The document summarizes experimental results from a process development unit (PDU) comparing CO2 removal from gas mixtures using aqueous solutions of monoethanolamine (MEA) and a mixture of 2-amino-2-methyl-1-propanol (AMP) and piperazine (PZ). Tests were conducted under identical energy input to the reboiler and similar process efficiencies. Results showed that using AMP/PZ can reduce solvent heat duty compared to MEA. Temperatures in the columns were also lower with AMP/PZ. Partial pressures of CO2 and temperatures measured within the absorber and stripper supported better performance with AMP/PZ versus MEA at equivalent operating conditions.
This document discusses the implementation of kinetic models into process simulators to simulate heterogeneous catalytic processes. It provides examples of kinetic modelling for methanol synthesis and bioethanol conversion reactions. Kinetic models like the Langmuir-Hinshelwood-Hougen-Watson model are preferred over simple power law models as they account for adsorption/desorption steps. The document outlines how to implement kinetic parameters from literature into simulators like Aspen Plus, including converting units and specifying temperature dependence and rate expressions. It emphasizes that accurate thermodynamic and transport property models are also needed for reliable process simulation.
Design and optimization of kemira leonard process for formic acid productionSanjanaSingh153
The document summarizes a study on the design and optimization of the Kemira-Leonard process for producing formic acid. Key aspects of the study included simulating the process in Aspen Plus, performing heat integration to reduce utility usage, sizing equipment and estimating capital costs, and conducting multi-objective optimization to minimize total capital and annual utility costs. The optimized process design was able to produce 98% formic acid at an annual capacity of 27,476 tonnes/year at minimized costs.
This study used Aspen HYSYS software to simulate a suspension (slurry) process for producing polyethylene. A loop reactor model mimicked the slurry polymerization process. The effects of increasing the ethylene monomer flow rate on solvent, catalyst, co-monomer, and hydrogen flow rates were examined. The model predicted that increasing the monomer flow rate linearly increased these other process variables. It also showed that a higher monomer flow rate led to greater polyethylene production. However, the model had the limitation of not accounting for temperature and pressure effects on other operating variables.
This document summarizes a study on the catalytic dehydration of methanol to dimethyl ether over γ-alumina. The researchers investigated the effects of temperature and feed composition on the conversion of methanol and deactivation of the catalyst. They found that methanol conversion strongly depended on the reactor operating temperature, increasing with higher temperatures. Using pure methanol as a feed resulted in slow catalyst deactivation, while adding water to the feed increased deactivation significantly. A temperature-dependent model was developed to predict methanol conversion and reasonably correlated with experimental data.
Water Gas Shift Reaction Characteristics Using Syngas from Waste Gasification inventionjournals
The characteristics of a high temperature water gas shift reaction over a commercial Fe-based catalyst using syngas from waste gasification were investigated using lab equipment tests and found to be feasible for producing valuable chemical products. The CO conversion and H2/CO ratio were observed using various values for the gas hourly space velocity(GHSV), steam/CO ratio, and temperature. The CO conversion and H2/CO ratio increased with increasing temperature, increasing steam/CO ratio and decreasing SV. The CO conversion values were 32.95% and 46.84% and the H2/CO ratios were 1.8 and 2.09 with temperatures of 350 C and 400C, respectively, when the steam/CO ratio was 2.4 and SV was 458 h-1 . The H2/CO ratio and CO conversion were 1.42 and 30.14%, respectively, when the steam/CO ratio was 1.45, and increased with an increase in the steam/CO ratio. The H2/CO ratio increased to 2.36 and the CO conversion increased to 51.70% when the steam/CO ratio was 3.44. However, the increase in the CO conversion was insignificant when the steam/CO ratio was greater than 2.9.
Deactivation Modeling through Separable Kinetics of Coking On Ni/CZ Catalyst ...IOSR Journals
Abstract : Steam methane reforming (SMR) is a very significant technique to produce hydrogen from fossil fuels. In this particular work, nickel is used as the active metal and ceria-zirconia (CZ) bi-metallic oxide is used as the support. The foremost challenge to this process is sooting or coking over the catalyst surface and blocking the active sites. For the economic viability of the catalyst, it is very significant to make it coke deposition resistant. This is the reason that the kinetic modeling of the deactivation is very important. Therefore, this paper is aimed to model the deactivation and activity of the catalyst. A rate model of the deactivation process is also developed using separable kinetics. A comparison with commercial catalyst is also reported to show that the Ni/CZ catalyst is much more stable towards the coking. Keywords –Coking, Deactivation, Methane, Separable kinetics, Steam reforming.
Adsorption of hydrogen sulfide using palm shell activated carboneSAT Journals
Abstract Removing H2S from biogas that is produced from anaerobic digestion of palm oil mill effluent is a crucial step in order for the biogas to be utilized as a source of energy. In this study, palm shell activated carbon (PSAC) prepared by steam activation was used to adsorb H2S from simulated biogas. The parameters studied were H2S concentration, adsorption temperature and space velocity. The effect of these parameters towards breakthrough adsorption capacity was studied using statistical analysis with Design Expert Software. H2S concentration and space velocity were found to be significant in affecting the breakthrough adsorption capacity.Adsorption temperature on its own was found not to have significant effect on the breakthrough adsorption capacity but its interaction with other parameters was found to be significant. Characterization of fresh and spent PSAC confirmed and provided further information on the adsorption of sulfur species on PSAC pore surface. Keywords: Activated carbon; Biogas; Hydrogen sulfide; Adsorption
The document presents a study on the hydrodynamic behavior of an external loop airlift reactor for two-phase systems. Experiments were conducted to determine the gas holdup and pressure drop characteristics of various electrolyte and solvent solutions at different concentrations and flow rates. The results show that gas holdup increases with superficial gas velocity and solvent concentration but decreases with electrolyte concentration, while pressure drop increases with gas velocity, liquid flow rate, and solution concentration.
This document discusses the implementation of kinetic models into process simulators to simulate heterogeneous catalytic processes. It provides examples of kinetic modelling for methanol synthesis and bioethanol conversion reactions. Kinetic models like the Langmuir-Hinshelwood-Hougen-Watson model are preferred over simple power law models as they account for adsorption/desorption steps. The document outlines how to implement kinetic parameters from literature into simulators like Aspen Plus, including converting units and specifying temperature dependence and rate expressions. It emphasizes that accurate thermodynamic and transport property models are also needed for reliable process simulation.
Design and optimization of kemira leonard process for formic acid productionSanjanaSingh153
The document summarizes a study on the design and optimization of the Kemira-Leonard process for producing formic acid. Key aspects of the study included simulating the process in Aspen Plus, performing heat integration to reduce utility usage, sizing equipment and estimating capital costs, and conducting multi-objective optimization to minimize total capital and annual utility costs. The optimized process design was able to produce 98% formic acid at an annual capacity of 27,476 tonnes/year at minimized costs.
This study used Aspen HYSYS software to simulate a suspension (slurry) process for producing polyethylene. A loop reactor model mimicked the slurry polymerization process. The effects of increasing the ethylene monomer flow rate on solvent, catalyst, co-monomer, and hydrogen flow rates were examined. The model predicted that increasing the monomer flow rate linearly increased these other process variables. It also showed that a higher monomer flow rate led to greater polyethylene production. However, the model had the limitation of not accounting for temperature and pressure effects on other operating variables.
This document summarizes a study on the catalytic dehydration of methanol to dimethyl ether over γ-alumina. The researchers investigated the effects of temperature and feed composition on the conversion of methanol and deactivation of the catalyst. They found that methanol conversion strongly depended on the reactor operating temperature, increasing with higher temperatures. Using pure methanol as a feed resulted in slow catalyst deactivation, while adding water to the feed increased deactivation significantly. A temperature-dependent model was developed to predict methanol conversion and reasonably correlated with experimental data.
Water Gas Shift Reaction Characteristics Using Syngas from Waste Gasification inventionjournals
The characteristics of a high temperature water gas shift reaction over a commercial Fe-based catalyst using syngas from waste gasification were investigated using lab equipment tests and found to be feasible for producing valuable chemical products. The CO conversion and H2/CO ratio were observed using various values for the gas hourly space velocity(GHSV), steam/CO ratio, and temperature. The CO conversion and H2/CO ratio increased with increasing temperature, increasing steam/CO ratio and decreasing SV. The CO conversion values were 32.95% and 46.84% and the H2/CO ratios were 1.8 and 2.09 with temperatures of 350 C and 400C, respectively, when the steam/CO ratio was 2.4 and SV was 458 h-1 . The H2/CO ratio and CO conversion were 1.42 and 30.14%, respectively, when the steam/CO ratio was 1.45, and increased with an increase in the steam/CO ratio. The H2/CO ratio increased to 2.36 and the CO conversion increased to 51.70% when the steam/CO ratio was 3.44. However, the increase in the CO conversion was insignificant when the steam/CO ratio was greater than 2.9.
Deactivation Modeling through Separable Kinetics of Coking On Ni/CZ Catalyst ...IOSR Journals
Abstract : Steam methane reforming (SMR) is a very significant technique to produce hydrogen from fossil fuels. In this particular work, nickel is used as the active metal and ceria-zirconia (CZ) bi-metallic oxide is used as the support. The foremost challenge to this process is sooting or coking over the catalyst surface and blocking the active sites. For the economic viability of the catalyst, it is very significant to make it coke deposition resistant. This is the reason that the kinetic modeling of the deactivation is very important. Therefore, this paper is aimed to model the deactivation and activity of the catalyst. A rate model of the deactivation process is also developed using separable kinetics. A comparison with commercial catalyst is also reported to show that the Ni/CZ catalyst is much more stable towards the coking. Keywords –Coking, Deactivation, Methane, Separable kinetics, Steam reforming.
Adsorption of hydrogen sulfide using palm shell activated carboneSAT Journals
Abstract Removing H2S from biogas that is produced from anaerobic digestion of palm oil mill effluent is a crucial step in order for the biogas to be utilized as a source of energy. In this study, palm shell activated carbon (PSAC) prepared by steam activation was used to adsorb H2S from simulated biogas. The parameters studied were H2S concentration, adsorption temperature and space velocity. The effect of these parameters towards breakthrough adsorption capacity was studied using statistical analysis with Design Expert Software. H2S concentration and space velocity were found to be significant in affecting the breakthrough adsorption capacity.Adsorption temperature on its own was found not to have significant effect on the breakthrough adsorption capacity but its interaction with other parameters was found to be significant. Characterization of fresh and spent PSAC confirmed and provided further information on the adsorption of sulfur species on PSAC pore surface. Keywords: Activated carbon; Biogas; Hydrogen sulfide; Adsorption
The document presents a study on the hydrodynamic behavior of an external loop airlift reactor for two-phase systems. Experiments were conducted to determine the gas holdup and pressure drop characteristics of various electrolyte and solvent solutions at different concentrations and flow rates. The results show that gas holdup increases with superficial gas velocity and solvent concentration but decreases with electrolyte concentration, while pressure drop increases with gas velocity, liquid flow rate, and solution concentration.
Presentation on "Study of process intensification of CO2 capture through modelling and simulation" given by Dr Meihong Wang from University of Hull in the Process Engineering Technical Session at the UKCCSRC Biannual Meeting in Cambridge on 2-3 April 2014
Feasibility study of mtbe physical adsorption from polluted water on gac, pac...eSAT Publishing House
IJRET : International Journal of Research in Engineering and Technology is an international peer reviewed, online journal published by eSAT Publishing House for the enhancement of research in various disciplines of Engineering and Technology. The aim and scope of the journal is to provide an academic medium and an important reference for the advancement and dissemination of research results that support high-level learning, teaching and research in the fields of Engineering and Technology. We bring together Scientists, Academician, Field Engineers, Scholars and Students of related fields of Engineering and Technology
Feasibility study of mtbe physical adsorption from polluted water on gac, pac...eSAT Journals
Abstract MTBE or Methyl Tertiary Butyl Ether is an organic compound, which is used to increase the gasoline Octane Number. At the beginning of 80’s, by discovering the undesirable effects of tetra ethyl lead usage in fuel, MTBE started to be used worldwide. But gradually the undesirable effects of MTBE on environment had been revealed. There are many technologies for MTBE removal from polluted water. Adsorption is the most conventional and economical technology. In this research, some experiments have been done for studying the adsorption of MTBE on different solid adsorbent in batch process. In these experiments a fixed amount of adsorbents including Granular Activated Carbon (GAC), Powdered Activated Carbon (PAC) and the Husk Rice Carbon (HRC) have been put in different one litter covered vessels containing water polluted with known initial MTBE concentration and stirring them. By measuring MTBE concentration in the vessel at different times the effect of different operating parameters such as temperature and pH have been studied on adsorption and optimum condition have been determined. The batch experimental results have been used to calculate the constant parameters of Freundlich and Langmuir adsorption isotherm equations for these systems. Keywords: MTBE, Adsorption, Activated Carbon, Husk Rice Carbon
Material Science and Engineering-B_Synthesis of ultra high molecular weight p...Shashi Kant
This document summarizes an article that appeared in a journal published by Elsevier. The attached copy is provided to the author for non-commercial research and education purposes only. The author is permitted to share the copy with colleagues and use it for teaching. However, reproducing, distributing, selling, licensing or posting the copy online is prohibited without permission from Elsevier. The authors are allowed to post their version of the article in Word or Tex format on their personal or institutional websites. Further information about Elsevier's archiving and manuscript policies can be found online.
The document describes an in situ study using UV-visible spectroscopy to measure the kinetics of propane oxidative dehydrogenation (ODH) on vanadium oxide catalysts. Transients in UV-visible intensity during ODH reactions were analyzed using a surface reaction mechanism. Rate constants for the kinetically relevant C-H bond activation step were determined and compared to values from steady-state ODH rates. The ratio of these values provides a measure of the fraction of active vanadium sites. Reoxidation rate constants, which cannot be obtained from steady-state analysis, were also determined and found to be orders of magnitude larger than C-H bond activation rates.
Methanol Steam Reforming in Pd-Ag Membrane Reactor for High Purity Hydrogen G...sameer_israni
The document summarizes Sameer Israni's research on methanol steam reforming in a palladium-silver membrane reactor. Key points:
1) Experiments and modeling were conducted to understand the effects of various species on hydrogen flux through Pd-Ag membranes during methanol steam reforming. Surface poisoning was found to be the main cause of reduced flux.
2) A packed bed membrane reactor with a single Pd-Ag fiber was tested and modeled. Higher temperatures and pressures led to increased hydrogen utilization and productivity.
3) A 3D model was developed to simulate large-scale multi-fiber membrane reactors and understand the effects of design parameters on productivity.
Dynamic Modeling for Gas Phase Propylene Copolymerization in a Fluidized Bed ...IJRES Journal
The document presents a dynamic two-phase model for a fluidized bed reactor used to produce polypropylene. The model divides the reactor into an emulsion phase and bubble phase, with reaction assumed to occur in both phases. Simulation results show the temperature profile is lower than previous single-phase models due to considering both phases. Approximately 13% of the produced polymer comes from the bubble phase, demonstrating the importance of accounting for both phases.
The document summarizes an experimental investigation on the performance of an air conditioner using R32 refrigerant. It begins with an abstract describing the refrigerant comparison experiment conducted on a 1.5 ton capacity air conditioning system using R22, R134a, and R32. Performance parameters like coefficient of performance, mass flow rate, and power to the compressor were calculated. The results and simulations showed R32 to be the most efficient refrigerant for retrofitting air conditioning systems due to its lower global warming potential and atmospheric lifetime compared to R22.
The document describes experimental studies of two cylindrical latent heat energy storage systems (LHESS) using lauric acid as the phase change material (PCM). The first is a horizontal cylinder with one finned copper pipe passing through the center. The second is a vertical cylinder with two finned copper pipes allowing for simultaneous charging and discharging. Experiments were conducted to study the phase change behavior of the PCM and heat transfer processes during charging, discharging, and simultaneous charging/discharging. Results show natural convection plays an important role in melting and simultaneous charging/discharging but less so in solidification.
Investigations into Advanced Laboratory Deactivation Methods for the Selectio...Zachary Sample
This document discusses methods for deactivating fresh fluid catalytic cracking (FCC) catalyst in the laboratory to simulate commercial equilibrium catalyst performance. Commonly used methods like cyclic deactivation and cyclic propene steaming can accurately mimic plant catalyst but are time-consuming. Rapid deactivation methods have been proposed as alternatives that can also simulate commercial catalyst performance without extensive testing procedures. This study aims to assess one such rapid deactivation method and characterize catalyst samples using techniques like XRD, TPR and SEM/EDX to evaluate its ability to predict commercial FCC performance.
This document summarizes a study that optimized parameters for the adsorption of hydrogen sulfide (H2S) using palm shell activated carbon. The parameters studied were H2S concentration, adsorption temperature, and space velocity. Statistical analysis was used to develop a regression model relating these parameters to breakthrough adsorption capacity. H2S concentration and space velocity had the most significant effects on capacity, with higher concentrations and lower space velocities resulting in higher capacity. Characterization of the activated carbon confirmed that H2S was being adsorbed onto pore surfaces.
1. The document describes a mathematical model developed to model esterification in a batch reactor coupled with pervaporation for producing ethyl acetate.
2. The model accounts for the reaction kinetics of esterification catalyzed by Amberlyst 15 resin and permeation rates of components through a polydimethylsiloxane membrane based on experimental data.
3. A parametric study using the model found that conversion increases with increasing temperature, molar ratios of reactants, and catalyst concentration, with optimal conditions being a temperature of around 343K, catalyst concentration of 10g, and 50% excess acetic acid relative to ethanol.
This document describes a computational fluid dynamics (CFD) study of methane decomposition into hydrogen and solid carbon in a packed bed fluid catalytic cracking (FCC) reactor. The study used CFD modeling in COMSOL Multiphysics to simulate the decomposition reaction over time in the packed bed reactor. Results showed that increasing the reaction time from 0 to 1000 seconds increased the production of hydrogen from 0 to 42 mol/dm3 and carbon from 0 to 21 mol/dm3, while decreasing methane concentration from 50 to 29 mol/dm3, indicating that decomposition was occurring. Spatial profiles of velocity, concentration, pressure and permeability within the reactor were also determined and discussed.
Amine Bearing Windows Opening Membrane for CO2 AdsorptionIRJET Journal
This document summarizes research on developing a membrane for capturing carbon dioxide (CO2) from gas mixtures. The membrane is a polysulfone composite containing dendrimers, which are spherical macromolecules that can incorporate amine groups. The membrane was characterized using various analytical techniques and showed CO2 adsorption through a chemical process. Adsorption experiments demonstrated the membrane effectively captured CO2 and followed a Langmuir adsorption isotherm model. The research aims to establish an efficient membrane technology for reducing CO2 emissions through adsorption-based separation.
This document describes the simulation and design of a process to recover monoethylene glycol (MEG) from effluent waste streams of a petrochemical company in Iran. Aspen Plus simulation software was used to model the process, which involves separating water, salts, and various glycols (MEG, DEG, TEG, TTEG) using a series of distillation columns. Sensitivity analyses were performed to optimize column parameters such as pressure, reflux ratio, and boilup ratio. The results showed that MEG, DEG, TEG, and TTEG could be recovered at rates of 5.01, 2.039, 0.062, and 0.089 kg/hr, respectively.
Macromol React Eng 2009 3 257262_Controlled Catalyst Dosing An ElegantShashi Kant
Ethylene polymerization using Ziegler-Natta catalysts comprising TiCl4 supported on MgCl2 with aluminum alkyls as co-catalyst produce UHMWPE through a mediated proportional reduction of the Ti oxidation states. The authors demonstrate molecular weight regulation of UHMWPE to be a combined function of hydrogen and the co-catalyst through controlled catalyst dosing and experimental optimization. Process optimization studies at 7.5 atm ethylene pressure could absorb small deviations in the catalyst systems to maintain the desired molecular weights of UHMWPE.
The document discusses methods for determining the carbon, hydrogen, nitrogen, and sulfur content of coal through ultimate analysis. It describes the standard Kjeldahl method for determining nitrogen, which involves digesting coal samples in sulfuric acid and a catalyst then distilling and titrating the resulting ammonia. Corrections may need to be made to carbon, hydrogen, and sulfur values depending on the forms in which they occur in coal. Automated systems now allow simultaneous determination of multiple elements.
This document presents a theoretical and experimental analysis of a direct-fired double effect lithium bromide/water absorption chiller located at a lighting technology company in Egypt. The chiller has a cooling capacity of 500 tons and uses a parallel flow configuration. Temperature measurements were taken at various points in the chiller components in July 2013 and July 2014. Mathematical equations were developed to model the chiller and estimate the coefficient of performance and heat transfer rates based on temperature and flow rate data. Theoretical and experimental analyses were conducted to evaluate how the COP is affected by factors like heat exchanger effectiveness and circulation ratio. The results show that the chiller's COP was lower in 2014 compared to 2013, possibly due to degradation of the heat ex
This document reviews biomass gasification technologies for producing hydrogen-rich syngas to be used in ammonia production as an alternative to natural gas. It summarizes the conventional natural gas-based process and outlines a potential process using biomass gasification. Several gasification technologies are assessed based on syngas composition, efficiency, operating conditions, scale, and experience with biomass. The goal is to evaluate biomass gasification for ammonia production through life cycle assessment and techno-economic analysis to identify environmental and economic impacts compared to conventional production.
Catalytic Upgrading of Methane to Higher Hydrocarbon in a Non-oxidative Chemi...Shaima Nahreen
This document discusses catalytic upgrading of methane to higher hydrocarbons using ruthenium catalysts. Ruthenium supported on zeolite ZSM-5 catalysts showed higher methane conversion compared to ruthenium supported on silica. With 3% ruthenium on ZSM-5, methane conversion increased above 700°C producing hydrocarbons from C4 to C10. This catalyst also produced some aromatic compounds. Ruthenium supported on ZSM-5 was found to produce methyl radicals and lower the activation energy of methane more than ruthenium supported on silica based on density functional theory analyses.
This document summarizes a pilot plant study on capturing CO2 from power plant flue gas using a vacuum swing adsorption (VSA) process with zeolite 13X. Key findings include:
1) A basic 4-step VSA cycle was able to achieve 95.9% CO2 purity and 86.4% recovery from a 15% CO2 flue gas stream.
2) A modified 4-step cycle with light product pressurization and two beds achieved improved performance of 94.8% purity and 89.7% recovery.
3) Energy consumption in the pilot plant was 339-583 kWh/tonne of CO2 captured, higher than theoretical calculations due to non
This document summarizes a study on the kinetics of methanol synthesis from carbon dioxide hydrogenation over copper-zinc oxide catalysts. Experiments were conducted in a fixed bed reactor between 200-230°C, 50-80 bar, and gas hourly space velocities of 7,800-23,400 h-1 using feeds with H2:CO2 ratios of 2-6 without CO. Kinetic parameters from a previous study were optimized to model the experimental data using a Langmuir–Hinshelwood–Hougen–Watson mechanism. The influences of catalyst support (alumina vs zirconia) and operating conditions on kinetics were examined. The goal was to determine optimized parameters to reliably scale-up the
Presentation on "Study of process intensification of CO2 capture through modelling and simulation" given by Dr Meihong Wang from University of Hull in the Process Engineering Technical Session at the UKCCSRC Biannual Meeting in Cambridge on 2-3 April 2014
Feasibility study of mtbe physical adsorption from polluted water on gac, pac...eSAT Publishing House
IJRET : International Journal of Research in Engineering and Technology is an international peer reviewed, online journal published by eSAT Publishing House for the enhancement of research in various disciplines of Engineering and Technology. The aim and scope of the journal is to provide an academic medium and an important reference for the advancement and dissemination of research results that support high-level learning, teaching and research in the fields of Engineering and Technology. We bring together Scientists, Academician, Field Engineers, Scholars and Students of related fields of Engineering and Technology
Feasibility study of mtbe physical adsorption from polluted water on gac, pac...eSAT Journals
Abstract MTBE or Methyl Tertiary Butyl Ether is an organic compound, which is used to increase the gasoline Octane Number. At the beginning of 80’s, by discovering the undesirable effects of tetra ethyl lead usage in fuel, MTBE started to be used worldwide. But gradually the undesirable effects of MTBE on environment had been revealed. There are many technologies for MTBE removal from polluted water. Adsorption is the most conventional and economical technology. In this research, some experiments have been done for studying the adsorption of MTBE on different solid adsorbent in batch process. In these experiments a fixed amount of adsorbents including Granular Activated Carbon (GAC), Powdered Activated Carbon (PAC) and the Husk Rice Carbon (HRC) have been put in different one litter covered vessels containing water polluted with known initial MTBE concentration and stirring them. By measuring MTBE concentration in the vessel at different times the effect of different operating parameters such as temperature and pH have been studied on adsorption and optimum condition have been determined. The batch experimental results have been used to calculate the constant parameters of Freundlich and Langmuir adsorption isotherm equations for these systems. Keywords: MTBE, Adsorption, Activated Carbon, Husk Rice Carbon
Material Science and Engineering-B_Synthesis of ultra high molecular weight p...Shashi Kant
This document summarizes an article that appeared in a journal published by Elsevier. The attached copy is provided to the author for non-commercial research and education purposes only. The author is permitted to share the copy with colleagues and use it for teaching. However, reproducing, distributing, selling, licensing or posting the copy online is prohibited without permission from Elsevier. The authors are allowed to post their version of the article in Word or Tex format on their personal or institutional websites. Further information about Elsevier's archiving and manuscript policies can be found online.
The document describes an in situ study using UV-visible spectroscopy to measure the kinetics of propane oxidative dehydrogenation (ODH) on vanadium oxide catalysts. Transients in UV-visible intensity during ODH reactions were analyzed using a surface reaction mechanism. Rate constants for the kinetically relevant C-H bond activation step were determined and compared to values from steady-state ODH rates. The ratio of these values provides a measure of the fraction of active vanadium sites. Reoxidation rate constants, which cannot be obtained from steady-state analysis, were also determined and found to be orders of magnitude larger than C-H bond activation rates.
Methanol Steam Reforming in Pd-Ag Membrane Reactor for High Purity Hydrogen G...sameer_israni
The document summarizes Sameer Israni's research on methanol steam reforming in a palladium-silver membrane reactor. Key points:
1) Experiments and modeling were conducted to understand the effects of various species on hydrogen flux through Pd-Ag membranes during methanol steam reforming. Surface poisoning was found to be the main cause of reduced flux.
2) A packed bed membrane reactor with a single Pd-Ag fiber was tested and modeled. Higher temperatures and pressures led to increased hydrogen utilization and productivity.
3) A 3D model was developed to simulate large-scale multi-fiber membrane reactors and understand the effects of design parameters on productivity.
Dynamic Modeling for Gas Phase Propylene Copolymerization in a Fluidized Bed ...IJRES Journal
The document presents a dynamic two-phase model for a fluidized bed reactor used to produce polypropylene. The model divides the reactor into an emulsion phase and bubble phase, with reaction assumed to occur in both phases. Simulation results show the temperature profile is lower than previous single-phase models due to considering both phases. Approximately 13% of the produced polymer comes from the bubble phase, demonstrating the importance of accounting for both phases.
The document summarizes an experimental investigation on the performance of an air conditioner using R32 refrigerant. It begins with an abstract describing the refrigerant comparison experiment conducted on a 1.5 ton capacity air conditioning system using R22, R134a, and R32. Performance parameters like coefficient of performance, mass flow rate, and power to the compressor were calculated. The results and simulations showed R32 to be the most efficient refrigerant for retrofitting air conditioning systems due to its lower global warming potential and atmospheric lifetime compared to R22.
The document describes experimental studies of two cylindrical latent heat energy storage systems (LHESS) using lauric acid as the phase change material (PCM). The first is a horizontal cylinder with one finned copper pipe passing through the center. The second is a vertical cylinder with two finned copper pipes allowing for simultaneous charging and discharging. Experiments were conducted to study the phase change behavior of the PCM and heat transfer processes during charging, discharging, and simultaneous charging/discharging. Results show natural convection plays an important role in melting and simultaneous charging/discharging but less so in solidification.
Investigations into Advanced Laboratory Deactivation Methods for the Selectio...Zachary Sample
This document discusses methods for deactivating fresh fluid catalytic cracking (FCC) catalyst in the laboratory to simulate commercial equilibrium catalyst performance. Commonly used methods like cyclic deactivation and cyclic propene steaming can accurately mimic plant catalyst but are time-consuming. Rapid deactivation methods have been proposed as alternatives that can also simulate commercial catalyst performance without extensive testing procedures. This study aims to assess one such rapid deactivation method and characterize catalyst samples using techniques like XRD, TPR and SEM/EDX to evaluate its ability to predict commercial FCC performance.
This document summarizes a study that optimized parameters for the adsorption of hydrogen sulfide (H2S) using palm shell activated carbon. The parameters studied were H2S concentration, adsorption temperature, and space velocity. Statistical analysis was used to develop a regression model relating these parameters to breakthrough adsorption capacity. H2S concentration and space velocity had the most significant effects on capacity, with higher concentrations and lower space velocities resulting in higher capacity. Characterization of the activated carbon confirmed that H2S was being adsorbed onto pore surfaces.
1. The document describes a mathematical model developed to model esterification in a batch reactor coupled with pervaporation for producing ethyl acetate.
2. The model accounts for the reaction kinetics of esterification catalyzed by Amberlyst 15 resin and permeation rates of components through a polydimethylsiloxane membrane based on experimental data.
3. A parametric study using the model found that conversion increases with increasing temperature, molar ratios of reactants, and catalyst concentration, with optimal conditions being a temperature of around 343K, catalyst concentration of 10g, and 50% excess acetic acid relative to ethanol.
This document describes a computational fluid dynamics (CFD) study of methane decomposition into hydrogen and solid carbon in a packed bed fluid catalytic cracking (FCC) reactor. The study used CFD modeling in COMSOL Multiphysics to simulate the decomposition reaction over time in the packed bed reactor. Results showed that increasing the reaction time from 0 to 1000 seconds increased the production of hydrogen from 0 to 42 mol/dm3 and carbon from 0 to 21 mol/dm3, while decreasing methane concentration from 50 to 29 mol/dm3, indicating that decomposition was occurring. Spatial profiles of velocity, concentration, pressure and permeability within the reactor were also determined and discussed.
Amine Bearing Windows Opening Membrane for CO2 AdsorptionIRJET Journal
This document summarizes research on developing a membrane for capturing carbon dioxide (CO2) from gas mixtures. The membrane is a polysulfone composite containing dendrimers, which are spherical macromolecules that can incorporate amine groups. The membrane was characterized using various analytical techniques and showed CO2 adsorption through a chemical process. Adsorption experiments demonstrated the membrane effectively captured CO2 and followed a Langmuir adsorption isotherm model. The research aims to establish an efficient membrane technology for reducing CO2 emissions through adsorption-based separation.
This document describes the simulation and design of a process to recover monoethylene glycol (MEG) from effluent waste streams of a petrochemical company in Iran. Aspen Plus simulation software was used to model the process, which involves separating water, salts, and various glycols (MEG, DEG, TEG, TTEG) using a series of distillation columns. Sensitivity analyses were performed to optimize column parameters such as pressure, reflux ratio, and boilup ratio. The results showed that MEG, DEG, TEG, and TTEG could be recovered at rates of 5.01, 2.039, 0.062, and 0.089 kg/hr, respectively.
Macromol React Eng 2009 3 257262_Controlled Catalyst Dosing An ElegantShashi Kant
Ethylene polymerization using Ziegler-Natta catalysts comprising TiCl4 supported on MgCl2 with aluminum alkyls as co-catalyst produce UHMWPE through a mediated proportional reduction of the Ti oxidation states. The authors demonstrate molecular weight regulation of UHMWPE to be a combined function of hydrogen and the co-catalyst through controlled catalyst dosing and experimental optimization. Process optimization studies at 7.5 atm ethylene pressure could absorb small deviations in the catalyst systems to maintain the desired molecular weights of UHMWPE.
The document discusses methods for determining the carbon, hydrogen, nitrogen, and sulfur content of coal through ultimate analysis. It describes the standard Kjeldahl method for determining nitrogen, which involves digesting coal samples in sulfuric acid and a catalyst then distilling and titrating the resulting ammonia. Corrections may need to be made to carbon, hydrogen, and sulfur values depending on the forms in which they occur in coal. Automated systems now allow simultaneous determination of multiple elements.
This document presents a theoretical and experimental analysis of a direct-fired double effect lithium bromide/water absorption chiller located at a lighting technology company in Egypt. The chiller has a cooling capacity of 500 tons and uses a parallel flow configuration. Temperature measurements were taken at various points in the chiller components in July 2013 and July 2014. Mathematical equations were developed to model the chiller and estimate the coefficient of performance and heat transfer rates based on temperature and flow rate data. Theoretical and experimental analyses were conducted to evaluate how the COP is affected by factors like heat exchanger effectiveness and circulation ratio. The results show that the chiller's COP was lower in 2014 compared to 2013, possibly due to degradation of the heat ex
This document reviews biomass gasification technologies for producing hydrogen-rich syngas to be used in ammonia production as an alternative to natural gas. It summarizes the conventional natural gas-based process and outlines a potential process using biomass gasification. Several gasification technologies are assessed based on syngas composition, efficiency, operating conditions, scale, and experience with biomass. The goal is to evaluate biomass gasification for ammonia production through life cycle assessment and techno-economic analysis to identify environmental and economic impacts compared to conventional production.
Catalytic Upgrading of Methane to Higher Hydrocarbon in a Non-oxidative Chemi...Shaima Nahreen
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[Chemical and process engineering] pdu scale experimental results of co2 removal with amp pz solvent
1. Chemical and Process Engineering 2015, 36 (1), 39-48
DOI: 10.1515/cpe-2015-0003
*Corresponding author, e-mail: dspiewak@ichpw.pl
1
PDU – Process Development Unit cpe.czasopisma.pan.pl; degruyter.com/view/j/cpe
39
PDU1
-SCALE EXPERIMENTAL RESULTS OF CO2 REMOVAL
WITH AMP/PZ SOLVENT
Dariusz Śpiewak*
, Aleksander Krótki, Tomasz Spietz, Marcin Stec,
Lucyna Więcław–Solny, Adam Tatarczuk, Andrzej Wilk
Institute for Chemical Processing of Coal, ul. Zamkowa 1, 41-803 Zabrze, Poland
This paper provides a discussion concerning results of CO2 removal from a gas mixture by the
application of aqueous solutions of ethanoloamine (MEA) and 2-amino-2-methyl-1-propanol (AMP)
promoted with piperazine (PZ). The studies were conducted using a process development unit.
Research of such a scale provides far more reliable representation of the actual industrial process
than modelling and laboratory tests. The studies comprised comparative analyses entailing identical
energy supplied to a reboiler as well as tests conducted at similar process efficiencies for both
solvents. The results thus obtained imply that using AMP/PZ enables reduction of the solvent heat
duty. Moreover, while using AMP/PZ temperature decrease was also observed in the columns.
Keywords: CO2 capture, MEA, AMP, PZ
1. INTRODUCTION
CO2 removal by the absorption method using amines seems to be the simplest solution to apply in coal-
fired power plants (Dreszer and Więcław-Solny, 2008). Unlike other CO2 emission reduction methods,
such as oxy-fuel combustion, the amine-based process of CO2 removal may be applied while erecting
new power units as well as in existing power generation facilities. The possibility to deploy a CO2
removal section in the existing facilities is actually one of the most significant factors taken into
account while making the choice of technology. It allows for the process to be implemented without the
need for considerable structural modifications in the power plant's technological line. The capability of
using any of the technologies currently offered by the chemical industry (Chen et al., 2013; Farla et al.,
1995) is limited due to characteristic flue gas parameters, such as low flue gas pressure, low partial
pressure of CO2 present in flue gas released from typical coal-fired units or high moisture content in the
flue gas.
In the amine-based process of removing acidic components from gas mixtures, ethanolamine (MEA)
has been used for years (Barchas and Davis, 1992; Sander and Mariz, 1992). It is characterised by a
high reaction rate and a high CO2 absorption capacity on low partial CO2 pressures (Wilk et al., 2013b).
Moreover, ethanolamine is a relatively cheap raw material As far as the disadvantages of ethanolamine
are concerned, one should mention high heat of CO2 absorption, which affects the energy that must be
delivered to regenerate the solvent (Kim and Svendsen, 2007). It is also susceptible to considerable
degradation, both thermal (Davis and Rochelle, 2009) and oxidation (Fredriksen and Jens, 2013)
induced, due to the oxygen content in flue gas. The aqueous solution of ethanolamine shows corrosive
properties, particularly at high temperatures and on high CO2 saturation (Kittel et al., 2009). Hence the
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2. D. Śpiewak et al., Chem. Process Eng., 2015, 36 (1), 39-48
40 cpe.czasopisma.pan.pl; degruyter.com/view/j/cpe
search for amines characterised by absorption capacity and reaction rate comparable to MEA, but not
displaying negative features of MEA. One of the available options in the search for efficient solvents is
using mixtures of amines of diversified properties. Primary and secondary amines are known for high
reaction rate (Vaidya and Kenig, 2007), Tertiary amines, such as N-methyldiethanolamine (MDEA)
display lower reaction energy compared to lower amines (Kim and Svendsen, 2007; Svensson et al.,
2013). However, the CO2 absorption process rate is far lower with tertiary amines (Wilk et al., 2013a).
Similar properties can be observed in amines with steric hindrance, such as 2-amino-2-methyl-1-
propanol (AMP). In the reaction of AMP and CO2, transient carbamate is formed, whereas CO2 mainly
reacts to form carbonate and bicarbonate ions. AMP is characterised by low energy demand for
regeneration compared to MEA (Wilk et al., 2014; Xie et al., 2013). In order to increase the reaction
rate of amines with steric hindrance and tertiary amines, primary and secondary amines are used as
activators. Such a mixture retains high absorption capacity, but its reaction rate increases considerably.
The amine used to activate both MDEA and AMP is piperazine (PZ). It is a heterocyclic amine
featuring a ring of two secondary amine groups. Aqueous mixtures of AMP/PZ and MDEA PZ are
characterised by a higher reaction rate than solutions not containing PZ (Wilk et al., 2013b). It is also
possible to use mixtures of different amines and water-soluble organic fluids. Owing to the lower
content of water, such mixtures are characterised by lower specific heat, which makes it possible to
reduce the energy consumption involved in the solvent regeneration process.
2. PLANT CHARACTERISTICS
The process development unit (PDU) used to study the process of CO2 removal by means of amines is
one of three units of this type used by the Institute for Chemical Processing of Coal. It has been
installed at the Centre for Clean Coal Technologies in Zabrze (Lajnert and Latkowska, 2013). Besides
that, the Institute also uses a laboratory-scale installation (Krótki et al., 2012) and mobile pilot plant
(Więcław-Solny et al., 2014) for post-combustion carbon capture research.
The testing unit presented in this paper is a transition-scale unit. However, unlike other plants, it can be
used to study CO2 removal from flue gas, process gas and mixtures of technical gases. The testing unit
overview and its schematic diagram are shown in Fig. 1.
The gas mixture is delivered to a pre-treatment scrubber where the gas becomes water saturated, and
the mixture is cooled down and cleaned of all particulate. Then it flows through a solid adsorption bed
where SOx are removed. Once it is free of SOx, the gas flows to an absorber where CO2 absorption
takes place by means of an aqueous amine solution. The system draws benefits from a split flow
arrangement of regenerated solution streams (Szczypiński et al., 2013). It is for this modification that
energy consumption of the regeneration process can be reduced. Semi-lean amine is delivered to the
lower absorber section, whereas lean amine is healed to the column top. Purified gas flows through an
additional packing layer at the top of the absorption column, where water condensate is fed from
a separator behind the stripper. The purpose of this section is to wash out droplets of solvent carried
together with a purified gas from the column and cool down the gas leaving the absorber at the same
time. The semi-lean amine is collected from a mid-level tray and delivered to the absorber. The
remaining part of the solvent flows off to the lower column section where it is regenerated in the
regenerator reboiler heated by an electric heater. The lean amine solution is delivered to the absorber
top. Streams of solvent are involved in mutual heat exchange in a system of plate heat exchangers. The
composition of gas at the system inlet and outlet was monitored on-line by means of ULTRAMAT 23
gas analysers. The solvent was analysed using the KEM DA-640 densitometer and by titration. The
amine content in the solvent was measured by means of the Dionex ion chromatograph by titration
methods.
The most important parameters of the system have been collected in Table 1.
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3. PDU-scale experimental results of CO2 removal with AMP/PZ solvent
cpe.czasopisma.pan.pl; degruyter.com/view/j/cpe 41
Fig. 1. Overview and process flow diagram of the testing unit
Table 1. Testing unit parameters
Parameter Value Unit
Nominal gas flow rate 100 [Nm3
/h]
Nominal solvent flow rate 0.515 [m3
/h]
Lean amine temperature 40 [°C]
Max. reboiler power 33 [kW]
Absorber pressure 130 [kPa]
Stripper pressure 145 [kPa]
Total absorber packing height 3.2 [m]
Absorber diameter 0.263 [m]
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4. D. Śpiewak et al., Chem. Process Eng., 2015, 36 (1), 39-48
42 cpe.czasopisma.pan.pl; degruyter.com/view/j/cpe
3. EXPERIMENTAL
The aim of this paper is to discuss energy consumption in the carbon capture process based on the
experimental comparison of two different solvents. Laboratory scale tests of the carbon dioxide
absorption alone are not sufficient to determine the behaviour of the solvent in industrial processes
therefore it seems reasonable to test the solvent in PDU scale, being closer to a full-scale industrial
process. Additionally, based on PDU scale results, it is possible to propose the solvent for a process
scale-up, for example for a pilot plant. The results were compared with the literature sources. Heat duty
for AMP/PZ solvent obtained during the research on our own laboratory rig and pilot plant were also
presented. Furthermore, the temperature and CO2 concentration profiles in the columns were also
measured.
Under the experimental studies, comparative tests were conducted using the following aqueous
solutions:
30% MEA
30% AMP 10% PZ
The ethanolamine solution was used as a reference for other solvents examined. In the course of the
laboratory tests of the CO2 absorption (Wilk et al., 2014), no formation of solid products of the CO2
reaction with the amines present in the relevant solutions within the system's range of operating
temperatures was observed. The Monoethanolamine (>98%), 2-amino-2-methyl-1-propanol (90%) and
piperazine (>99%) were all purchased from Sigma-Aldrich. Aqueous solutions were prepared
according to pre-defined concentrations. The gas examined was a mixture of CO2 and N2. Both gases
were supplied by Messer. The gas composition was adjusted to match the average CO2 concentration
similar to the flue gas studied at the Tauron’s pilot plant. The plant features more than 100
measurement points (temperature, pressure, fluid level, flow rate). Figure 2 below illustrates fluid and
gas sample taking points as well as the arrangement of temperature measurement points within the
absorption column.
Fig. 2. Arrangement of measurement points
The tests were conducted in a steady state for several hours. Liquid and gaseous samples were collected
from individual analysis points. The MEA tests were performed on a higher reboiler power in order to
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5. PDU-scale experimental results of CO2 removal with AMP/PZ solvent
cpe.czasopisma.pan.pl; degruyter.com/view/j/cpe 43
attain the efficiency of ca. 90%. The AMP/PZ tests were carried out under identical conditions and on a
lower reboiler power, so that the efficiency of ca. 90% could be attained. The parameters describing the
conducted tests have been collated in Table 2. Gas flow rates, values of pressure in the apparatus as
well as temperatures of the solvent delivered to the absorber were constant for all the tests.
Table 2. Process conditions for trials
Test Solvent
Gas flow
rate
[Nm3
/h]
CO2
[% vol.]
Lean amine
flow rate
[m3
/h]
Semi-lean
amine flow
rate [m3
/h]
Reboiler
power
[kW]
1 MEA 99.8 12.27 0.255 0.260 33
2 MEA 99.4 12.27 0.306 0.310 33
3 AMP/PZ 99.7 12.38 0.306 0.310 33
4 AMP/PZ 98.9 12.33 0.254 0.260 33
5 AMP/PZ 99.9 12.32 0.254 0.260 24.75
6 AMP/PZ 100.5 12.30 0.304 0.315 24.75
4. RESULTS
The tests have made it possible to compare values of efficiency and reboiler heat duty in the
regeneration process for different solvents. For the power of 33 W, the efficiency values recorded for
AMP/PZ significantly exceed the level of 90%. When MEA is used, the efficiency values are about
90%. For both solvents, slightly higher process efficiency is attained at an increased solvent flow rate.
Due to the decreased desorption time while raising the solvent flow rate, the quality of solvent
regeneration drops. Tests conducted at the solvent flow rate of 0.615 m3
/h are characterised by higher
loading of rich and lean amine, which is typical of both solvent types. The loading for AMP/PZ is
lower compared to MEA. Since the heat absorption of AMP/PZ is lower than of MEA, AMP/PZ
regenerates better when the same energy is delivered during regeneration. Moreover, the CO2
absorption rate decreases as the loading rises. This fact triggers the increased rate of the CO2 absorption
process with AMP/PZ compared to MEA. Table 4 provides a summary of partial CO2 pressure data and
temperatures inside the absorber and the stripper.
Fig. 3. Distribution of CO2 partial pressure (a), absorber temperature (b) and stripper temperature (c)
for MEA and AMP/PZ at reboiler power 33kW
a) b) c)
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6. D. Śpiewak et al., Chem. Process Eng., 2015, 36 (1), 39-48
44 cpe.czasopisma.pan.pl; degruyter.com/view/j/cpe
Having measured the partial CO2 pressure profiles and the temperatures inside the absorber and the
stripper (Figs. 3 a, b, c and Tables 3, 4, 5), one can observe that the partial CO2 pressure is lower at
each point for AMP/PZ. The stripper temperature is also slightly lower, whereas the most significant
differences can be observed in the absorber. On the account of lower heat of absorption, a smaller
amount of heat is released for AMP/PZ. For both MEA and AMP/PZ, the highest temperature occurs at
the lower absorber section. It may imply that it is the point at which the absorption process rate is the
highest, since the relatively high partial CO2 pressure affects the absorption process driving factor.
Table 3. Measured values of CO2 partial pressure for all the tests
CO2 partial pressure [kPa]
Column height [m] 1 2 3 4 5 6
0.00 15.95 15.96 16.09 16.02 16.01 16.00
0.20 12.68 13.55 10.67 12.14 13.69 11.79
1.50 9.76 9.19 6.21 7.51 10.49 10.70
3.14 4.81 4.38 2.04 2.51 5.02 5.90
3.74 3.21 2.91 0.53 0.96 2.99 2.85
4.60 2.00 1.87 0.22 0.53 2.02 2.07
5.15 1.99 1.83 0.19 0.49 1.97 1.97
Table 4. Measured values of absorber temperatures for all the tests
Absorber temperature [°C]
Column
height [m]
Measured phase 1 2 3 4 5 6
0.00 liquid phase 50.0 52.1 54.2 53.3 52.0 50.1
0.41 liquid phase 54.7 56.7 56.5 55.5 53.3 52.8
1.28 liquid phase 71.4 59.4 52.6 69.6 62.1 54.6
3.30 liquid phase 66.8 53.9 44.5 62.1 64.5 58.5
3.75 liquid phase 59.9 45.2 42.1 48.9 55.3 46.7
5.15 vapour phase 50.8 39.7 37.2 44.8 49.8 46.1
A similar correlation between the maximum temperature and maximum rate of absorption process has
been discussed in the literature (Asendrych et al., 2013; Niegodajew et al., 2013). Reboiler heat duty in
the solvent regeneration process is higher when MEA is used. On account of the identical power
supplied to the reboiler, it only depends on the amount of CO2 removed. Reboiler heat duty is a
correlation between the energy supplied to the process and the mass of CO2 removed. Reboiler heat
duty values provided entail the losses of heat released to the environment.
Table 5. Measured values of stripper temperatures for all the tests
Stripper temperature [°C]
Column
height [m]
Measured phase 1 2 3 4 5 6
0.00 liquid phase 112.4 112.1 110.4 110.7 110.0 107.3
0.20 liquid phase 111.6 111.3 110.1 110.2 108.1 107.2
0.60 liquid phase 108.2 107.2 106.3 106.3 99.2 97.1
2.35 liquid phase 106.4 105.7 103.8 105.5 95.8 92 8
4.35 liquid phase 103.1 102.6 100.7 101.8 92.4 90.8
5.78 vapour phase 97.7 99.0 97.6 99.1 84.2 82.2
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7. PDU-scale experimental results of CO2 removal with AMP/PZ solvent
cpe.czasopisma.pan.pl; degruyter.com/view/j/cpe 45
Fig. 4. Distribution of CO2 partial pressure (a), absorber temperature (b) and stripper temperature (c) for AMP/PZ
at different solvent flow rate
Further tests using AMP/PZ were aimed at comparing the results obtained for solvents at a similar
value of CO2 removal process efficiency. The power delivered to the regenerator was reduced to a level
enabling process efficiency of ca. 90% to be obtained. Based on the data thus acquired, one could
observe an increase loading amine for the tests run on reduced power. The process rate attained when
using a regenerated solution of higher loading is lower, and hence the decrease in the process
efficiency. Insofar as the loading of the lean amine did not increase much, the semi-lean amine loading
was considerable, approaching the value typical for rich amine. The temperature profile (Fig. 4) implies
that the maximum absorber temperature point shifted up the column for both solvent flow rates which
was probably due to moving the area of the highest process rate. And as in the previous case, the major
impact is exerted by partial CO2 pressure, being higher along the entire height of the column for lower
power capacities.
Furthermore, a solution of a relatively high loading is supplied to the lower column section, causing the
process driving force to be low in this part of the column. The CO2 removal efficiencies are similar for
both solvent flow rates. When comparing Figs. 4b and 4c one can notice that the temperatures of the
absorber and of the stripper decrease at the increasing solvent flow rate.
Comparing partial pressure and temperature distributions (Fig. 5) for tests with similar efficiency for
MEA and AMP/PZ, one may observe significant differences in temperature profiles. Temperatures in
columns are far lower when AMP/PZ is used. The maximum temperature difference between both
solvents comes to ca. 10C. A similar temperature difference occurs at the stripper top. The higher the
mixture temperature leaving the stripper, the larger the quantity of cooling water needed to effectively
cool it. Moreover, the partial pressure of steam increases as temperature rises, which triggers an
increase of the quantity of water condensing in the separator. Having analysed the loading values, one
can certainly notice that loading values of rich and of the semi-lean one are rather similar for both
solvents. However, the loading of the lean amine is lower for AMP/PZ.
Lean amine loading increases insignificantly as the solvent amine flow rate increase.
The reboiler heat duty for tests involving smaller power is much lower in comparison with both
AMP/PZ tests for larger powers as well as for MEA. Compared to MEA, the reboiler heat duty was
dropped by more than 25% while similar efficiency was maintained.
a) b) c)
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8. D. Śpiewak et al., Chem. Process Eng., 2015, 36 (1), 39-48
46 cpe.czasopisma.pan.pl; degruyter.com/view/j/cpe
Fig. 5. Distribution of CO2 partial pressure (a), absorber temperature (b) and stripper temperature (c) for MEA
and AMP/PZ at similar process efficiency
Table 6. Efficiency, reboiler heat duty and CO2 loading for all the tests
Test
Efficiency
[%]
Reboiler heat
duty
[MJ/kg CO2]
L/G ratio
[kg/kg]
Rich amine
loading
[mol/mol]
Lean amine
loading
[mol/mol]
Semi-lean
amine
loading
[mol/mol]
1 88.6 5.21 4.33 0.43 0.21 0.30
2 89.5 5.12 5.12 0.40 0.22 0.31
3 98.9 4.80 5.08 0.27 0.05 0.16
4 96.9 4.88 4.25 0.21 0.04 0.10
5 90.6 3.69 4.17 0.38 0.09 0.29
6 88.8 3.81 5.15 0.38 0.12 0.33
Table 7 contains a comparison of the results with literature data for AMP/PZ aqueous solvents. It can
be seen that the reboiler heat duty obtained during the tests is comparable to that for CESAR1 solvent
(Mangalapally and Hasse, 2011). This similarity can be partly explained by a comparable concentration
of the CESAR1 solvent, which is 45 wt% (28 wt% AMP and 17 wt% PZ). The concentration of the
second solvent used in this comparison is 30 wt% (25 wt% AMP and 5 wt% PZ) (Artanto et al., 2014;
and Table 7).
Table 7. Comparison of the efficiencies and reboiler heat duties with literature data
Source
Gas flow rate
[Nm3
/h]
L/G ratio
Efficiency
[%]
Reboiler heat
duty
[MJ/kg CO2]
Mangalapally and Hasse (2011) ≈ 66 1.4 [kg/kg] 90 3.3
Artanto et al. (2014) 100 5.6 [m3
/1000m3
] 85 4.9
This paper 100 4.17 [kg/kg] 90.6 3.69
From our research it can be seen that an increase of the scale of the plant causes a decrease in the heat
duty of the reboiler (Table 8). The lowest reboiler heat duty can be observed for pilot plant tests where
a) b) c)
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9. PDU-scale experimental results of CO2 removal with AMP/PZ solvent
cpe.czasopisma.pan.pl; degruyter.com/view/j/cpe 47
similar removal efficiency was achieved for all units. This fact is related to the increase of efficiency of
heat exchangers while increasing the scale and the decrease of overall heat losses to ambient. The
laboratory unit works in standard process flow sheet, while other plants use modified, advanced process
flow sheets allowing the reduction of energy consumption.
Table 8. Scaling up effects of the efficiencies and reboiler heat duties
Unit type
Gas flow rate
[Nm3
/h]
L/G ratio
[kg/kg]
Efficiency
[%]
Reboiler heat
duty
[MJ/kg CO2]
Laboratory unit 5 8.15 89.7 4.84
PDU 100 4.17 90.6 3.69
Pilot plant 200 3.92 89.9 3.13
5. CONCLUSION
A comparison of test results obtained for both solvents studied implies a considerable drop in the
reboiler heat duty on similar process efficiency attained when using AMP/PZ. Furthermore, the
temperatures recorded for AMP/PZ both in the absorber and the regenerator were lower than those
when MEA was applied, even for identical energy supplied to the reboiler. Increasing the L/G ratio
causes a slight efficiency increase for both solvents in the case when power of 33 kW is applied.
However, as regards AMP/PZ, the efficiency slightly declines for decreased power. Increasing the L/G
ratio also triggers an increase in the solvent loading value and a drop of temperatures in both columns.
The results presented in this paper were obtained during research co-financed by the National Centre
of Research and Development in the framework of Contract SP/E/1/67484/10 – Strategic Research
Programme – Advanced technologies for energy generation: Development of a technology for highly
efficient zero-emission coal-fired power units integrated with CO2 capture.
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Received 16 September 2014
Received in revised form 19 January 2053
Accepted 28 January 2015
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