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ayout the best fluids are not of the drytoltuyenpee(41e.2x)clusively, but instead wet (ethanol) 360 ne) while c2-butene is vaguely dry. This indicates that dry fluids are dependent on a benzene (9.6) acetone (18.7) ethanol (14.4) toluene (41.2) (3b6e.n8z)ene (71.8) 8.0) ethanol (85.9) c-pentane (10.6) Process thermal efficiency % 360 0.98 m nce of having benzene (71.8) ethanol (85.9) toluene (12.7) acetone (47.2) e superior efficie3n0c0y. However, the difference in net power between the best fluid and ethanol (53.1) lternatives is minor (5-8%). 240 360 180 300 240 Table 3: Engine parameters Property Engine type Engine tuning method Load Cylinders Bore Stroke Turbocharger type Mean effective pressure c2-butene acetone ( 0 10 20 toluene (12.7) Unit - - % - 30 40 acetone (47.2) ethanol (53.1) 12 Exhaust temperature after turbocharger 284 cale systems). The consequences of a 20 bar limit on the cycle are up to 2.5% lowCerylindeetr cooling load 8570 Figure 4: Optimum fluid and pressure (bar) at temperatures from C kW gest decreases are seen at higher source temperatures. All fluids are of the dry type, and entiontahnedipmrepssourrteasnacreobfelhowavtihnegirarersepdeuctcievdecbrioticlearlpreesssuurerse..DrOeF2si,cghu7re2e.r85%e:tONapl2t.i,m9[u4.4m]%mfluCeindOta2inoadnpdre5s.s5u%reH(b2aOr).attemperatures and cost concerns. Lai et al. [15] mention that the 20 bar limit has come from legal main if one of the hazard types was at a higher level than atl w their respective critical pressures. ◦ froFmlu1i8d0ctaon3d6i0daCtewsiwtherliemditisocfar2d0ebdarfronmhtighhepsroelsustuiroen. do- LP et hy l uids and up to 6% for the third best fluids compared to when the limit is 120 bar; see mm (7.5) hexane (14.8) a pressure limit of 120 bar and LP+SI) where the simple -c -he x an e (12 .9 ) 240 hexane (14.8) 180 Fuel flow rate 3.5 kg/s Air flow rate 169.6 kg/s Scavenge air pressure 4.10 bar recuperator, LP) a high pressure limit of 20 bar with recu- LP) a high pressure limit of 20 bar with recupera- perator, SI) a simple plant layout without recuperator and tor, SI) a simple plant layout without recuperator Value 12K98ME-C7 Part load 100 benzene (20.0) sure (bar) at temper 180 acetone (8.0) benzene (9.6) acetone (18.7) High efficiency - 19.2 bar ◦ methyl-c-hexane (12.9) :Optimumfluidandpresaturesfrom180to360Cwithnorecuperator.Nominalenginespeed104rpm c2-butene (36.8) ethanol (14.4) 300 octane (9.3) s mention the importa ety and cost concerns0. Lai et10al. [152]0mentio3n0that t4h0e 20 bar limit has come from legal i-hexane (18.9) Scavenge air temperature 37.0 ◦C Maximum continuous rating 72240 kW Maximum pressure 151 bar Mean effective pressure 19.2 bar a reduced boiler pressure. Drescher et al. [4] Fmuelnlotwioenr heating value 42700 kJ/kg c-pentane (10.6) mm (7.5) heptane (20.0) c-hexane (20.0) 2.40 m toluene (20.0) rtain countries. Kuo et al.P[r2o0c]easrsgtuheerfomraal eliffimcitieonfcy25%bar in order to keep material choexsatnse (6.1) c-pentane (9.5) Exhaust flow rate 173.1 kg/s i-hexane (7.4) ◦ 0 2 4 6 8 10 12 ptimumfluidandp◦ressure(bar)attemperaturesfrom180to360◦Cwithnorecuperator. t fluids a1n8d0 tuop36t0oC6%witfhonrotrheecutpheirradtorb.est fluids compared to when the limit is 120 bar; see Net power output MW gas enthalpy and the mass composition used was: 12.2% al. [20] argue for a in countries. Kuo et e systems). The consequences of a 20 b 300 c-hexane (20.0) a specified maximum. Figure 6 shows the cycle thermal benzene (20.0) tive tion and Wit mul 360 limit of 25 bar in order to keep material costs a toluene (20.0) efficiency for each of the hazard levels under the follow- r l i m octane (9.3) heptane (20.0) n t h m i t o hazard levels under the following constraints: NO) inaghciognhstprarienstsu:rNeOli)maithiogfh1p2r0essbuarre lwimitiht orfe1cu20pebraartworit,h e cycle are up to 2.5% lower net t higher sourc and a pressure limit of 120 bar and LP+SI) where tdecreasesarese2e4n0aetemperatures.Allfluidsareofthedrytype,and1, i-hexane (18.9) heir respective critical pressures. c-pentane (9.5) the simple plant is limited to 20 bar. 0.25 0.2 44 R 3ar tob cies flui ord out whe rec mis tob R imu the tain glo stro tha the (wi F sam sur eral 3.2. A erty for 180 360 300 hexane (6.1) i-hexane (7.4) 0 c-hexane (20.0) 30 benz4e0ne (20.0) 10 20 Process thermal efficiency % Figure 5: Optimum fluid and pressure (bar) at tem◦peratures from m fluid and pressure (bar) at temperatures from 180 to 360 C with limit of 20 bar on high pressure. 180 to 360◦C with limit of 20 bar on high pressure. mm (7.5) 240 3.2. Engine design point two-stroke die0sel eng1in0e is pr2e0sented3i0n the f4o0llowing case. The heat source is 284◦C hot exhaust gas which leaves the ◦ Process thermal efficiency % system at 160 C to prevent excessive corrosion in heat ex- NO LP SI LP+SI 10 no significant decreases are observed when moving [22]. For the sake of computational efficiency, only the main species were included in the calculation of exhaust 6 hazard level 2 the thermal efficiencies are markedly lower toluene (20.0) methyl-c-hexane (12.9) octane (9.3) heptane (20.0) hexane (14.8) i-hexane (18.9) 0.15 0.1 c-pentane (9.5) hexane (6.1) An op1t8i0misation of the process at the expected design i-hexane (7.4) plant is limited to 20 bar. point conditions for a MAN10Diesel and Turbo low speed 4321 Maximum hazard level changers. The resulting heat transfer fluid temperatures are 255◦C at the inlet and 129◦C at the outlet of◦ the boiler. fluid and pressure (bar) at temperatures from 180 to 360 C with limit of 20 bar on high pressure. The engine data shown in Table 3 was acquired from the MAN engine room dimensioning software [19] and the cor- responding engine project guide [20]. The exhaust gas composition was found using a marine engine model derived in previous work of the authors [21], which uses a methodology derived by Rakopoulus et al. Figure 6: Effects of constraints and hazard levels Figure 6: Effects of constraints and hazard levels As shoownnininthtehfiegfiugreu,rteh,eththeertmhearlmeffialcieffinccieies,ncaicerso,ss caoncrsotrsasinctosn, astrreagienntesr,aallryedgeecrneearsainllgyadsetchreealslionwgedashatzhaerd levels are decreasing. In general, no significant decreases allowed hazard levels are decreasing. In general, are observed when moving from hazard level 4 to 3. At from hazard level 4 to 3. At hazard level 2 the ther- under all constraints and the same pattern is seen when mal efficiencies are markedly lower under all con- moving to hazard level 1. straints and the same pattern is seen when moving to hazard level 1. Requiring a limited maximum pressure of 20 bar is seen to cause modestly reduced efficiencies com- pared to the SI constraint. At levels 4 and 3, the 7 o v a e m o a c e l a sw t u % e d e p u e m b t t o e . m Heat source temperature ◦C ◦ Heat source temperature C Heat source temperature ◦C ◦ Heat source temperature C Thermal efficiency (ηth) Heat source temperature ◦CPDF Image | organic Rankine cycles for waste heat recovery in marine settings
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