We read every piece of feedback, and take your input very seriously.
To see all available qualifiers, see our documentation.
Have a question about this project? Sign up for a free GitHub account to open an issue and contact its maintainers and the community.
By clicking “Sign up for GitHub”, you agree to our terms of service and privacy statement. We’ll occasionally send you account related emails.
Already on GitHub? Sign in to your account
Tank_information
# -*- coding: utf-8 -*- """ Created on Wed Jul 20 09:37:03 2022 @author: 252914 """ import numpy as np class Cargo_tank(): # def Tank_info(Tank_type): # 0: Membrane, 1: Flex, 2: Type-B, 3:Type-C Type_tank_list = ['Membrane','Membrane-Flex', 'Type-B', 'Type-C'] Type_tank = Type_tank_list[0] if Type_tank == Type_tank_list[3]: Circle_ratio = 3 else: Circle_ratio = 1.7 Model = "SN2434" if Model == "7_5k_TypeC": BOR = 0.2 # %/day FR = 90 # % ## Tank 정보는 Model 표 만들어서 거기서 가져오는것으로 만들기 Vol_tank_1 = 3750 # m3 Vol_tank_2 = 0 # m3 Vol_tank_3 = 0 # m3 Vol_tank_4 = 0 # m3 Vol_tank_list = np.array([Vol_tank_1, Vol_tank_2, Vol_tank_3, Vol_tank_4]) Vol_tank = np.sum(Vol_tank_list) Area_tank_1 = 2874/2 # m2 Area_tank_2 = 0 # m2 Area_tank_3 = 0 # m2 Area_tank_4 = 0 # m2 Area_tank_list = np.array([Area_tank_1, Area_tank_2, Area_tank_3, Area_tank_4]) Area_tank = np.sum(Area_tank_list) Tank_info = [Type_tank, Circle_ratio, Vol_tank_list, Vol_tank, Area_tank_list, Area_tank, BOR, FR] Ins_thick = 300 # mm Wall_thick = 24 # mm M_wall = 550000/2 # kg SUS weight Cp_wall = 0.35 # kJ/kg/C Cond_wall = 17 # kJ/h/m/C M_ins = 44000/2 # kg Ins weight Cp_ins = 1.071 # kJ/kg/C D_ins = 118 # kg/m3 Cond_ins = 0.0837 # kJ/h/m/C ht_NG = 37.46 # kJ/h/m2/C ht_atm = 19.5 # kJ/h/m2/C Tank_prop = [Ins_thick, M_wall, Cp_wall, M_ins, Cp_ins, D_ins, Cond_ins, ht_NG, ht_atm] sec = 0 # secondary barrier location in insulation elif Model == "SN2430": BOR = 0.239 # %/day FR = 90 # % ## Tank 정보는 Model 표 만들어서 거기서 가져오는것으로 만들기 Vol_tank_1 = 3777 # m3 Vol_tank_2 = 3777 # m3 Vol_tank_3 = 0 # m3 Vol_tank_4 = 0 # m3 Vol_tank_list = np.array([Vol_tank_1, Vol_tank_2, Vol_tank_3, Vol_tank_4]) Vol_tank = np.sum(Vol_tank_list) Area_tank_1 = 2874 /2 # m2 Area_tank_2 = 2874 /2 # m2 Area_tank_3 = 0 # m2 Area_tank_4 = 0 # m2 Area_tank_list = np.array([Area_tank_1, Area_tank_2, Area_tank_3, Area_tank_4]) Area_tank = np.sum(Area_tank_list) Tank_info = [Type_tank, Circle_ratio, Vol_tank_list, Vol_tank, Area_tank_list, Area_tank, BOR, FR] Ins_thick = 300 # mm Wall_thick = 24 # mm M_wall = 550000 # kg SUS weight Cp_wall = 0.35 # kJ/kg/C Cond_wall = 17 # kJ/h/m/C M_ins = 44000 # kg Ins weight Cp_ins = 1.071 # kJ/kg/C D_ins = 40 # kg/m3 Cond_ins = 0.0837 # kJ/h/m/C ht_NG = 420 # kJ/h/m2/C ht_atm = 50 # kJ/h/m2/C Tank_prop = [Ins_thick, M_wall, Cp_wall, M_ins, Cp_ins, D_ins, Cond_ins, ht_NG, ht_atm] sec = 0 # secondary barrier location in insulation elif Model == "6k_Mem": # SN2586 BOR = 0.345 # %/day FR = 98.5 # % ## Tank 정보는 Model 표 만들어서 거기서 가져오는것으로 만들기 Vol_tank_1 = 6000 # m3 Vol_tank_2 = 0 # m3 Vol_tank_3 = 0 # m3 Vol_tank_4 = 0 # m3 Vol_tank_list = np.array([Vol_tank_1, Vol_tank_2, Vol_tank_3, Vol_tank_4]) Vol_tank = np.sum(Vol_tank_list) Area_tank_1 = 2075 # m2 Area_tank_2 = 0 # m2 Area_tank_3 = 0 # m2 Area_tank_4 = 0 # m2 Area_tank_list = np.array([Area_tank_1, Area_tank_2, Area_tank_3, Area_tank_4]) Area_tank = np.sum(Area_tank_list) Tank_info = [Type_tank, Circle_ratio, Vol_tank_list, Vol_tank, Area_tank_list, Area_tank, BOR, FR] Ins_thick = 270 # mm Wall_thick = 1.2 # mm M_wall = 23912 # kg SUS weight Cp_wall = 0.46 # kJ/kg/C Cond_wall = 35 # kJ/h/m/C M_ins = 175343 # kg Ins weight Cp_ins = 1.071 # kJ/kg/C D_ins = 118 # kg/m3 Cond_ins = 0.0837 # kJ/h/m/C ht_NG = 37.76 # kJ/h/m2/C ht_atm = 24 # kJ/h/m2/C Tank_prop = [Ins_thick, M_wall, Cp_wall, M_ins, Cp_ins, D_ins, Cond_ins, ht_NG, ht_atm] sec = 0.1 # secondary barrier location in insulation elif Model == "12k_Type-B": # SN2434 BOR = 0.2 # %/day FR = 98.0 # % ## Tank 정보는 Model 표 만들어서 거기서 가져오는것으로 만들기 Vol_tank_1 = 12000 # m3 Vol_tank_2 = 0 # m3 Vol_tank_3 = 0 # m3 Vol_tank_4 = 0 # m3 Vol_tank_list = np.array([Vol_tank_1, Vol_tank_2, Vol_tank_3, Vol_tank_4]) Vol_tank = np.sum(Vol_tank_list) Area_tank_1 = 3293 # m2 Area_tank_2 = 0 # m2 Area_tank_3 = 0 # m2 Area_tank_4 = 0 # m2 Area_tank_list = np.array([Area_tank_1, Area_tank_2, Area_tank_3, Area_tank_4]) Area_tank = np.sum(Area_tank_list) Tank_info = [Type_tank, Circle_ratio, Vol_tank_list, Vol_tank, Area_tank_list, Area_tank, BOR, FR] Ins_thick = 300 # mm Wall_thick = 12 # mm M_wall = 1020000 # kg SUS weight Cp_wall = 0.35 # kJ/kg/C