ASSESSMENT OF HEAT EXCHANGER NETWORK IN BOILING HOUSE OF SUGAR PLANT TO INCREASE ENERGY EFFICIENCY VIA PINCH EXERGY ANALYSIS

• Main Author: Riadi, Indra
• Format: Theses
• Language: Indonesia
• Subjects: Teknik kimia
• Online Access: https://digilib.itb.ac.id/gdl/view/79339
• Institution: Institut Teknologi Bandung

Sulphitation process dominates the white sugar producing process in Indonesia. The application of sulphitation technology results in colored sugar and a high sulphur concentration. To improve the quality of white sugar, the most recent juice purification technique is Defecation Remelt and Carbonatation (DRC), which produces white sugar with the same quality as refined sugar. However, DRC technology involves multiple process manufacturing phases that require additional equipment and energy investment. This study investigates the energy optimization strategy of the sugar factory's boiling house with 2 (two) different juice purification technologies, namely the sulphitation process and the DRC process, using a combination of pinch analysis principles and comprehensive exergy analysis and comparing them from an energy standpoint after having exchange networks. fresh heat by taking pressure drop into consideration. To accomplish this purpose, the research will use process modeling aided by commercial simulators to analyze the performance of the boiling house in 2 (two) purification methods, the sulphitation process and the DRC process, after alteration of the heat exchanger network. Aspen Plus v.11 software was used to do steady-state modeling of a boiling house. Meanwhile, heat exchanger network (HEN) energy optimization is being performed using the Aspen Energy Analyzer v.11 software. The cane crushing rate that will be investigated in this study for two processes is 8,000 TCD at design capacity. Exergy lost for HEN optimization outcomes in the Sulfitation process was reduced by 2.17 MW, or 15.89%, from 13.63 MW to 11.46 MW. The decreasing exergy value indicates that after optimization, there is more heat supply that can be transferred to the cold stream than to the hot stream. From the optimization results reduced the Low Pressure Steam load by 17.8%, with a 16.07 MW drop in heating load. The Low Pressure Steam load has been reduced from 90.22 MW to 74.15 MW. The cooling consumption for the sulphitation process is 44.99 MW, a 14.7% decrease from the starting figure of 52.76 MW. With this amount, total utility demand (the sum of heating and cooling utilities) reduced by 18.11% or 25.90 MW in the HEN energy optimization scheme from 142.98 MW to 117.07 MW. The HEN optimization results in the DRC process reduced the exergy loss value by 6.30 MW, or by 41.69% from 15.12 MW to 8.82 MW. The decreasing exergy amount indicates that, after optimization, there is more heat supply available for transfer to the cold flow than to the hot flow. The optimization results achieved a 15.83% reduction in exhaust steam with a 13.52 MW reduction in heating load. The exhaust steam load is presently 71.93 MW, decreasing from the initially heating load of 85.45 MW. The cooling utility demand is 49.50 MW after HEN energy optimization, a decrease of 8.49% from the initial value of 57.99 MW. overall utility demand (the combination of heating and cooling utilities) reduced by 15.34% or 22.01 MW from the overall base case utility demand of 143.44 MW to 121.43 MW with this amount. When the energy value of the hot utility is compared between the two processes, the Sulfation process is 3% higher. There are energy savings in the DRC process due to the condensate Heater, which creates a surplus of sensible energy. While the cold utility's energy value is 9% lower. Having more condenser units with a larger overall evaporation capacity to the condenser in the DRC process. The pressure drop is calculated by comparing the HEN optimization method with the base case configuration. Heat exchangers, pumps, and pipes are all subjected to calculations. According to the study's findings after assessing the effect of pressure drop on equipment, in order to achieve the targeted energy optimization results, a larger equipment size will be required. According to the results of a comparison of economic calculations for the two processes, the DRK process has a longer payback period than the Sulphitation process. This is due to the higher capital required in the DRK boiling house process than in the Sulphitation process.