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Norifumi Matsumiya - One of the best experts on this subject based on the ideXlab platform.
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Evaluation of energy consumption for separation of CO2 in flue gas by hollow fiber facilitated transport membrane module with permeation of amine Solution
Separation and Purification Technology, 2005Co-Authors: Norifumi Matsumiya, Masaaki Teramoto, Satoshi Kitada, Hideto MatsuyamaAbstract:Abstract Energy consumption for the separation of CO 2 in flue gas by a novel hollow fiber facilitated transport membrane module was evaluated and compared with those by conventional separation processes such as gas absorption and polymeric membrane separation. In the novel facilitated transport membrane system, both a feed gas (CO 2 /N 2 mixture) and a carrier Solution (aqueous diethanolamine Solution) are supplied to the lumen side (feed side, high pressure side) of the hollow fiber ultrafiltration membrane module and flow upward. The carrier Solution, which contains dissolved solute gas, CO 2 in the present case, permeates the membrane to the permeate side (low pressure side, shell side), where the Solution liberates dissolved gas to become a Lean Solution and the Lean Solution is returned to the lumen side by a pump. The feed side pressure was atmospheric and the permeate side pressure was controlled in the range from 10 to 27 kPa. CO 2 in the feed gas consisting of 10% CO 2 and 90% N 2 was concentrated to higher than 99%. The effects of various system parameters, such as permeate side pressure, temperature, gas and liquid flow rates and the inner diameter of hollow fiber membrane, on the energy consumption for CO 2 recovery were investigated. Energy consumption decreased with increasing temperature and had a minimum at an optimum permeate side pressure. The minimum energy consumption was estimated as 0.211 kWh kg-CO 2 −1 when the inner diameter of the hollow fiber was 0.8 mm. The energy consumption increased with feed gas flow rate, however, it was little influenced by liquid flow rate. The energy consumption decreased remarkably with increasing the inner diameter of the hollow fiber, and it was estimated as 0.072 kWh kg-CO 2 −1 when hollow fibers of 1.4 mm in inner diameter were used. This value is the lowest among those reported so far.
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ethylene ethane separation and concentration by hollow fiber facilitated transport membrane module with permeation of silver nitrate Solution
Separation and Purification Technology, 2005Co-Authors: Masaaki Teramoto, Satoshi Shimizu, Hideto Matsuyama, Norifumi MatsumiyaAbstract:Abstract Novel hollow fiber facilitated transport membrane modules were used for ethylene/ethane separation using an aqueous silver nitrate Solution as a carrier Solution. In this membrane system, a feed gas consisting of 80 mol% C 2 H 4 and 20 mol% C 2 H 6 and an aqueous 4 M silver nitrate Solution are supplied to the lumen side (high pressure side, feed side) of a hollow fiber ultrafiltration membrane module and flow upward. In the lumen, the Solution absorbs C 2 H 4 selectively to become a rich or laden Solution. Some part of the rich Solution permeates the membrane to the permeate side (low pressure side, shell side) and other part of the Solution leaves the module from its top and then it is supplied to the top of the shell side, where the absorbed gas is stripped from the rich Solution and recovered as enriched ethylene. The Lean Solution is circulated to the lumen of the hollow fiber module by a pump. The feed side pressure was from 200 to 500 kPa and the permeate side pressure was atmospheric. Three modules with different liquid permeability and design were used in experiments. The module, in which the carrier Solution permeated the membrane at the upper part of the module, had higher performance than the module in which the Solution permeated at the lower part. The module, in which the Solution did not permeate the membrane, also had high performance although a large gas–liquid separator was needed downstream of the module. The module efficiency, which is defined as the ratio of the experimentally observed ethylene recovery to the recovery calculated by assuming gas–liquid phase equilibria at both sides of the membrane, was from 61 to almost 100%. Ethylene in the feed gas was concentrated from 80 to 99.8 mol%. The maximum C 2 H 4 permeance was 1.1 × 10 −4 mol m −2 s −1 kPa −1 (3.3 × 10 −4 cm 3 cm −2 s −1 cm Hg −1 ) and the selectivity of C 2 H 4 over C 2 H 6 was about 375 at the ethylene partial pressure of 164 kPa. The maximum ethylene recovery was 87% when the mean residence time of the feed gas in the module was 4.9 s. The membrane was confirmed to be stable during a series of experiments.