Cond_wall = 35 # kJ/h/m/C M_ins = 53000 # kg Ins weight Cp_ins = 1.07 # kJ/kg/C D_ins = 118 # kg/m3 Cond_ins = 0.13 # kJ/h/m/C Insulation conductivity 를 제대로 적용해야함. ht_NG = 420 # kJ/h/m2/C ht_atm = 50.0 # kJ/h/m2/C Tank_prop = [Ins_thick, M_wall, Cp_wall, M_ins, Cp_ins, D_ins, Cond_ins, ht_NG, ht_atm] sec = 0.1 # secondary barrier location in insulation elif Model == "SN2434": # Type B, 12K LFV BOR = 0.2 # %/day FR = 98.0 # % ## Tank 정보는 Model 표 만들어서 거기서 가져오는것으로 만들기 Vol_tank_1 = 12000 # m3 Vol_tank_2 = 0 # m3 Vol_tank_3 = 0 # m3 Vol_tank_4 = 0 # m3 Vol_tank_list = np.array([Vol_tank_1, Vol_tank_2, Vol_tank_3, Vol_tank_4]) Vol_tank = np.sum(Vol_tank_list) Area_tank_1 = 3293 # m2 Area_tank_2 = 0 # m2 Area_tank_3 = 0 # m2 Area_tank_4 = 0 # m2 Area_tank_list = np.array([Area_tank_1, Area_tank_2, Area_tank_3, Area_tank_4]) Area_tank = np.sum(Area_tank_list) Tank_info = [Type_tank, Circle_ratio, Vol_tank_list, Vol_tank, Area_tank_list, Area_tank, BOR, FR] Ins_thick = 300 # mm Wall_thick = 12 # mm M_wall = 1020000 # kg SUS weight Cp_wall = 0.35 # kJ/kg/C Cond_wall = 35 # kJ/h/m/C M_ins = 53000 # kg Ins weight Cp_ins = 1.07 # kJ/kg/C D_ins = 118 # kg/m3 Cond_ins = 0.13 # kJ/h/m/C Insulation conductivity 를 제대로 적용해야함. ht_NG = 420 # kJ/h/m2/C ht_atm = 50.0 # kJ/h/m2/C Tank_prop = [Ins_thick, M_wall, Cp_wall, M_ins, Cp_ins, D_ins, Cond_ins, ht_NG, ht_atm] sec = 0.1 # secondary barrier location in insulation elif Model == "174k_Mem": BOR = 0.1 # %/day FR = 98.5 # % ## Tank 정보는 Model 표 만들어서 거기서 가져오는것으로 만들기 Vol_tank_1 = 25997 # m3 Vol_tank_2 = 49716 # m3 Vol_tank_3 = Vol_tank_2 # m3 Vol_tank_4 = Vol_tank_2 # m3 # Vol_tank_1 = 6000 # m3 # Vol_tank_2 = 0 # m3 # Vol_tank_3 = Vol_tank_2 # m3 # Vol_tank_4 = Vol_tank_2 # m3 Vol_tank_list = np.array([Vol_tank_1, Vol_tank_2, Vol_tank_3, Vol_tank_4]) Vol_tank = np.sum(Vol_tank_list) Area_tank_1 = 5060 # m2 Area_tank_2 = 7877 # m2 Area_tank_3 = Area_tank_2 # m2 Area_tank_4 = Area_tank_2 # m2 # Area_tank_1 = 2300 # m2 # Area_tank_2 = 0 # m2 # Area_tank_3 = Area_tank_2 # m2 # Area_tank_4 = Area_tank_2 # m2 Area_tank_list = np.array([Area_tank_1, Area_tank_2, Area_tank_3, Area_tank_4]) Area_tank = np.sum(Area_tank_list) Tank_info = [Type_tank, Circle_ratio, Vol_tank_list, Vol_tank, Area_tank_list, Area_tank, BOR, FR] # return Tank_info Ins_thick = 270 # mm Wall_thick = 1.2 # mm M_wall = 383849 # kg SUS weight Cp_wall = 0.46 # kJ/kg/C Cond_wall = 35 # kJ/h/m/C M_ins = 1891303 # kg Ins weight Cp_ins = 1.071 # kJ/kg/C D_ins = 190 # kg/m3 Cond_ins = 0.096 # kJ/h/m/C ht_NG = 37.46 # kJ/h/m2/C ht_atm = 16.8 # kJ/h/m2/C # Ins_thick = 270 # mm # M_wall = 31000 # kg SUS weight # Cp_wall = 0.46 # kJ/kg/C # M_ins = 170000 # kg Ins weight # Cp_ins = 1.07 # kJ/kg/C # D_ins = 118 # kg/m3 # Cond_ins = 0.08 # kJ/h/m/C # ht_NG = 37.46 # kJ/h/m2/C # ht_atm = 16.8 # kJ/h/m2/C Tank_prop = [Ins_thick, M_wall, Cp_wall, M_ins, Cp_ins, D_ins, Cond_ins, ht_NG, ht_atm] sec = 0.1 # secondary barrier location in insulation # return Tank_prop # def TypeC_7_5k() : # SN2430 # BOR = 0.2 # %/day # FR = 90 # % # ## Tank 정보는 Model 표 만들어서 거기서 가져오는것으로 만들기 # Vol_tank_1 = 3750 # m3 # Vol_tank_2 = 3750 # m3 # Vol_tank_3 = 0 # m3 # Vol_tank_4 = 0 # m3 # Vol_tank_list = np.array([Vol_tank_1, Vol_tank_2, Vol_tank_3, Vol_tank_4]) # Vol_tank = np.sum(Vol_tank_list) # Area_tank_1 = 2874/2 # m2 # Area_tank_2 = 2874/2 # m2 # Area_tank_3 = 0 # m2 # Area_tank_4 = 0 # m2 # Area_tank_list = np.array([Area_tank_1, Area_tank_2, Area_tank_3, Area_tank_4]) # Area_tank = np.sum(Area_tank_list) # Tank_info = [Type_tank, Circle_ratio, Vol_tank_list, Vol_tank, Area_tank_list, Area_tank, BOR, FR] # Ins_thick = 300 # mm # M_wall = 550000 # kg SUS weight # Cp_wall = 0.35 # kJ/kg/C # M_ins = 44000 # kg Ins weight # Cp_ins = 1.071 # kJ/kg/C # D_ins = 118 # kg/m3 # Cond_ins = 0.08 # kJ/h/m/C # ht_NG = 37.46 # kJ/h/m2/C # ht_atm = 19.5 # kJ/h/m2/C # Tank_prop = [Ins_thick, M_wall, Cp_wall, M_ins, Cp_ins, D_ins, Cond_ins, ht_NG, ht_atm] U = 1/(1/ht_NG + Wall_thick/1000/Cond_wall + Ins_thick/1000/Cond_ins + 1/ht_atm) print(Model, Vol_tank, Ins_thick)
The text was updated successfully, but these errors were encountered:
# -*- coding: utf-8 -*- """ 22. 06. 27 """ import os, numpy as np import math import imageio import matplotlib.pyplot as plt from win32com.client import Dispatch import pandas as pd import numpy as np # from scipy import integrate import pickle import csv import openpyxl import sys from ctREFPROP.ctREFPROP import REFPROPFunctionLibrary from scipy import integrate import Tank_information as T import time Tank = T.Cargo_tank() seconds = 3 while seconds > 0: print("Check Model :", seconds, "sec") time.sleep(0.5) seconds = seconds - 1 os.environ['RPPREFIX'] = r'E:\REFPROP' RP = REFPROPFunctionLibrary(os.environ['RPPREFIX']) RP.SETPATHdll(os.environ['RPPREFIX']) SI = RP.GETENUMdll(0,"SI WITH C").iEnum # Property = "P;T;D;H;M;CP;Phase;Qmass" # Prop_list = "P;T;D;H;M;CP;Phase;Qmass;VIS;TCX;PRANDTL;KV;Heatvapz_P" # Property_total = "T;P;D;H;CP;Phase;Qmass;" Prop_list = "P;T;D;H;M;CP;Qmass;VIS;TCX;PRANDTL;KV;Heatvapz_P;Phase;" # VISCOSITY 는 100만 나누어야 함. Prop_index = np.array(Prop_list.replace(';',' ').split()) # df1 = pd.read_pickle('Pipetable.p') def Heat_transfer(Supply_condition, Init_cond, P_mode, T_ins, T_ins_ave, Ins_node, dt): #################### Initial Calculation condition # Init_cond = Init_condition(Comp_name, Comp_init, P_init, Surface, Filling, Vol_liq, Vol_vap, Step, LastStep, Target) T_vap = Init_cond[2][1] h = Init_cond[2][3] d = Init_cond[2][2] Phase = Init_cond[5] Qmass = Init_cond[2][6] h_liq = Init_cond[3][3] d_liq = Init_cond[3][2] h_vap = Init_cond[4][3] d_vap = Init_cond[4][2] Comp = Comp_init Comp_liq = Init_cond[0] Comp_vap = Init_cond[1] # P = RP.REFPROPdll(Comp_name, "DH" , "P", SI, 1, 0, d, h, Comp).Output[0] # print('Pressure : ', P) Supply = Supply_condition val = Supply[4].find("Warm") #Operation check Warm-up 시에는 열공급 효율 70%로 진행 val2 = Supply[4].find("Inert") #Operation check Inert 시에는 O2, CH4 composition print val_cool = Supply[4].find("Cool") #Operation check CD 시에는 spray 누적량 표기, Exhaust 량 표기 dt = dt # dtt = 2 * dt T_wall = T_vap Mass_tank = Volume * Init_cond[2][2] Mass_vap = Mass_tank * Qmass Mass_liq = Mass_tank - Mass_vap T_ins_var = 0 T_ins = T_ins Ins_node = Ins_node T_ins_temp = np.zeros(len(T_ins)) Mass_exhaust_init = 0 # 100 kg/h Vol_exhaust_init = 0 Amount_spray = 0 # kg/h accumulate T_ins_sec = (T_ins[loc_sec] + T_ins[loc_sec_1]) / 2 Q_tank = U * Surface * (T_atm - T_vap) ################### Data save ############################################# strFormat = '%' T_ins_table = np.append(T_ins, T_ins_ave) T_ins_table = np.append(T_ins_table, T_ins_sec) Prop_table = np.array([0, P_init, T_vap, T_wall, d, h, Mass_tank, Phase, Qmass, Mass_exhaust_init, Vol_exhaust_init, Amount_spray]) print(Comp_init) print(Comp_liq) print(Comp_vap) Comp_table = np.array([Comp_init, Comp_liq, Comp_vap]) heatleak = [] for i in range (Calculation): # if i < 100: # 초기 계산에만 time step 줄여서 계산하다가 100번 iteration 후에는 time step 10배로 # dt = dt # else: # dt = dtt # if Operation == "Cool-down": # if T_vap < -140: # break # elif Operation == "Cool-down": if val == -1: dh = (-1 * (Supply[2][i] * (h - Supply[1][3]) + ht_NG * Surface * (T_vap - T_wall)) * dt) / Mass_tank else: #Operation check : Warm-up 시에는 열공급 효율 70%로 진행 dh = (-1 * (Supply[2][i]*0.7 * (h - Supply[1][3]) + ht_NG * Surface * (T_vap - T_wall)) * dt) / Mass_tank # print(i*dt+dt, T_vap, dh, Mass_tank) dT_wall = ((ht_NG * Surface * (T_vap - T_wall) + ht_atm * Surface * (T_atm - T_ins[-1])) * dt - M_ins * Cp_ins* T_ins_var) / (M_wall * Cp_wall) Comp = list(map(lambda x, y: (x * Mass_tank + y * Supply[2][i] * dt) / (Mass_tank + Supply[2][i]*dt), Comp, Supply[0])) h_pre = h # 이전 스텝 h값 # 압력항에 대한 것도 같이 넣어줘야 할것 같음. if P_mode == 0: # 0: Const, 1: Various h = h + dh d = RP.REFPROPdll(Comp_name, "PH" , "D", SI, 1, 0, P_init, h, Comp).Output[0] Mass_exhaust = (Mass_tank + (Supply[2][i] * dt) - (Volume * d)) / dt Vol_exhaust = Mass_exhaust / d ### Vol_exhause = (Mass_tank/d - Mass_tank/d_pre + Spray_mass * dt/d) / dt Mass_tank = Volume * d P = P_init T_vap = np.array(RP.REFPROPdll(Comp_name,"DH","T",SI,1,1,d,h,Comp).Output[0]) Qmass = np.array(RP.REFPROPdll(Comp_name,"DH","Qmass",SI,1,1,d,h,Comp).Output[0]) Phase = np.array(RP.REFPROPdll(Comp_name,"DH","Phase",SI,1,1,d,h,Comp).hUnits) T_wall = T_wall + dT_wall else: Mass_exhaust = 0 ## user가 수정 h = ((-1 * (Supply[2][i] * (- Supply[1][3]) + ht_NG * Surface * (T_vap - T_wall)) * dt) + Mass_liq * h_liq + (Mass_vap - Mass_exhaust * dt) * h_vap) / Mass_tank # print(((ht_atm * Surface) * (T_atm - T_ins[-1]))/509) Mass_tank = Mass_tank + Supply[2][i]*dt-Mass_exhaust d = Mass_tank / Volume P = RP.REFPROPdll(Comp_name, "DH" , "P", SI, 1, 1, d, h, Comp).Output[0] Vol_exhaust = Mass_exhaust / d ## user가 수정 T_vap = RP.REFPROPdll(Comp_name,"DH","T",SI,1,1,d,h,Comp).Output[0] Qmass = RP.REFPROPdll(Comp_name,"DH","Qmass",SI,1,1,d,h,Comp).Output[0] Phase = np.array(RP.REFPROPdll(Comp_name,"DH","Phase",SI,1,1,d,h,Comp).hUnits) T_wall = T_wall + dT_wall Comp_liq = np.array(RP.REFPROPdll(Comp_name,"DT","xmassliq",SI,1,0,d,T_vap,Comp).Output[0:Comp_name.count(';')]) Comp_vap = np.array(RP.REFPROPdll(Comp_name,"DT","xmassvap",SI,1,0,d,T_vap,Comp).Output[0:Comp_name.count(';')]) Mass_vap = Mass_tank * Qmass Mass_liq = Mass_tank - Mass_vap if Qmass >0 and Qmass < 1: # two-phase P = RP.REFPROPdll(Comp_name, "DH" , "P", SI, 1, 1, d, h, Comp).Output[0] # d_vap = RP.REFPROPdll(Comp_name,"PQmass","Dvap",SI,1,1,P, Qmass,Comp_vap).Output[0] # d_liq = RP.REFPROPdll(Comp_name,"PQmass","Dliq",SI,1,1,P, Qmass,Comp_liq).Output[0] # h_vap = RP.REFPROPdll(Comp_name,"PD","H",SI,1,1,P,d_vap, Comp_vap).Output[0] # h_liq = RP.REFPROPdll(Comp_name,"PD","H",SI,1,1,P,d_liq, Comp_liq).Output[0] d_vap = RP.REFPROPdll(Comp_name,"Ph","Dvap",SI,1,1,P, h, Comp).Output[0] d_liq = RP.REFPROPdll(Comp_name,"Ph","Dliq",SI,1,1,P, h, Comp).Output[0] # h_vap = RP.REFPROPdll(Comp_name,"PD","H",SI,1,1,P,d_vap, Comp_vap).Output[0] # h_liq = RP.REFPROPdll(Comp_name,"PD","H",SI,1,1,P,d_liq, Comp_liq).Output[0] h_vap = RP.REFPROPdll(Comp_name,"PD","Hvap",SI,1,1,P,d, Comp).Output[0] h_liq = RP.REFPROPdll(Comp_name,"PD","Hliq",SI,1,1,P,d, Comp).Output[0] else: d_vap = np.array(RP.REFPROPdll(Comp_name,"PT","Dvap",SI,1,1,P,T_vap,Comp_vap).Output[0]) d_liq = np.array(RP.REFPROPdll(Comp_name,"PT","Dliq",SI,1,1,P,T_vap,Comp_liq).Output[0]) h_vap = np.array(RP.REFPROPdll(Comp_name,"PD","h",SI,1,1,P,d_vap,Comp_vap).Output[0]) h_liq = np.array(RP.REFPROPdll(Comp_name,"PD","h",SI,1,1,P,d_liq,Comp_liq).Output[0]) # Prop = Properties(Comp_name, Comp, "DH", d, h)[0] # Prop = np.array(RP.REFPROPdll(Comp_name,"DH",Prop_list,SI,1,0,d,h,Comp).Output[0:Prop_list.count(';')]) Comp_array = np.array([Comp, Comp_liq, Comp_vap]) Comp_table = np.vstack([Comp_table, Comp_array]) # Comp_table = np.vstack([Comp_table, Comp]) for j in range (len(T_ins)-2): k = j+1 T_ins_temp[0] = T_wall T_ins_temp[k] = diffusivity * dt / Ins_interval**2 * (T_ins[j] + T_ins[j+2]) + (1- 2* (diffusivity * dt / Ins_interval**2)) * T_ins[j+1] T_ins_temp[len(T_ins)-1] = Cond_ins/ ht_atm * (T_ins[len(T_ins)-2] - T_ins[len(T_ins)-1]) / (Ins_node[len(T_ins)-1] - Ins_node[len(T_ins)-2]) + T_atm T_ins_sec = (T_ins[loc_sec] + T_ins[loc_sec_1]) / 2 T_ins_temp_ave = simpson(T_ins_temp,len(T_ins)-1) T_ins_temp_table = np.append(T_ins_temp, T_ins_temp_ave) T_ins_temp_table = np.append(T_ins_temp_table, T_ins_sec) T_ins_table = np.vstack([T_ins_table, T_ins_temp_table]) # Time step 별 Insul node 별 테이블화 Amount_spray = Amount_spray + Supply[2][i]*dt Prop_tank = np.array([np.round(i*dt+dt,2), np.round(P,4), np.round(T_vap,4), np.round(T_wall,4), np.round(d,2), np.round(h,4), np.round(Mass_tank,2), Phase, np.round(Qmass,4), np.round(Mass_exhaust,2), np.round(Vol_exhaust,2), Amount_spray]) # print (Prop_tank) Prop_table = np.vstack([Prop_table, Prop_tank]) T_ins_var = T_ins_temp_ave - T_ins_ave # print(T_ins_temp_ave, T_ins_ave, T_ins_var) T_ins = T_ins_temp T_ins_ave = T_ins_temp_ave print('Time :', "%-8s" % np.round(i*dt+dt,2), 'Press. :', "%-8s" % np.round(P,6), 'T_vap :', "%-8s" % np.round(T_vap,6), 'T_wall :', "%-8s" % np.round(T_wall,2), 'T_sec :', np.round(T_ins_sec,2)) if val_cool is not -1: print('Amount of Spray : ', "%-10s" % np.round(Amount_spray,2), "Exhaust : ", "%-10s" % np.round(Mass_exhaust,2)) ### dew point ### https://en.wikipedia.org/wiki/Dew_point ### https://en.wikipedia.org/wiki/Arden_Buck_equation if val2 == -1: dew_point = 0 else: water_mole = RP.REFPROPdll(Comp_name,"DT","Xmole",SI,1,1,d,T_vap,Comp).Output[10] print(water_mole) RH = (P*water_mole)/RP.REFPROPdll("Water","TQmass","P",SI,1,1,T_vap,0,[1.0]).Output[0] ## 상대 습도 print(RH) dew_point = 243.04*(np.log(RH)+(17.625*T_vap/(243.04+T_vap)))/(17.625-np.log(RH)-(17.625*T_vap/(243.04+T_vap))) print("Methane : " , "%-10s"%np.round(Comp[1]*100,4), "Oxygen : ", "%-10s"%np.round(Comp[8]*100,4), "N2 :" , Amount_spray/1000) print("Dew Point : ", dew_point) Heat_to_gas = Mass_tank * (h - h_pre) / dt # kJ/h Heat_to_pri = M_wall * Cp_wall * T_ins_var / dt # kJ/h ################################ Plot ########################################### ### 시간에 따라 지속적으로 plot # fig = plt.figure(figsize=(10,10)) # ax = fig.add_subplot() # x_axis.append(i * dt) # y_axis.append(T_vap) # y_axis2.append(T_wall) # y_axis3.append(T_ins_ave) # # ax.plot(x_axis,y_axis, color = 'b', linewidth = 4.0) # # ax.plot(x_axis,y_axis2, color = 'r', linewidth = 4.0) # # ax.plot(x_axis,y_axis3, color = 'green', linewidth = 4.0) # plt.plot(x_axis, y_axis, 'b', x_axis, y_axis2, 'r', x_axis, y_axis3, 'green', linewidth = 4.0 ) # ax.patch.set_facecolor('#c6d9f1') # axes 배경색 # # plt.setp(line, color = 'b', linewidth = 4.0) # plt.xlabel('Time (hr)', size=15) # plt.ylabel('Temperature (C)', size=15) # # plt.rc('axes', labelsize = 70) # plt.xlim(0,) # plt.ylim(-180,40) # plt.grid(True) # plotting = int(i % 100) ### 100 step 마다 plot # plt.plot(1,1) # plt.figure(figsize=(10,10)) plt.rcParams["figure.figsize"] = (10,10) ax = plt.gca() ax.set_facecolor('#c6d9f1') # axes 배경색 x_axis.append(i * dt) y_axis.append(T_vap) y_axis2.append(T_wall) y_axis3.append(T_ins_ave) y_axis4.append(T_ins_sec) # plt.subplot(211) plt.plot(x_axis, y_axis, 'b', x_axis, y_axis2, 'r', x_axis, y_axis3, 'green', x_axis, y_axis4, 'Orange', linewidth = 4.0 ) plt.xlabel('Time (hr)', size=15) plt.ylabel('Temperature (C)', size=15) plt.xlim(0, Calculation*dt) plt.ylim(-180,50) plt.grid(True) plotting = int(i % 100) gif = int(i % 10) ### GIF 만들기 # if gif == 0: # plotname = f'Plot{i}.png' # plotnames.append(plotname) # plt.savefig(plotname, bbox_inches = 'tight', pad_inches = 0) # if i == (Calculation-1): # name = f'Last.jpeg' # plt.savefig(name, bbox_inches = 'tight', pad_inches = 0 ) if plotting == 0: plt.show() ### Insulation 온도 분포 (누적, 또는 나중에 Table 해서 그냥 한번만 뽑기) # if plotting == 0: # x2_axis = Ins_node # y2_axis = T_ins # plt.subplot(212) # plt.rcParams["figure.figsize"] = (10,10) # ax = plt.gca() # ax.set_facecolor('#c6d9f1') # axes 배경색 # plt.xlim(0,Ins_thick/1000) # plt.ylim(-170,50) # plt.xlabel('Insulation Thickness (m)', size=15) # plt.ylabel('Temperature (C)', size=15) # plt.grid(True) # print(x2_axis, y2_axis) # plt.plot(x2_axis, y2_axis, linewidth = 4.0) # plt.show() return Prop_table, T_ins_table, Comp_table # Exhaust vapor 계산하기 # Mass_conv = Mass_supply * dt + Mass_tank - Mass_exhaust # for i in (len(T_ins)-1): # k = i+1 # T_ins_temp[i] = T_wall # T_ins_temp[k] = diffusivity * dt / Ins_interval**2 * (T_ins[i] + T_ins[i+2]) + (1- 2* (diffusivity * dt / Ins_interval**2)) * T_ins[i+1] # for i in range (0,12/3600+t_step,t_step): def Supply_condition(Comp_name, Mode_operation, Input_prop, Input1, Input2, Mass_supply, Calculation): # 0 'Inerting', 1'Inerting_N', 2'Gassing-up', 3'Cool-down', 4'Cool-down_N', 5'Warm-up', 6'Warm-up_N', 7'Aeration', 8'Hold'] if Mode_operation == Mode_list[0]: Comp_supply = np.array([0.85, 0, 0, 0, 0, 0, 0, 0, 0.01, 0.14, 0]) elif Mode_operation == Mode_list[1] or Mode_operation == Mode_list[4] or Mode_operation == Mode_list[6]: Comp_supply = np.array([1.0, 0, 0, 0, 0, 0, 0, 0, 0, 0, 0]) elif Mode_operation == Mode_list[2] or Mode_operation == Mode_list[3] or Mode_operation == Mode_list[5] or Mode_operation == Mode_list[8]: Comp_supply = Comp_init else: # Aeration Comp_supply = np.array([0.78, 0, 0, 0, 0, 0, 0, 0, 0.21, 0.01, 0]) Value = Properties(Comp_name, Comp_supply, Input_prop, Input1, Input2)[0] Volume_supply = Mass_supply / Value[2] ## Supply ramp-up Cal_time = Calculation Supply_mass = np.full(Cal_time, Mass_supply) for i in range (11): if i < 6: Supply_mass[i] = 1/(10-i) * Mass_supply else: Supply_mass[i] = (i-5) / 5 * Mass_supply return Comp_supply, Value, Supply_mass, Volume_supply, Mode_operation def Properties(Comp_name, Comp_value, Input_prop, input1, input2): Prop = [] Value = [] for k in Prop_index: # P;T;D;H;M;CP;Qmass;VIS;TCX;PRANDTL;KV;Heatvapz_P;Phase; r = RP.REFPROPdll(Comp_name, Input_prop, k, SI, 1, 0, input1, input2, Comp_value) Prop.append([k,r.hUnits,r.Output[0]]) Value.append(r.Output[0]) DY = Value[2] * Value[11] / (100**2) # Dynamic viscousity df_prop = pd.DataFrame(Prop, index = Prop_index, columns=['Prop','Units','Values']) df_prop = df_prop.drop(['Prop'], axis=1) df_prop.loc['DV'] = ['kg/m-s', DY] return Value, df_prop # Value, dataframe def Init_condition(Comp_name, Comp_init, P_init, Filling, Step, LastStep, Target): Qmass = 0.01 # Initial Qmass direction = 0 # Try and Error Initial direction D_tank = RP.REFPROPdll(Comp_name,"PQmass","D",SI,1,0,P_init,Qmass,Comp_init).Output[0] D_liq = RP.REFPROPdll(Comp_name,"PQmass","Dliq",SI,1,0,P_init,Qmass,Comp_init).Output[0] D_vap = RP.REFPROPdll(Comp_name,"PQmass","Dvap",SI,1,0,P_init,Qmass,Comp_init).Output[0] Vol_liq = Volume * Filling/100 Vol_vap = Volume - Vol_liq Mass_tank = Volume * D_tank Mass_liq = Vol_liq * D_liq Mass_vap = Vol_vap * D_vap Mass_conv = Mass_tank - Mass_liq - Mass_vap # 질량보존 확인항 if Mass_conv < Target: direction = 1 else: direction = -1 if Mass_conv == Target: sys.exit(0) # sys.exit(0) 프로그램 정상 종료, (1) 강제 종료 if Filling == 0: Comp_liq_mass = np.array(RP.REFPROPdll(Comp_name,"PT","xmassliq",SI,1,0,P_init,T_set_vapor,Comp_init).Output[0:Comp_name.count(';')]) Comp_vap_mass = np.array(RP.REFPROPdll(Comp_name,"PT","xmassvap",SI,1,0,P_init,T_set_vapor,Comp_init).Output[0:Comp_name.count(';')]) Pro_init_mass = np.array(Properties(Comp_name, Comp_init, "PT", P_init, T_set_vapor)[0]) Pro_liq_mass = Pro_init_mass Pro_vap_mass = Pro_init_mass Phase = RP.REFPROPdll(Comp_name,"PT","Phase",SI,1,0,P_init,T_set_vapor,Comp_init).hUnits else: for i in range(1,10000,1): Qmass = Qmass + Step * direction if i % 100 == 0: ## 수렴 가속화 print('=====================================================') print('Qmass reset') print('=====================================================') Qmass = Mass_vap / Mass_tank # Step = Step * 10 if Mass_conv < Target: ### Qmass 가 음수가 되는 경우 피하기 위한 함수 if Qmass < 0: if direction == -1: if Step > LastStep: # Step = Step / 10 direction = direction * -1 ############################################## elif direction == 1: if Step > LastStep: Step = Step / 10 direction = direction * -1 else: if direction == -1: if Step > LastStep: Step = Step / 10 direction = direction * -1 if Step < LastStep: break aa = Mass_vap / Mass_tank # print(Step, aa, direction) # print(D_tank, D_liq, D_vap) # print(i, Qmass, Step) print("Calculating... i: {} Mass_conv {} Tank {} Liq {} Vap {} Qmass: {}".format(i,round(Mass_conv,8), round(Mass_tank,2), round(Mass_liq,2), round(Mass_vap,2), round(Qmass,15))) D_tank = RP.REFPROPdll(Comp_name,"PQmass","D",SI,1,0,P_init,Qmass,Comp_init).Output[0] D_liq = RP.REFPROPdll(Comp_name,"PQmass","Dliq",SI,1,0,P_init,Qmass,Comp_init).Output[0] D_vap = RP.REFPROPdll(Comp_name,"PQmass","Dvap",SI,1,0,P_init,Qmass,Comp_init).Output[0] Mass_tank = Volume * D_tank Mass_liq = Vol_liq * D_liq Mass_vap = Vol_vap * D_vap Mass_conv = Mass_tank-Mass_liq-Mass_vap print('Done', i) print('Qmass : ', Qmass) print('Mass_conv : ', Mass_conv) Comp_liq_mass = np.array(RP.REFPROPdll(Comp_name,"PQmass","xmassliq",SI,1,0,P_init,Qmass,Comp_init).Output[0:Comp_name.count(';')]) Comp_vap_mass = np.array(RP.REFPROPdll(Comp_name,"PQmass","xmassvap",SI,1,0,P_init,Qmass,Comp_init).Output[0:Comp_name.count(';')]) Pro_init_mass = np.array(Properties(Comp_name, Comp_init, "PQmass", P_init, Qmass)[0]) Pro_liq_mass = np.array(Properties(Comp_name, Comp_liq_mass, "PQmass", P_init, 0)[0]) Pro_vap_mass = np.array(Properties(Comp_name, Comp_vap_mass, "PQmass", P_init, 1)[0]) Phase = RP.REFPROPdll(Comp_name,"PQmass","Phase",SI,1,0,P_init,Qmass,Comp_init).hUnits return Comp_liq_mass, Comp_vap_mass, Pro_init_mass, Pro_liq_mass, Pro_vap_mass, Phase def Unitconv_nominal(Comp_name, Comp, P, T, iflag, Value): # iflag 0: Nominal flowrate, 1: Volumetric flowrate, 2 : Mass flowrate d = RP.REFPROPdll(Comp_name, "PT" , "D", SI, 1, 0, P, T, Comp).Output[0] d_no = RP.REFPROPdll(Comp_name, "PT" , "D", SI, 1, 0, 0.101325, 0, Comp).Output[0] if iflag == 0: Nominal = Value Mass = Nominal * d_no Vol = Mass / d elif iflag == 1: Vol = Value Mass = Vol * d Nominal = Mass / d_no elif iflag == 2: Mass = Value Vol = Mass / d Nominal = Mass / d_no print("Nominal : ", np.round(Nominal,2), "Nm3/h") print("Volume flow : ", np.round(Vol,2), "m3/h") print("Mass flow : ", np.round(Mass,2), "kg/h") return Nominal, Vol, Mass def BOG_calculation(Tank_volume, Filling_Ratio, BOR, Comp_name, Comp_LNG): # methane, LNG, Revised_BOR Vol = Tank_volume d_methane = RP.REFPROPdll("Methane", "PQmass", "D", SI, 1, 0, P_init, 0, [1.0]).Output[0] LH_methane = RP.REFPROPdll("Methane", "PQmass", "Heatvapz_P", SI, 1, 0, P_init, 0, [1.0]).Output[0] d = RP.REFPROPdll(Comp_name, "PQmass", "D", SI, 1, 0, P_init, 0, Comp_LNG).Output[0] ## LNG 기화된 Vap 의 LH 사용 Comp_vap_LNG = RP.REFPROPdll(Comp_name,"PQmass","XmassVAP",SI,1,0,P_init,0.01,Comp_LNG).Output[0:len(Comp_LNG)] LH = RP.REFPROPdll(Comp_name, "PQmass", "Heatvapz_P", SI, 1, 0, P_init, 0, Comp_vap_LNG).Output[0] # print(Comp_vap_LNG) # print(LH) BOG_methane = Vol * FR/100 * d * BOR /24 /100 BOG_LNG = BOG_methane * LH_methane * d_methane / LH / d Revised_BOR = BOR * LH_methane * d_methane / LH / d print("BOG Methane :", "%-5s" % round(BOG_methane,2), "%-5s" % "kg/h") print("BOG_LNG :", "%-5s" % round(BOG_LNG,2), "kg/h") return BOG_methane, BOG_LNG, Revised_BOR # 메탄 BOG(kg/h) LNG BOG(kg/h), IMO 수정된 BOR # def BOR_check(BOG, Comp_name, Comp_init, P_init, Filling, Step, LastStep, Target, Mode_list, Sim_time): # Init_cond = Init_condition(Comp_name, Comp_init, P_init, Filling, Step, LastStep, Target) # Operation = Mode_list[6] # Supply = Supply_condition(Comp_name, Operation, "PT", 0.11, 60, 0, Sim_time) # Hold = Heat_transfer(Supply, Init_cond, 0, T_ins, T_ins_ave, Ins_node, dt) # Exhaust = Hold[0][9] # if Exhaust < BOG: # direction = 1 # else: # direction = -1 # if round(Exhaust,1) < round(BOG,1)*1.1 and