar, T cN2 =-147°C) allo stato gassoso.

14 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Study of advanced components

15 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Study of advanced components OTM technology is based on ceramic materials which can rapidly transport oxygen ions at 800 - 1000°C. The fraction of oxygen that a OTM system recovers from a given flow rate of feed air can be adjusted by varying one of the following parameters (assuming that membrane composition and thickness are fixed): feed air pressure (↑p f ↑ η O2 ) membrane temperature (↑T ↑σ ↑ η O2 ) permeate suction pressure (↓p p ↑ η O2 ) membrane area (↑A ↑ η O2 )

16 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Study of advanced components Formulation of mathematical problem A one-dimensional model has been set up in Matlab. During each step mass and heat transfer across the membrane are solved. Our scope is evaluating membrane area, considering the separation efficiency as an input data. If N is the number of control volumes chosen and n O2,f is the oxygen molar flow at feed inlet, the amount of oxygen permeated through each control volume is given by: Membrane area required in each control volume is related to oxygen flow through the membrane by means of the local permeation rate j O2 :

17 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Study of advanced components

18 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Study of advanced components

19 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems REFERENCE POWER PLANTS

20 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems REFERENCE POWER PLANT: IGCC Coal gasification island is composed of: coal treatment plant, gasifier syngas cooling and cleaning The syngas is then burned in the gas turbine combustor In order to use profitably heat from gasification island, more steam is produced by using Q 1 and Q 2. The optimal integration between gasification island and power section is developed by using the calculation model SuperTarget6, which performs the Pinch Technology

21 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems EXHAUST GAS TREATMENT EXHAUST GAS TREATMENT (chemical absorption) Chemical absorption It is the most suitable method for CO 2 separation when carbon dioxide has a low concentration (5- 15% by volume) in a gaseous stream at low pressure It consists of two steps: absorptionabsorption of CO 2 by chemical solvent at low temperature (40-65°C); recoveryrecovery of CO 2 from the chemical solvent by using low grade heat, (100-150°C). Liquefaction and dehydration compressioncompression is carried out in various steps by alternately compressing and cooling; final coolingfinal cooling reaches a temperature below the CO 2 critic temperature.

22 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems It consists of several steps: partial oxidation: methane, air and steam are introduced into a catalytic air-blown partial oxidation reactor where different chemical reactions take place: partial and total oxidation together with steam and CO 2 reforming of methane; shift reaction: converts CO to H 2 in order to produce a hydrogen-rich fuel gas; this reaction is exothermic and is accomplished in two stages; fuel gas purification: the CO 2 must be separated by a chemical process that consists of two steps:  absorption of CO 2 at low temperature by a proper solvent  recovery of CO 2 by using heat (to break the chemical bonds) CO 2 liquefaction: it is performed in various steps by compressing and cooling alternately HYDROGEN PRODUCTION BY METHANE DECARBONIZATION (partial oxidation)

23 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems It consists of several steps: steam methane reforming: methane and steam are introduced into a reformer where the endothermic steam methane reforming reaction takes place; external heat, needed to drive the reaction, can be provided by the combustion between a proper oxidizer and the final fuel; shift reaction: convert CO to H 2 in order to produce a hydrogen-rich fuel gas; this reaction is exothermic and is accomplished in two stages; fuel gas purification: the CO 2 must be separated by a chemical process that consists of two steps:  absorption of CO 2 at low temperature by a proper solvent  recovery of CO 2 by using heat (to break the chemical bonds) CO 2 liquefaction: it is performed in various steps by compressing and cooling alternately HYDROGEN PRODUCTION BY METHANE DECARBONIZATION (steam methane reforming)

24 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems It consists of several steps: gasification: coal-water slurry and oxygen react chemically in order to form a syngas which is composed of CO and H 2 mainly. Some chemical reactions are exothermic and provide heat to drive the endothermic ones; shift reaction: convert CO to H 2 in order to produce a hydrogen-rich fuel gas; this reaction is exothermic and is accomplished in two stages; fuel gas purification: the CO 2 must be separated by a physical process that consists of two steps:  absorption of CO 2 at high pressure by a proper solvent  recovery of CO 2 by lowering the pressure of the rich solvent CO 2 liquefaction: it is performed in various steps by compressing and cooling alternately HYDROGEN PRODUCTION BY COAL GASIFICATION (TEXACO TECHNOLOGY)

25 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems INTEGRATION OF REFERENCE POWER PLANTS AND EXHAUST GAS TREATMENT SECTION

26 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems INTEGRATION OF AMC PLANT AND EXHAUST GAS TREATMENT SECTION The performance of AMC is very interesting: an efficiency over 2 points higher than CC a CO 2 emission of about 0.04 kg/kWh

