ISS (Isotope Separation System) 초저온증류공정시뮬레이션 공주대학교화학공학부조정호
목 차 1. ISS(Isotope Separation System) 소개 2. ITER ISS 평형반응기 3. 헬륨냉동사이클 4. Pure Component Properties 5. ITER ISS 공정시뮬레이션 Case 1 6. ITER ISS 공정시뮬레이션 Case 2 7. ITER ISS 공정시뮬레이션 Case 3 2
3. 헬륨냉동사이클 3
3. 헬륨냉동사이클 He Refrigeration Cycle (nominal operation temperature between 20-24 K) EU Contribution to ITER Fuel Cycle, Alain Teissier, IBF 2013 4
3. 헬륨냉동사이클 4.5 K Helium refrigeration unit 대기압에서끓는점이 4.22K(-268.96 ) 인헬륨을냉매로이용하여초저온수소동위원소분리에냉매로이용함 헬륨을 320K 에서 14 K 까지낮춤 Helium Refrigeration Cycle 수소동위원소를분리하기위한증류조건은초저온 (~30K) 에서운전되므로, 위해사용되는헬륨냉동기는수소동위원소분리를위한헬륨냉동기의용량은 1,800W 정도이다. 1bar 에서 22bar 까지압축 14 K 까지온도가낮아진헬륨을사용해열교환함 5
3. 헬륨냉동사이클 ISS 14K~ 30K 1) Helium Expansion Tank 2) Helium Screw Compressors 3) Helium Refrigerator 4) Cryogenic Distillation Cold Box Cold Box 6
3. 헬륨냉동사이클 Refrigeration Process Operating Pressure Determination Considering the compression efficiency which was applied to 2-stage compression system 22.0 bar 6.0 bar 11.5 bar Expansion Turbine Compression Ratio= 7 C/W (Given the temperature in summer season in Korea, which is assumed to be cooled down to 45 ) n P 1/ d P s
3. 헬륨냉동사이클 Determining the optimum operating pressure from helium refrigeration process P2 7.0 P1 P2 P1 Compression ratio 6.5 6.0 5.5 5.0 4.5 4.0 From operating pressure of 22 bar or more, to a pressure increase, compression ratio reduction rate is very low. if it s operating in 22 bar or more, it s inefficient. 3.5 Decreasing Compressor power required 3.0 5 10 15 20 25 30 35 C03 outlet pressure (bar) 8
3. 헬륨냉동사이클 311 K 5.6 bar 18 K 6.2 bar 311 K 5.6 bar 453 K 22.0 bar 318 K 21.7 bar 14 K 6.5 bar 30 K 21.4 bar 26 K 21.1 bar 9
3. 헬륨냉동사이클 311 K 5.6 bar 18 K 6.2 bar 318 K 21.7 bar 30 K 21.4 bar 22 K 20.8 bar 14 K 6.5 bar 26 K 21.1 bar 10
M01 V01 CD1 EQ1 E02 CD2 EQ2 V02 SP01 E03 EQ6 EQ3 E05 P03 P02 P01 EQ4 P04 CD3 E06 CD4 EQ7 P05 V05 EQ5 P06 V06 V04 P07 V07 P08 V08 P09 P10 V09 MX01 1 2 3 4 5 6 8 11 9 4A 9B 11A 7 24 12 25 16 14 10 13 27 22 23 15B 14A 24A 25A 26 18 20 16A 28 29 19 30 21 15C 9C 24B 25B 17 V10 MIXER MIXER 3. 헬륨냉동사이클 11
3. 헬륨냉동사이클 12
3. 헬륨냉동사이클 Oil Flooded Screw Compressor Oil Removal + Gas Management Helium Refrigerator Cold Box 27K 24K 23K 14K Reboiler Condenser 13
3. 헬륨냉동사이클 30K 26K 18K 14K Reboiler Condenser Stream Number 5 6 10 11 Stream Name Reboiler Inlet Reboiler Outlet Condenser Inlet Condenser Outlet Temperature (K) 30.00 26.00 14.05 18.08 Pressure (ATM) 20.00 20.00 6.25 6.25 Phase Vapor Vapor Vapor Vapor Total Molar Rate (KG-MOL/HR) 113.18 113.18 128.58 128.58 Total Mass Rate (KG/HR) 453.00 453.00 514.66 514.66 Flow rate (kmol/hr) Percent (mol%) Flow rate (kmol/hr) 14 Percent (mol%) Flow rate (kmol/hr) Percent (mol%) Flow rate (kmol/hr) Percent (mol%) Helium 113.18 100.00 113.18 100.00 128.58 100.00 128.58 100.00
PRO/II 를활용한냉동사이클공정모사방법 15
Refrigeration cycle Example Problem. 프로판을냉매로사용하여증기재압축냉동사이클에대한전산모사를수행하고자한다. 액화하고자하는원료는다음의표와같다. 원료스트림의액화후온도는 -30 이다. 액화하고자하는원료조건 Component Mole% Propane 7.80 Iso-Butane 49.08 N-Butane 43.12 Temperature ( ) 25.0 Pressures (bar) 1.2 Flow rate (kg/hr) 15,078 냉매로는순수한프로판을사용한다. 냉매응축기에서 2 차냉매로써냉각수를사용하며, 공급온도는 32 이고회수온도는 37 이다. 2 차냉매에의해프로판은 45 까지응축되고응축기압력강하는 0.5 bar 가정. 냉매가증발기로주입되는온도는 -40 이다. 열역학모델식 Peng-Robinson 상태방정식적용 16
Problem: 1 증기재압축냉동사이클의개요도를그리고, 개략적으로설명하라. 단, 팽창밸브후단의 Two-phase flow 는기액분리를위해서 Flash drum 을설치한다. 17
Problem 1: 냉동사이클개요도 Refrigeration Cycle Diagram Compressor Condenser Evaporator Expansion Valve 18
증기재압축을이용한냉동사이클의기본원리 Compressor Condenser P C D A T A T D D Evaporator P A, P D Expansion Condensation T B =T C B Expansion Valve A P B, P C B Evaporation H evap C Refrigeration Cycle Diagram Pressure Enthalpy Diagram H Refrigeration Cycle Step : A B C D Expansion Evaporation Compression Condensation 19
Problem 2 증발기의 heat duty 를결정하라. 20
Problem 2: 증발기의 heat duty 결정 21
Problem 2: 증발기의 heat duty 결정 증발기의 heat duty ------------------------------------------------------- UNIT 1, 'EVAPORATOR' OPERATING CONDITIONS DUTY, M*KCAL/HR 1.712 LMTD, C 29.383 F FACTOR (FT) 1.000 MTD, C 29.383 U*A, KCAL/HR-C 58247.946 ------------------------------------------------------- 22
Problem 3 압축기후단의압력을결정하라. 23
Problem 3: 압축기후단압력결정 Compressor outlet Pressure = Bubble pressure of propane at 45 + 0.5 bar (Pressure drop) C3 Phase= Vapor T 1 = -40 o C W Phase= Liquid Temp.= 45 o C P =0.5 bar 24
Problem 3: 압축기후단압력결정 Result 25
Problem 4 팽창밸브후단의압력을결정하라. 26
Problem 4: 팽창밸브후단압력결정 Propane -40 Valve outlet Pressure = Dew Pressure of Propane at -40 27
Problem 4: 팽창밸브후단압력결정 28
Problem 5 증발기로주입되는냉매의유량을결정하라. 29
Problem 5: 증발기로주입되는냉매의유량결정 30
Problem 5: 증발기로주입되는냉매의유량결정 ------------------------------------------------------------------------------ UNIT 1, 'EVAPORATOR' OPERATING CONDITIONS DUTY, M*KCAL/HR 1.712 CONDENSATION, KG-MOL/HR 264.390 TEMPERATURE, C 25.000-30.000 PRESSURE, BAR 1.200 1.200 COLD SIDE CONDITIONS INLET OUTLET ----------- ----------- REFRIGERANT, KG/HR 16946.501 16946.501 SATURATION PRESSURE, BAR 1.109 SATURATION TEMPERATURE, C -40.000 ------------------------------------------------------------------------------ 31
Problem 6 냉매의총순환유량을결정하라. 32
Problem 6: 냉매의총순환유량결정 33
Problem 6: 냉매의총순환유량결정 Steam S4 ----------------------------------------------------------------------- STREAM 'S4' TOTAL LIQUID ---------- ---------- RATE, KG/HR 35139.6939 35139.6939 TEMPERATURE, C 45.00 45.00 PRESSURE, BAR 15.38 15.38 MOLECULAR WEIGHT 44.0965 44.0965 WEIGHT FRACTION 1.0000 ENTHALPY, KCAL/KG 30.9152 30.9152 CP, KCAL/KG-C 0.7693 0.7693 MASS FLOWRATES, KG/HR 1 - C3 35139.6939 35139.6939 2 - IC4 0.0000 0.0000 3 - NC4 0.0000 0.0000 ----------------------------------------------------------------------- 34
Problem 7 압축기의소요동력을추산하라. 단, 압축기의효율은 70% 라고가정하라. 35
Problem 7: 압축기소요동력추산하라 압축기효율 70% 36
Problem 7: 압축기소요동력추산하라 압축기효율 70% 37
Problem 8 응축기의 heat duty 를결정하라. 38
Problem 8: 응축기의 heat duty 를결정 응축기압력강하 0.5 bar, 45 까지프로판응축 39
Problem 8: 응축기의 heat duty 를결정 응축기압력강하 0.5 bar, 45 까지프로판응축 40
Problem 9 냉각수소모량을추산하라. 41
Problem 9: 냉각수소모량추산 냉각수 in/out 32 /37, 프로판 45 까지응축 42
Problem 9: 냉각수소모량추산 냉각수 in/out 32 /37, 프로판 45 까지응축 ---------------------------------------------------------------------------------------------- UNIT 5, 'E2' OPERATING CONDITIONS DUTY, M*KCAL/HR 3.221 LMTD, C 27.312 F FACTOR (FT) 0.947 MTD, C 25.860 U*A, KCAL/HR-C 124551.633 CONDENSATION, KG-MOL/HR 796.881 TEMPERATURE, C 86.533 45.001 PRESSURE, BAR 15.885 15.385 COLD SIDE CONDITIONS INLET OUTLET ----------- ----------- COOLING WATER, KG/HR 644179.101 644179.101 TEMPERATURE, C 32.000 37.000 ---------------------------------------------------------------------------------------------- 43
Problem 10 전체냉동사이클을하나의 PRO/II File 로완성하고, 각각의결과와전체결과를서로비교하라. 44
Problem 10 45
Problem 10 Contents 단계별계산전체시스템계산 증발기 heat duty (M*kcal/hr) 1.7115 1.7115 압축기후단압력 (bar) 15.385 15.385 팽창밸브후단의압력 (bar) 1.114 1.114 증발기로주입되는냉매유량 (kg/hr) 16,946 16,978 냉매의총순환유량 (kg/hr) 35,139 35,139 압축기소요동력 (kw) 1,755 1,755 응축기 heat duty (M*kcal/hr) 3.2209 3.2209 냉각수소모량 (kg/hr) 644,179 644,196 46
감사합니다 47