round(Exhaust,1) > round(BOG,1)*0.9: # sys.exit(0) # sys.exit(0) 프로그램 정상 종료, (1) 강제 종료 # for i in range(1,10000,1): # print(ht_atm, Exhaust, BOG) # ht_atm = ht_atm + Step * direction # Exhaust = Heat_transfer(Supply, Init_cond, 0, T_ins, T_ins_ave, Ins_node, dt)[0][9] # if Exhaust < BOG: # ### Qmass 가 음수가 되는 경우 피하기 위한 함수 # if ht_atm < 0: # if direction == -1: # if Step > LastStep: # Step = Step / 10 # direction = 1 # ############################################## # elif direction == 1: # if Step > LastStep: # Step = Step / 10 # direction = direction * -1 # else: # if direction == -1: # if Step > LastStep: # Step = Step / 10 # direction = direction * -1 # if Step < LastStep: # break # return Exhaust ''''''''''''''''''''''''''' Initial Condition ''''''''''''''''''''''''''' Comp_name = "Nitrogen;Methane;Ethane;Propane;Butane;Isobutane;Pentane;Isopentane;Oxygen;CO2;Water;" Comp_name_index = np.array(Comp_name.replace(';',' ').split()) Comp_init = np.array([1.0, 0.0, 0, 0, 0, 0, 0, 0, 0, 0, 0]) # pure N2 # Comp_init = np.array([0.0, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0]) # Pure_methane = np.array([0.0, 1, 0, 0, 0, 0, 0, 0, 0, 0, 0]) # Comp_init = np.array([0.0079, 0.9205, 0.0547, 0.0133, 0.0037, 0, 0, 0, 0, 0]) # Mass base # Comp_init = np.array([0.751, 0.0, 0, 0, 0, 0, 0, 0, 0.2319, 0.0152, 0.0019]) # Air T_atm = 25 # C P_init = 0.126325 # Mpa T_set_vapor = -160 Volume = Tank.Vol_tank # m3 Surface = Tank.Area_tank # m2 Filling = 0 # % FR = Tank.FR BOR = Tank.BOR ''''''''''''''''''''''''''''' Insulation information ''''''''''''''''''''''''''''' M_wall = Tank.M_wall # kg Cp_wall = Tank.Cp_wall # kJ/kg/C Cond_wall = Tank.Cond_wall # kJ/h/m/C Wall_thick = Tank.Wall_thick # mm M_ins = Tank.M_ins # kg Cp_ins = Tank.Cp_ins # kJ/kg/C D_ins = Tank.D_ins # kg/m3 Cond_ins = Tank.Cond_ins # kJ/h/m/C Ins_thick = Tank.Ins_thick # mm ht_NG = Tank.ht_NG # kJ/h/m2/C ht_atm = Tank.ht_atm # kJ/h/m2/C U = Tank.U ''''''''''''''''''''''''''' Equilibrium Mode ''''''''''''''''''''''''''' # Qmass = 0.1 # initial value funcion 에 기입 Step = 0.2 LastStep = 0.0000000000001 Target = 0.001 # direction = 0 ''''''''''''''''''''''''''' Plot ''''''''''''''''''''''''''' x_axis = [] y_axis = [] y_axis2 = [] y_axis3 = [] y_axis4 = [] # sec barrier x2_axis = [] y2_axis = [] filenames = [] plotnames = [] ############################################################## ####################### Definition ########################### ############################################################## # Input_prop = 'PT', 'PH' 등등 Init_cond = Init_condition(Comp_name, Comp_init, P_init, Filling, Step, LastStep, Target) T_vap = Init_cond[4][1] T_lng = Init_cond[2][1] T_liq = Init_cond[3][1] T_wall = T_vap Mass_tank = Volume * Init_cond[2][2] Mass_vap = Mass_tank * Init_cond[2][6] Mass_liq = Mass_tank - Mass_vap ''''''''''''''''''''''''''' Select Mode ''''''''''''''''''''''''''' Mode_list = ['Inerting', 'Inerting_N', 'Gassing-up', 'Cool-down', 'Cool-down_N', 'Warm-up', 'Warm-up_N', 'Aeration', 'Hold'] Mode_pressure = "Constant" # Constant, Variable ''''''''''''''''''''''''''''''''''''''' Insulation Initial condition ''''''''''''''''''''''''''''''''''''''' n = 12 # Insulation node 수 Ins_interval = Ins_thick/1000 / n # Node 별 거리 Ins_node = np.arange(0,Ins_thick/1000+Ins_interval/100,Ins_interval) # Insulation 각 위치 T2 = (T_wall + (ht_atm * Ins_thick/1000/Cond_ins)*T_atm) / (1+(ht_atm*Ins_thick /1000/Cond_ins)) #Ins Outer temp. T_ins_step = (T2 - T_wall) / (Ins_thick/1000/Ins_interval) # ins del_T T_ins = np.zeros(n+1) ### Insulation secondary barrier 위치 정하기 Ins_sec = Tank.sec if np.any(Ins_node == Ins_sec) == True: # Insulation node 와 secondary barrier 가 같은경우, loc_sec = np.where(Ins_node == Ins_sec)[0][0] #Insulation location loc_sec_1 = np.where(Ins_node == Ins_sec)[0][0] # T_ins_sec = (T_ins[loc_sec] + T_ins[loc_sec_1]) / 2 else: # 다를 경우는, 근처 2개 값의 평균값을 사용 nearest = Ins_node.flat[np.abs(Ins_node - Ins_sec).argmin()] if nearest > Ins_sec: Ins_sec_1 = Ins_sec - 0.01 elif nearest < Tank.sec: Ins_sec_1 = Ins_sec + 0.01 nearest_1 = Ins_node.flat[np.abs(Ins_node - Ins_sec_1).argmin()] loc_sec = np.where(Ins_node == nearest)[0][0] loc_sec_1 = np.where(Ins_node == nearest_1)[0][0] # T_ins_sec = (T_ins[loc_sec] + T_ins[loc_sec_1]) / 2 # Insulation 초기온도 조건 if T_ins_step == 0: T_ins = np.full(n+1, T_wall) else: T_ins = np.linspace(T_wall, T2, n+1) def simpson(array, n): # simpson's rule integration = array[0] + array[-1] for i in range(1,n): if i%2 ==0: integration = integration + 2*array[i] else: integration = integration + 4*array[i] integration = integration / (len(array)-1) /3 return integration T_ins_ave = simpson(T_ins,n) dt_ins = 0 diffusivity = Cond_ins / (Cp_ins * D_ins) ## 제어기? 