27 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems INTEGRATION OF REFERENCE POWER PLANT AND FOSSIL FUEL DECARBONIZATION SECTION (POX) The best power plant performance is attained when all the possible heat, discharged by the hydrogen production plant, is profitably used: all heat loads (Q 1, Q 2, Q 3 ) of the production plant can be put in the thermodynamic cycle in order to increase steam production steam, for the reactor and the CO 2 removal plant, is extracted at the suitable pressures from the steam turbines

28 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems INTEGRATION OF REFERENCE POWER PLANT AND FOSSIL FUEL DECARBONIZATION SECTION (SMR)  exhaust gases, at the gas turbine exit, are used in the reformer as oxidizer (they contain enough oxygen to do the combustion and they are also rather hot)  fuel to drive the reforming reaction is part of the total hydrogen rich fuel gas, the other part goes into the combustion chambers of the power plants  fuel at the reformer exit, before shift reactors, is used to heat the mixture steam-methane before reformer inlet  steam for reforming and CO 2 removal is extracted at 4 bars in the steam section of the power plant  steam for the reforming reaction is laminated until to the atmospheric pressure and mixed with natural gas  Q 3 is used to heat water from environmental condition up to return condensate condition

29 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems INTEGRATION OF REFERENCE POWER PLANT AND FOSSIL FUEL DECARBONIZATION SECTION (SMR)  the consumption of hydrogen rich fuel in the reformer is over 20%  overall efficiency is 44.02%  CO 2 emission is 0.0806 kg/kWh

30 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems INTEGRATION OF REFERENCE POWER PLANT AND FOSSIL FUEL DECARBONIZATION SECTION (CG) The best power plant performance is attained when all the possible heat, discharged by the hydrogen production plant, is profitably used: all heat loads (Q 1, Q 2, Q 3 ) of the production plant can be put in the thermodynamic cycle in order to increase steam production steam, for the reactor and the CO 2 removal plant, is extracted at the suitable pressures from the steam turbines warm water, to prepare water-coal slurry is generated by the intercooling heat of oxygen compression

31 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems TECHNICAL COMPARISON: overall efficiency (exhaust gas treatment vs fossil fuel decarbonization) coalwhen coal is used, the exhaust gas treatment (IGCC-R) penalizes plant performance very much, while energy results are better when coal decarbonization is performed: the specific work reduction is about 13% for the coal decarbonisation and about 20% for the exhaust gas treatment and overall efficiency decreases of about 7.5 percentage points for the CC-CG and over 9 percentage points for the IGCC-R; natural gaswhen natural gas is used, the exhaust gas treatment is the best solution in order to obtain low CO 2 emission and good performance (CC-R): efficiency reduction of about 5.5 percentage points. Vice versa, natural gas decarbonization is a very penalizing system to reduce CO 2 emissions

32 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems TECHNICAL COMPARISON: specific emissions (exhaust gas treatment vs fossil fuel decarbonization) CC-Rthe CC-R stands out because it exhibits the highest net efficiency and thus the lowest final specific CO 2 emission CC-CGthe CC-CG and the IGCC-R are the worst power plants because they have the lowest net efficiency, are fed by the most poor fuel and thus they have the highest final specific CO 2 emission coal fuel decarbonization natural gas exhaust gas treatment

33 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems ECONOMIC COMPARISON: kWh cost increase (exhaust gas treatment vs fossil fuel decarbonization) coalcoal: the economic penalizations are similar between the two CO 2 emission abetment methodologies: 41.5% for the IGCC-R and 34% for the CC-CG. Coal decarbonization seems to have major potential; natural gasnatural gas: the economic penalizations are very moderate only for the exhaust gas treatment (the kWh cost increase is about 18%). This result depends on the high overall efficiency of this solution and on the small increase of the total capital cost. The natural gas decarbonization (CC-POX and CC-SMR) shows similar increases (33.6% and 41.5% respectively) in comparison with coal decarbonization. In fact, even if the total capital costs become very high, the good overall efficiencies allow a positive limitation in the kWh cost increase

34 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems FINAL COMPARISONS (exhaust gas treatment vs fossil fuel decarbonization) in order to reduce CO 2 emissions when coal is used, the coal decarbonization must be implemented: in this case it is possible to attain 38% a global efficiency of about 38% 0.1117 kg/kWh a specific CO 2 emission of 0.1117 kg/kWh 34% an increase of kWh cost of about 34% vice versa, in order to reduce CO 2 emissions when natural gas is used, the exhaust gas treatment must be implemented: in this case it is possible to attain 50.7% a global efficiency of about 50.7% 0.0391 kg/kWh a specific CO 2 emission of 0.0391 kg/kWh 18% an increase of kWh cost of about 18%