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CO2 capture and enrichment by novel hollow fiber facilitated transport membrane module with low energy consumption
Greenhouse Gas Control Technologies 7, 2005Co-Authors: Masaaki Teramoto, Satoshi Kitada, Nobuaki Ohnishi, Norifumi Matsumiya, Satoshi Shimizu, Hideto Matsuyama, Miho Nakamura, Kazuhiro Okabe, Hiroshi ManoAbstract:Publisher Summary This chapter proposes a novel gas separation method using capillary membrane modules for simultaneous recovery and enrichment of CO2 in simulated flue gases. Several capillary membrane modules were fabricated with different dimensions and experiments were performed at several conditions by using an amine and an amino acid as the carriers of CO2. The energy consumption of the current process is compared to those of conventional gas absorption processes and membrane gas separation processes using polymeric membranes. Both a feed gas and a carrier Solution are supplied to the feed side (high pressure side) of the capillary ultrafiltration membrane module and flow upward. Most of the carrier Solution that contains dissolved CO2 permeates the membrane to the permeate side (low-pressure side), where the Solution liberates CO2 to become a Lean Solution and the Lean Solution is returned to the lumen of the capillary module by a pump. Experiments were performed at several operational conditions by using diethanolamine (DEA) and 2, 3-diaminopropionic acid (DAPA) as carriers. The energy required for CO2 capture, enrichment, and liquefaction was about 0.27kWh kgC02-1, which is much lower than those by using polymeric membranes, conventional gas absorption processes consisting of absorption and stripping column. The proposed process is promising for the CO2 recovery with low energy consumption.
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Ethylene/ethane separation and concentration by hollow fiber facilitated transport membrane module with permeation of silver nitrate Solution
Separation and Purification Technology, 2005Co-Authors: Masaaki Teramoto, Satoshi Shimizu, Hideto Matsuyama, Norifumi MatsumiyaAbstract:Abstract Novel hollow fiber facilitated transport membrane modules were used for ethylene/ethane separation using an aqueous silver nitrate Solution as a carrier Solution. In this membrane system, a feed gas consisting of 80 mol% C 2 H 4 and 20 mol% C 2 H 6 and an aqueous 4 M silver nitrate Solution are supplied to the lumen side (high pressure side, feed side) of a hollow fiber ultrafiltration membrane module and flow upward. In the lumen, the Solution absorbs C 2 H 4 selectively to become a rich or laden Solution. Some part of the rich Solution permeates the membrane to the permeate side (low pressure side, shell side) and other part of the Solution leaves the module from its top and then it is supplied to the top of the shell side, where the absorbed gas is stripped from the rich Solution and recovered as enriched ethylene. The Lean Solution is circulated to the lumen of the hollow fiber module by a pump. The feed side pressure was from 200 to 500 kPa and the permeate side pressure was atmospheric. Three modules with different liquid permeability and design were used in experiments. The module, in which the carrier Solution permeated the membrane at the upper part of the module, had higher performance than the module in which the Solution permeated at the lower part. The module, in which the Solution did not permeate the membrane, also had high performance although a large gas–liquid separator was needed downstream of the module. The module efficiency, which is defined as the ratio of the experimentally observed ethylene recovery to the recovery calculated by assuming gas–liquid phase equilibria at both sides of the membrane, was from 61 to almost 100%. Ethylene in the feed gas was concentrated from 80 to 99.8 mol%. The maximum C 2 H 4 permeance was 1.1 × 10 −4 mol m −2 s −1 kPa −1 (3.3 × 10 −4 cm 3 cm −2 s −1 cm Hg −1 ) and the selectivity of C 2 H 4 over C 2 H 6 was about 375 at the ethylene partial pressure of 164 kPa. The maximum ethylene recovery was 87% when the mean residence time of the feed gas in the module was 4.9 s. The membrane was confirmed to be stable during a series of experiments.
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separation and concentration of co2 by capillary type facilitated transport membrane module with permeation of carrier Solution
Journal of Membrane Science, 2004Co-Authors: Masaaki Teramoto, Satoshi Kitada, Nobuaki Ohnishi, Hideto Matsuyama, Norifumi MatsumiyaAbstract:A novel facilitated transport membrane module for gas separation is proposed in which a carrier Solution is forced to permeate the membrane. Both a feed gas and a carrier Solution are supplied to the lumen side (high-pressure side, feed side) of the capillary ultrafiltration membrane module and flow upward. Most of the carrier Solution which contains dissolved solute gas, CO2 in the present case, permeates the membrane to the permeate side (low-pressure side, shell side), where the Solution liberates dissolved gas to become a Lean Solution, and the Lean Solution is returned to the lumen of the capillary module by a pump. This type of capillary membrane module was applied to the separation of CO2 from model flue gases consisting of CO2 and N2 using various amines as carriers or absorbents of CO2. The feed side pressure was atmospheric and the permeate side pressure was controlled at 9–27 kPa. CO2 in the feed was successfully concentrated from 1.5–15 to 98.5–99.8 mol%. When the CO2 mole fraction in the feed was 0.1 and the mean residence time of gas in the module was 0.28 s, the CO2 permeance was 3.8×10−4 mol m−2 s−1 kPa−1 (1.1×10−3 cm3 cm−2 s−1 cmHg−1) and the CO2 recovery was 76%. The selectivity of CO2 over N2 was in the range from about 800 to 8000. The membrane was very stable over a discontinuous 4-month testing period. The energy consumption was found to be much smaller than those of conventional chemical absorption and membrane separation processes.
Masaaki Teramoto - One of the best experts on this subject based on the ideXlab platform.
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Evaluation of energy consumption for separation of CO2 in flue gas by hollow fiber facilitated transport membrane module with permeation of amine Solution
Separation and Purification Technology, 2005Co-Authors: Norifumi Matsumiya, Masaaki Teramoto, Satoshi Kitada, Hideto MatsuyamaAbstract:Abstract Energy consumption for the separation of CO 2 in flue gas by a novel hollow fiber facilitated transport membrane module was evaluated and compared with those by conventional separation processes such as gas absorption and polymeric membrane separation. In the novel facilitated transport membrane system, both a feed gas (CO 2 /N 2 mixture) and a carrier Solution (aqueous diethanolamine Solution) are supplied to the lumen side (feed side, high pressure side) of the hollow fiber ultrafiltration membrane module and flow upward. The carrier Solution, which contains dissolved solute gas, CO 2 in the present case, permeates the membrane to the permeate side (low pressure side, shell side), where the Solution liberates dissolved gas to become a Lean Solution and the Lean Solution is returned to the lumen side by a pump. The feed side pressure was atmospheric and the permeate side pressure was controlled in the range from 10 to 27 kPa. CO 2 in the feed gas consisting of 10% CO 2 and 90% N 2 was concentrated to higher than 99%. The effects of various system parameters, such as permeate side pressure, temperature, gas and liquid flow rates and the inner diameter of hollow fiber membrane, on the energy consumption for CO 2 recovery were investigated. Energy consumption decreased with increasing temperature and had a minimum at an optimum permeate side pressure. The minimum energy consumption was estimated as 0.211 kWh kg-CO 2 −1 when the inner diameter of the hollow fiber was 0.8 mm. The energy consumption increased with feed gas flow rate, however, it was little influenced by liquid flow rate. The energy consumption decreased remarkably with increasing the inner diameter of the hollow fiber, and it was estimated as 0.072 kWh kg-CO 2 −1 when hollow fibers of 1.4 mm in inner diameter were used. This value is the lowest among those reported so far.
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ethylene ethane separation and concentration by hollow fiber facilitated transport membrane module with permeation of silver nitrate Solution
Separation and Purification Technology, 2005Co-Authors: Masaaki Teramoto, Satoshi Shimizu, Hideto Matsuyama, Norifumi MatsumiyaAbstract:Abstract Novel hollow fiber facilitated transport membrane modules were used for ethylene/ethane separation using an aqueous silver nitrate Solution as a carrier Solution. In this membrane system, a feed gas consisting of 80 mol% C 2 H 4 and 20 mol% C 2 H 6 and an aqueous 4 M silver nitrate Solution are supplied to the lumen side (high pressure side, feed side) of a hollow fiber ultrafiltration membrane module and flow upward. In the lumen, the Solution absorbs C 2 H 4 selectively to become a rich or laden Solution. Some part of the rich Solution permeates the membrane to the permeate side (low pressure side, shell side) and other part of the Solution leaves the module from its top and then it is supplied to the top of the shell side, where the absorbed gas is stripped from the rich Solution and recovered as enriched ethylene. The Lean Solution is circulated to the lumen of the hollow fiber module by a pump. The feed side pressure was from 200 to 500 kPa and the permeate side pressure was atmospheric. Three modules with different liquid permeability and design were used in experiments. The module, in which the carrier Solution permeated the membrane at the upper part of the module, had higher performance than the module in which the Solution permeated at the lower part. The module, in which the Solution did not permeate the membrane, also had high performance although a large gas–liquid separator was needed downstream of the module. The module efficiency, which is defined as the ratio of the experimentally observed ethylene recovery to the recovery calculated by assuming gas–liquid phase equilibria at both sides of the membrane, was from 61 to almost 100%. Ethylene in the feed gas was concentrated from 80 to 99.8 mol%. The maximum C 2 H 4 permeance was 1.1 × 10 −4 mol m −2 s −1 kPa −1 (3.3 × 10 −4 cm 3 cm −2 s −1 cm Hg −1 ) and the selectivity of C 2 H 4 over C 2 H 6 was about 375 at the ethylene partial pressure of 164 kPa. The maximum ethylene recovery was 87% when the mean residence time of the feed gas in the module was 4.9 s. The membrane was confirmed to be stable during a series of experiments.
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CO2 capture and enrichment by novel hollow fiber facilitated transport membrane module with low energy consumption
Greenhouse Gas Control Technologies 7, 2005Co-Authors: Masaaki Teramoto, Satoshi Kitada, Nobuaki Ohnishi, Norifumi Matsumiya, Satoshi Shimizu, Hideto Matsuyama, Miho Nakamura, Kazuhiro Okabe, Hiroshi ManoAbstract:Publisher Summary This chapter proposes a novel gas separation method using capillary membrane modules for simultaneous recovery and enrichment of CO2 in simulated flue gases. Several capillary membrane modules were fabricated with different dimensions and experiments were performed at several conditions by using an amine and an amino acid as the carriers of CO2. The energy consumption of the current process is compared to those of conventional gas absorption processes and membrane gas separation processes using polymeric membranes. Both a feed gas and a carrier Solution are supplied to the feed side (high pressure side) of the capillary ultrafiltration membrane module and flow upward. Most of the carrier Solution that contains dissolved CO2 permeates the membrane to the permeate side (low-pressure side), where the Solution liberates CO2 to become a Lean Solution and the Lean Solution is returned to the lumen of the capillary module by a pump. Experiments were performed at several operational conditions by using diethanolamine (DEA) and 2, 3-diaminopropionic acid (DAPA) as carriers. The energy required for CO2 capture, enrichment, and liquefaction was about 0.27kWh kgC02-1, which is much lower than those by using polymeric membranes, conventional gas absorption processes consisting of absorption and stripping column. The proposed process is promising for the CO2 recovery with low energy consumption.
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Ethylene/ethane separation and concentration by hollow fiber facilitated transport membrane module with permeation of silver nitrate Solution
Separation and Purification Technology, 2005Co-Authors: Masaaki Teramoto, Satoshi Shimizu, Hideto Matsuyama, Norifumi MatsumiyaAbstract:Abstract Novel hollow fiber facilitated transport membrane modules were used for ethylene/ethane separation using an aqueous silver nitrate Solution as a carrier Solution. In this membrane system, a feed gas consisting of 80 mol% C 2 H 4 and 20 mol% C 2 H 6 and an aqueous 4 M silver nitrate Solution are supplied to the lumen side (high pressure side, feed side) of a hollow fiber ultrafiltration membrane module and flow upward. In the lumen, the Solution absorbs C 2 H 4 selectively to become a rich or laden Solution. Some part of the rich Solution permeates the membrane to the permeate side (low pressure side, shell side) and other part of the Solution leaves the module from its top and then it is supplied to the top of the shell side, where the absorbed gas is stripped from the rich Solution and recovered as enriched ethylene. The Lean Solution is circulated to the lumen of the hollow fiber module by a pump. The feed side pressure was from 200 to 500 kPa and the permeate side pressure was atmospheric. Three modules with different liquid permeability and design were used in experiments. The module, in which the carrier Solution permeated the membrane at the upper part of the module, had higher performance than the module in which the Solution permeated at the lower part. The module, in which the Solution did not permeate the membrane, also had high performance although a large gas–liquid separator was needed downstream of the module. The module efficiency, which is defined as the ratio of the experimentally observed ethylene recovery to the recovery calculated by assuming gas–liquid phase equilibria at both sides of the membrane, was from 61 to almost 100%. Ethylene in the feed gas was concentrated from 80 to 99.8 mol%. The maximum C 2 H 4 permeance was 1.1 × 10 −4 mol m −2 s −1 kPa −1 (3.3 × 10 −4 cm 3 cm −2 s −1 cm Hg −1 ) and the selectivity of C 2 H 4 over C 2 H 6 was about 375 at the ethylene partial pressure of 164 kPa. The maximum ethylene recovery was 87% when the mean residence time of the feed gas in the module was 4.9 s. The membrane was confirmed to be stable during a series of experiments.
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separation and concentration of co2 by capillary type facilitated transport membrane module with permeation of carrier Solution
Journal of Membrane Science, 2004Co-Authors: Masaaki Teramoto, Satoshi Kitada, Nobuaki Ohnishi, Hideto Matsuyama, Norifumi MatsumiyaAbstract:A novel facilitated transport membrane module for gas separation is proposed in which a carrier Solution is forced to permeate the membrane. Both a feed gas and a carrier Solution are supplied to the lumen side (high-pressure side, feed side) of the capillary ultrafiltration membrane module and flow upward. Most of the carrier Solution which contains dissolved solute gas, CO2 in the present case, permeates the membrane to the permeate side (low-pressure side, shell side), where the Solution liberates dissolved gas to become a Lean Solution, and the Lean Solution is returned to the lumen of the capillary module by a pump. This type of capillary membrane module was applied to the separation of CO2 from model flue gases consisting of CO2 and N2 using various amines as carriers or absorbents of CO2. The feed side pressure was atmospheric and the permeate side pressure was controlled at 9–27 kPa. CO2 in the feed was successfully concentrated from 1.5–15 to 98.5–99.8 mol%. When the CO2 mole fraction in the feed was 0.1 and the mean residence time of gas in the module was 0.28 s, the CO2 permeance was 3.8×10−4 mol m−2 s−1 kPa−1 (1.1×10−3 cm3 cm−2 s−1 cmHg−1) and the CO2 recovery was 76%. The selectivity of CO2 over N2 was in the range from about 800 to 8000. The membrane was very stable over a discontinuous 4-month testing period. The energy consumption was found to be much smaller than those of conventional chemical absorption and membrane separation processes.
Jian-feng Chen - One of the best experts on this subject based on the ideXlab platform.
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Study of Gas Dehydration Process by Ionic Liquid Method in a Rotating Packed Bed
Energy & Fuels, 2017Co-Authors: Weiwei Geng, Jian-feng Chen, Gao Lidong, Hong ZhaoAbstract:The dehydration of moist air using ionic liquids (ILs) in a rotating packed bed (RPB) was innovatively studied. The effects of operating conditions, including rotational speed, liquid and gas flow rate, temperature, inlet gas water content, and water content of Lean Solution on the water dew point depression (ΔTd) in the RPB, were systematically studied. The experimental results showed that the water dew point depression can be up to 40 °C under the optimum experimental conditions of a motor speed of 1695 rpm, a liquid–gas ratio of 9 L/m3, temperature of 20 °C, Lean Solution water content of 0.8 wt %, and inlet gas water content of 18.77 g/m3. Moreover, a correlation to predict the water dew point depression was established, and the data predicted by the correlation is consistent with the data of experiment, with deviations of ±10%. This work exhibits great potential application of ILs in gas dehydration process in a RPB.
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Mass-Transfer Characteristics of the CO2 Absorption Process in a Rotating Packed Bed
Energy & Fuels, 2016Co-Authors: Miaopeng Sheng, Fuming Zhang, Lili Zhang, Jian-feng ChenAbstract:This article presents systematic investigations on the mass-transfer characteristics, including the overall gas-phase volumetric mass-transfer coefficient (KGa) and the height of mass-transfer unit (HTU), of the CO2 absorption process into a mixture of diethylenetriamine (DETA) and piperazine (PZ) Solution in a rotating packed bed (RPB). The effects of operating conditions, including PZ concentration, rotation speed, liquid volumetric flow rate, gas volumetric flow rate, gas treatment capacity of packing, inlet CO2 mole fraction, temperature, CO2 loading of Lean Solution, and distributor specification on KGa and HTU in the RPB, were systematically studied. Also, a comparison of CO2 absorption performance between the packed column with Dixon rings packing and the RPB is presented. Results indicate that both KGa and HTU were significantly affected by rotation speed, liquid volumetric flow rate, gas volumetric flow rate, temperature, and Lean CO2 loading while the PZ concentration, inlet CO2 mole fraction, a...
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Mass-Transfer Characteristics of the CO2 Absorption Process in a Rotating Packed Bed
Energy & Fuels, 2016Co-Authors: Miaopeng Sheng, Fuming Zhang, Lili Zhang, Jian-feng ChenAbstract:This article presents systematic investigations on the mass-transfer characteristics, including the overall gas-phase volumetric mass-transfer coefficient (KGa) and the height of mass-transfer unit (HTU), of the CO2 absorption process into a mixture of diethylenetriamine (DETA) and piperazine (PZ) Solution in a rotating packed bed (RPB). The effects of operating conditions, including PZ concentration, rotation speed, liquid volumetric flow rate, gas volumetric flow rate, gas treatment capacity of packing, inlet CO2 mole fraction, temperature, CO2 loading of Lean Solution, and distributor specification on KGa and HTU in the RPB, were systematically studied. Also, a comparison of CO2 absorption performance between the packed column with Dixon rings packing and the RPB is presented. Results indicate that both KGa and HTU were significantly affected by rotation speed, liquid volumetric flow rate, gas volumetric flow rate, temperature, and Lean CO2 loading while the PZ concentration, inlet CO2 mole fraction, a...
Hideto Matsuyama - One of the best experts on this subject based on the ideXlab platform.
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Evaluation of energy consumption for separation of CO2 in flue gas by hollow fiber facilitated transport membrane module with permeation of amine Solution
Separation and Purification Technology, 2005Co-Authors: Norifumi Matsumiya, Masaaki Teramoto, Satoshi Kitada, Hideto MatsuyamaAbstract:Abstract Energy consumption for the separation of CO 2 in flue gas by a novel hollow fiber facilitated transport membrane module was evaluated and compared with those by conventional separation processes such as gas absorption and polymeric membrane separation. In the novel facilitated transport membrane system, both a feed gas (CO 2 /N 2 mixture) and a carrier Solution (aqueous diethanolamine Solution) are supplied to the lumen side (feed side, high pressure side) of the hollow fiber ultrafiltration membrane module and flow upward. The carrier Solution, which contains dissolved solute gas, CO 2 in the present case, permeates the membrane to the permeate side (low pressure side, shell side), where the Solution liberates dissolved gas to become a Lean Solution and the Lean Solution is returned to the lumen side by a pump. The feed side pressure was atmospheric and the permeate side pressure was controlled in the range from 10 to 27 kPa. CO 2 in the feed gas consisting of 10% CO 2 and 90% N 2 was concentrated to higher than 99%. The effects of various system parameters, such as permeate side pressure, temperature, gas and liquid flow rates and the inner diameter of hollow fiber membrane, on the energy consumption for CO 2 recovery were investigated. Energy consumption decreased with increasing temperature and had a minimum at an optimum permeate side pressure. The minimum energy consumption was estimated as 0.211 kWh kg-CO 2 −1 when the inner diameter of the hollow fiber was 0.8 mm. The energy consumption increased with feed gas flow rate, however, it was little influenced by liquid flow rate. The energy consumption decreased remarkably with increasing the inner diameter of the hollow fiber, and it was estimated as 0.072 kWh kg-CO 2 −1 when hollow fibers of 1.4 mm in inner diameter were used. This value is the lowest among those reported so far.
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ethylene ethane separation and concentration by hollow fiber facilitated transport membrane module with permeation of silver nitrate Solution
Separation and Purification Technology, 2005Co-Authors: Masaaki Teramoto, Satoshi Shimizu, Hideto Matsuyama, Norifumi MatsumiyaAbstract:Abstract Novel hollow fiber facilitated transport membrane modules were used for ethylene/ethane separation using an aqueous silver nitrate Solution as a carrier Solution. In this membrane system, a feed gas consisting of 80 mol% C 2 H 4 and 20 mol% C 2 H 6 and an aqueous 4 M silver nitrate Solution are supplied to the lumen side (high pressure side, feed side) of a hollow fiber ultrafiltration membrane module and flow upward. In the lumen, the Solution absorbs C 2 H 4 selectively to become a rich or laden Solution. Some part of the rich Solution permeates the membrane to the permeate side (low pressure side, shell side) and other part of the Solution leaves the module from its top and then it is supplied to the top of the shell side, where the absorbed gas is stripped from the rich Solution and recovered as enriched ethylene. The Lean Solution is circulated to the lumen of the hollow fiber module by a pump. The feed side pressure was from 200 to 500 kPa and the permeate side pressure was atmospheric. Three modules with different liquid permeability and design were used in experiments. The module, in which the carrier Solution permeated the membrane at the upper part of the module, had higher performance than the module in which the Solution permeated at the lower part. The module, in which the Solution did not permeate the membrane, also had high performance although a large gas–liquid separator was needed downstream of the module. The module efficiency, which is defined as the ratio of the experimentally observed ethylene recovery to the recovery calculated by assuming gas–liquid phase equilibria at both sides of the membrane, was from 61 to almost 100%. Ethylene in the feed gas was concentrated from 80 to 99.8 mol%. The maximum C 2 H 4 permeance was 1.1 × 10 −4 mol m −2 s −1 kPa −1 (3.3 × 10 −4 cm 3 cm −2 s −1 cm Hg −1 ) and the selectivity of C 2 H 4 over C 2 H 6 was about 375 at the ethylene partial pressure of 164 kPa. The maximum ethylene recovery was 87% when the mean residence time of the feed gas in the module was 4.9 s. The membrane was confirmed to be stable during a series of experiments.