혹은 기준설정 후 자동으로 종료되게 만들기 # def Operation_criteria(Mode_list, Operation, Temperature, Composition): # ### [0] Inerting # ### [1] Inerting_N # ### [2] Gassing-up # ### [3] Cool-down # ### [4] Cool-down_N # ### [5] Warm-up # ### [6] Warm-up_N # ### [7] Aeration # Operation = Mode_list # if Operation.find("Cool") is not -1: # if Temperature < -140: # break # elif Operation.find("Inert") is not -1: # if Composition < 0.02: # break # Prop = Properties(Comp_name, Comp_init, "PT", 0.12, 0) """"""""""""""""""""""" Calculation """"""""""""""""""""""" # Supply 조건 지정. # Input_prop = "PQmass" # 2가지 고르기 (input에서) # Input1 = 0.106 # MPaA Input 1 값 # Input2 = 0 # Input 2 값 simulation = 120 # hours dt = 0.01 # hour Calculation = round(simulation / dt) # ### BOR check 하는 function 만들기 # BOG = BOG_calculation(Volume, FR, BOR, Comp_name, Pure_methane)[0] # BOG_check = BOR_check(BOG, Comp_name, Comp_init, P_init, FR, Step, LastStep, Target, Mode_list, 30) Mass_supply = 5000 ## kg/h # time_range = np.arange(dt, time + dt, dt) #### 우선 압력 고정일 때, ## Mass_supply 를 dt 에 대한 배열로 입력하는것도 고려해보기 ### Mode_list = ['Inerting', 'Inerting_N', 'Gassing-up', 'Cool-down', 'Cool-down_N', 'Warm-up', 'Warm-up_N', 'Aeration'] Operation = Mode_list[4] ###### Supply_condition(Comp_name, Mode_operation, Input_prop, Input1, Input2, Mass_supply, Calculation): # Supply = Supply_condition(Comp_name, Operation, "PQmass", 0.2, 0, Mass_supply, Calculation) # CD Supply = Supply_condition(Comp_name, Operation, "PT", 0.12, 40, Mass_supply, Calculation) # WU # Supply = Supply_condition(Comp_name, Operation, "PT", 0.15, 20, Mass_supply, Calculation) # Inert # Unitconv_nominal(Comp_name, Comp_init, 0.1, 40, 2, 4000) # Supply 유량 계산위한 def # def Unitconv_nominal(Comp_name, Comp, P, T, iflag, Value): ## def Heat_transfer(Supply_condition, Init_cond, P_mode, T_ins, T_ins_ave, Ins_node, dt): # Cooldown = Heat_transfer(Supply, Init_cond, 0, T_ins, T_ins_ave, Ins_node, dt) # Op_inert = Heat_transfer(Supply, Init_cond, 0, T_ins, T_ins_ave, Ins_node, dt) Warmup = Heat_transfer(Supply, Init_cond, 0, T_ins, T_ins_ave, Ins_node, dt) # Hold = Heat_transfer(Supply, Init_cond, 1, T_ins, T_ins_ave, Ins_node, dt) # BOR = Heat_transfer(Supply, Init_cond, 0, T_ins, T_ins_ave, Ins_node, dt) ### CHS 와 연계를 위해서 Tank info. 와 mode 같은것들은 다른걸로 빼는건 어떨지?? ### 기존 계산값에서 이어서 계산할수 있는 def 도 만들기 ### BOR check 하는 것 만들기... """"""""""""""""""""""" 추출 하기 """"""""""""""""""""""" ##pd.set_option('display.float_format', '{:,.4f}'.format) 다 안먹힘 ## pd.options.display.float_format = '{:.4f}'.format ## df.style.set_precision(4) # DataFrame Prop_col_name = ['Time', 'Tank Pressure', 'T_vap', 'T_wall', 'Density', 'Enthalpy', 'Mass_tank', 'Phase', 'Qmass', 'Mass_exhaust', 'Vol_exhaust', 'Amount_spray'] Ins_col_name = np.round(Ins_node.astype(np.float64),4) # Node 소수점이 4개 고정위해서 float64로 변환 Ins_col_name = Ins_col_name.tolist() Ins_col_name.append('Ins_ave') Ins_col_name.append('Ins_secondary') # df = pd.DataFrame(Cooldown[0], columns = Prop_col_name) df = pd.DataFrame(Warmup[0], columns = Prop_col_name) ###Time 열 분리 Index_time = df['Time'] df_unit = pd.DataFrame({'Time': ['hr'],'Tank Pressure': ['MPaA'], 'T_vap': ['C'], 'T_wall': ['C'], 'Density': ['kg/m3'], 'Enthalpy': ['kJ/kg'], 'Mass_tank': ['kg'], 'Phase': ['-'], 'Qmass': ['-'], 'Mass_exhaust': ['kg/hr'], 'Vol_exhaust': ['m3/hr'], 'Amount_supply': ['kg']},index=['Units']) df = pd.concat([df_unit, df]) df.set_index('Time', inplace = True) df_ins = pd.DataFrame(Warmup[1], columns = Ins_col_name, index = Index_time) # df_ins.style.set_precision(4) # DataFrame df_comp = pd.DataFrame(np.round(Warmup[2],4), columns = Comp_name_index, index = Index_time) """"""""""""""""""""""" 출력 하기 # """"""""""""""""""""""" # address = 'C:\\Python_code\\04_Tank model\\Tank_result\\' # df.to_csv(address+'Prop.csv', header = True, index= True) # df_comp.to_csv(address+'Comp.csv', header = True, index= True) # df_ins.to_csv(address+'Insulation.csv', header = True, index= True) ### GIF 만들기 # duration_rate = 0.01 # 속도 # frames_plot = [] # for plotname in plotnames: # if plotname.endswith(".png"): # # print(plotname) # frames_plot.append(imageio.imread(plotname)) # exportname = "Plot.gif" # imageio.mimsave(exportname, frames_plot, format='GIF', duration=duration_rate, loop=1) # loop = 0 무한대 # for plotname in set(plotnames): # os.remove(plotname)
Sorry, something went wrong.
No branches or pull requests
Tank_information
The text was updated successfully, but these errors were encountered: