ZERO-DIMENSIONAL MODELING AND SIMULATION OF THE CARBON DIOXIDE CAPTURE PROCESS WITH AMMONIA SOLVENT
Abstract Carbon capture and storage is one option to reduce CO2 concentrations in the atmosphere. The carbon capture and storage project itself is still being developed. One carbon dioxide capture technology that is already in the commercial stage is capture using amine as a solvent. However,...
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| Format: | Final Project |
| Language: | Indonesia |
| Online Access: | https://digilib.itb.ac.id/gdl/view/81247 |
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| Institution: | Institut Teknologi Bandung |
| Language: | Indonesia |
| Summary: | Abstract
Carbon capture and storage is one option to reduce CO2 concentrations in the atmosphere.
The carbon capture and storage project itself is still being developed. One carbon dioxide capture
technology that is already in the commercial stage is capture using amine as a solvent. However,
currently research is being done as a substitute for amine solvents, namely ammonia. The dissolution
of carbon dioxide into ammonia occurs at low temperatures in a component called an absorber. The
stripper as a companion to the absorber is used to regenerate ammonia. In reality, the process of
simulating absorber and stripper components takes a long time and is not easy. Another alternative
that might be used is to use a flash distillation process.
This research analyzes the difficulties in modeling absorbers for multi-component systems
including variations in NH3 mass rate, dimensions of the absorber, and so on. Not only that, the main
thing is to simulate the flash's ability to replace the absorber and stripper with temperature variations
in the flash, heater and cooler capacity, and NH3 mass rate. The methods used for analysis are
ENRTL-RK, NRTL, and Pitzer. The results show that the maximum efficiency of using a flash is
approximately the same as using an absorber, namely in the range of 70–75%, the fluid temperature
in the absorber replacement flash for maximum efficiency is in the range of 10–20oC, and for the
maximum replacement flash the appropriate temperature is in the range 70–80oC. Variations in the
flash temperature of the absorber replacement show more significant results for changes in efficiency
compared to the NH3 mass rate and temperature variations in the stripper can produce changes in the
NH3/CO2 mole ratio compared to variations in heat duty. Temperature control and heating schemes
are also discussed in this study. |
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