35 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems EFFECTS OF FUEL AND OXIDIZER SWITCHING IN COMBINED CYCLES Using oxygen instead of air and hydrogen instead of natural gas the first consequence is a very high (and inadmissible) oxygen excess in the exhaust gases in order to obtain a fixed TIT (  15 and TIT=1250°C, the final oxygen fraction is over 87% by mass! ) A possible idea for reducing oxygen excess could be the subdivision of the total expansion and the addition of working fluid reheat between two consecutive expansions (like depicted in figure) Also in this way, it is not possible to limit properly the oxygen fraction at the plant discharge and, even if it could happen, there would be another problem: the working fluid, composed mainly of steam, is discharged into the environment at the HRSG exit and thus there is a great thermal loss related to this steam, discharged at ambient pressure.

36 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems EFFECTS OF FUEL AND OXIDIZER SWITCHING IN STEAM TURBINE TECHNOLOGY This is the AMC layout. Starting from the scheme it is possible to understand, qualitatively, the main modifications correlated to a change in the oxidizer and in the fuel:  limit the oxygen excess by steam injection in the combustion chamber  working fluid composed mainly of H 2 O it could be interesting to study the working fluid expansion until to pressures, typical of the conventional steam cycle. using hydrogen as fuel and oxygen as oxidizer, the thermodynamic solution is an internal combustion steam cycle (ICSC) where H 2 O (steam) plays a role of inert in the H 2 -O 2 combustion.

37 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems H 2 /O 2 CYCLES: first reference case  a fuel compression section with intercooling;  an oxidizer compression section with intercooling;  two gas turbines; in the MPT the working fluid is composed mainly of steam;  a steam turbine where there is the steam expansion before its injection in the combustion chamber;  a heat recovery steam generator for the steam generation and steam reheating;  an atmospheric separator in order to obtain the water separation and its recovery

38 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems  =30 TIT=1350°C W=5865 kJ/kg  =50.6% H 2 /O 2 CYCLES: first reference case performance

39 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems H 2 /O 2 CYCLES: second reference case  there will not be water separation in the last HRSG section (SEP)  there will be another steam turbine, LPT  there will be a “conventional” condenser where all the steam will condense: after, part of the water is sent into the HRSG and part is discharged into the environment This is the new layout:

40 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems  =70 TIT=1700°C W=8834 kJ/kg  =62.5% H 2 /O 2 CYCLES: second reference case

41 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems The main inlet are air and fossil fuel The emission outlet is located in the H 2 production plant (it is liquid CO 2 and gaseous CO 2 only for the reforming) and in the power section (the syngas is not pure hydrogen) The integration between the three systems is very simple: oxygen flow from ASU to power section and H 2 production plant (for gasification) hydrogen flow from H2 production plant to power section cycle work from power section to production plants in order to satisfy all mechanical auxiliaries. H 2 /O 2 CYCLE POWER PLANTS: overall performance evaluation Two performance parameters are defined: cycle efficiency overall efficiency

42 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems H 2 /O 2 CYCLE POWER PLANTS: overall results cycle efficiencies of power plants, coupled with coal gasification, are always greater than those of power plants, coupled with steam-methane reforming, because the first syngas is pressurized for the first reference case, cycle efficiencies attain a mean value of about 58%. The overall efficiencies are very low, especially those coupled with the steam methane reforming: the mean values are about 21% and over 28% for H 2 /O 2 cycle power plants based on steam methane reforming and coal gasification respectively. for the second reference case, cycle efficiencies attain a mean value of about 64%. The overall efficiencies are very low, especially those coupled with the steam methane reforming: the mean values are about 25% and 33% for H 2 /O 2 cycle power plants based on steam methane reforming and coal gasification respectively.

43 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Current research projects

44 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Current research projects

45 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Current research projects

46 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Current research projects

47 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Thank you for your attention

48 Università di Roma “Tor Vergata” PhD of Industrial Engineering - Research Activity on Energy Rome, 17 October, 2014 M. Gambini, M. Vellini – Advanced Energy Systems Study of unconventional components SEPARATORE D’ACQUA analisi termodinamica del processo di raffreddamento di un gas saturo; sviluppo di un modello di calcolo, sua validazione e applicazione. TURBINA A GAS SATURO D’ACQUA analisi termodinamica del processo di espansione di un gas saturo; sviluppo di un modello di calcolo in sede limite e reale e sua applicazione.


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