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CO2 capture and enrichment by novel hollow fiber facilitated transport membrane module with low energy consumption
Greenhouse Gas Control Technologies 7, 2005Co-Authors: Masaaki Teramoto, Satoshi Kitada, Nobuaki Ohnishi, Norifumi Matsumiya, Satoshi Shimizu, Hideto Matsuyama, Miho Nakamura, Kazuhiro Okabe, Hiroshi ManoAbstract:Publisher Summary This chapter proposes a novel gas separation method using capillary membrane modules for simultaneous recovery and enrichment of CO2 in simulated flue gases. Several capillary membrane modules were fabricated with different dimensions and experiments were performed at several conditions by using an amine and an amino acid as the carriers of CO2. The energy consumption of the current process is compared to those of conventional gas absorption processes and membrane gas separation processes using polymeric membranes. Both a feed gas and a carrier Solution are supplied to the feed side (high pressure side) of the capillary ultrafiltration membrane module and flow upward. Most of the carrier Solution that contains dissolved CO2 permeates the membrane to the permeate side (low-pressure side), where the Solution liberates CO2 to become a Lean Solution and the Lean Solution is returned to the lumen of the capillary module by a pump. Experiments were performed at several operational conditions by using diethanolamine (DEA) and 2, 3-diaminopropionic acid (DAPA) as carriers. The energy required for CO2 capture, enrichment, and liquefaction was about 0.27kWh kgC02-1, which is much lower than those by using polymeric membranes, conventional gas absorption processes consisting of absorption and stripping column. The proposed process is promising for the CO2 recovery with low energy consumption.
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Ethylene/ethane separation and concentration by hollow fiber facilitated transport membrane module with permeation of silver nitrate Solution
Separation and Purification Technology, 2005Co-Authors: Masaaki Teramoto, Satoshi Shimizu, Hideto Matsuyama, Norifumi MatsumiyaAbstract:Abstract Novel hollow fiber facilitated transport membrane modules were used for ethylene/ethane separation using an aqueous silver nitrate Solution as a carrier Solution. In this membrane system, a feed gas consisting of 80 mol% C 2 H 4 and 20 mol% C 2 H 6 and an aqueous 4 M silver nitrate Solution are supplied to the lumen side (high pressure side, feed side) of a hollow fiber ultrafiltration membrane module and flow upward. In the lumen, the Solution absorbs C 2 H 4 selectively to become a rich or laden Solution. Some part of the rich Solution permeates the membrane to the permeate side (low pressure side, shell side) and other part of the Solution leaves the module from its top and then it is supplied to the top of the shell side, where the absorbed gas is stripped from the rich Solution and recovered as enriched ethylene. The Lean Solution is circulated to the lumen of the hollow fiber module by a pump. The feed side pressure was from 200 to 500 kPa and the permeate side pressure was atmospheric. Three modules with different liquid permeability and design were used in experiments. The module, in which the carrier Solution permeated the membrane at the upper part of the module, had higher performance than the module in which the Solution permeated at the lower part. The module, in which the Solution did not permeate the membrane, also had high performance although a large gas–liquid separator was needed downstream of the module. The module efficiency, which is defined as the ratio of the experimentally observed ethylene recovery to the recovery calculated by assuming gas–liquid phase equilibria at both sides of the membrane, was from 61 to almost 100%. Ethylene in the feed gas was concentrated from 80 to 99.8 mol%. The maximum C 2 H 4 permeance was 1.1 × 10 −4 mol m −2 s −1 kPa −1 (3.3 × 10 −4 cm 3 cm −2 s −1 cm Hg −1 ) and the selectivity of C 2 H 4 over C 2 H 6 was about 375 at the ethylene partial pressure of 164 kPa. The maximum ethylene recovery was 87% when the mean residence time of the feed gas in the module was 4.9 s. The membrane was confirmed to be stable during a series of experiments.
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separation and concentration of co2 by capillary type facilitated transport membrane module with permeation of carrier Solution
Journal of Membrane Science, 2004Co-Authors: Masaaki Teramoto, Satoshi Kitada, Nobuaki Ohnishi, Hideto Matsuyama, Norifumi MatsumiyaAbstract:A novel facilitated transport membrane module for gas separation is proposed in which a carrier Solution is forced to permeate the membrane. Both a feed gas and a carrier Solution are supplied to the lumen side (high-pressure side, feed side) of the capillary ultrafiltration membrane module and flow upward. Most of the carrier Solution which contains dissolved solute gas, CO2 in the present case, permeates the membrane to the permeate side (low-pressure side, shell side), where the Solution liberates dissolved gas to become a Lean Solution, and the Lean Solution is returned to the lumen of the capillary module by a pump. This type of capillary membrane module was applied to the separation of CO2 from model flue gases consisting of CO2 and N2 using various amines as carriers or absorbents of CO2. The feed side pressure was atmospheric and the permeate side pressure was controlled at 9–27 kPa. CO2 in the feed was successfully concentrated from 1.5–15 to 98.5–99.8 mol%. When the CO2 mole fraction in the feed was 0.1 and the mean residence time of gas in the module was 0.28 s, the CO2 permeance was 3.8×10−4 mol m−2 s−1 kPa−1 (1.1×10−3 cm3 cm−2 s−1 cmHg−1) and the CO2 recovery was 76%. The selectivity of CO2 over N2 was in the range from about 800 to 8000. The membrane was very stable over a discontinuous 4-month testing period. The energy consumption was found to be much smaller than those of conventional chemical absorption and membrane separation processes.
Kefa Cen - One of the best experts on this subject based on the ideXlab platform.
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CO2 chemical absorption by using membrane vacuum regeneration technology
Energy Procedia, 2009Co-Authors: Mengxiang Fang, Shuiping Yan, Zhongyang Luo, Kefa CenAbstract:Abstract The novel regeneration process by using membrane vacuum technology was put forward to reduce the regeneration energy consumption in the chemical absorption process for CO2 separation from flue gas. The rich MEA Solution was flowed in the lumen of the hydrophobic PP hollow fiber membrane contactors, and the shell side was maintained at a reduced pressure by a vacuum pump. In addition, the additional low temperature steam whose temperature is the same to rich MEA Solution was also provided to act as the sweep gas to improve the regeneration performance and to prevent the water loss of the Lean Solution. Results showed that this membrane vacuum regeneration process can regenerate rich MEA Solution to reach a relatively better regeneration performance and can effectively utilize the low temperature energy or waste heat in the power plants.
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Regeneration of CO2 from CO2-rich alkanolamines Solution by using reduced thickness and vacuum technology: Regeneration feasibility and characteristic of thin-layer solvent
Chemical Engineering and Processing: Process Intensification, 2009Co-Authors: Shuiping Yan, Mengxiang Fang, Zhongyang Luo, Kefa CenAbstract:Abstract The novel regeneration concept by using reduced thickness and vacuum technology was put forward in this paper to solve the higher regeneration energy consumption in the chemical absorption process for CO 2 separation from flue gas. A 120-mm I.D. vessel was precisely designed to regenerate the CO 2 -rich Solution, and the change of the thickness of thin-layer Solutions was simulated by controlling the volume of rich Solution added into the vessel. The experimental results show that vacuum regeneration may be viable if the CO 2 -rich Solution can be easily partitioned into the continuous single thin-layer Solutions with an appropriate thickness. The great decrease of thin-layer Solution thickness and regeneration pressure, and the increase of liquid temperature can improve the regeneration performance considerably. In addition, it is worthy to determine the optimum initial CO 2 loading of rich Solution, regeneration time and absorbent concentration due to the contradiction between the CO 2 loading of Lean Solution and regeneration energy consumption per kg of CO 2 . Finally, the simple comparison between vacuum and heating regeneration methods shows that the novel regeneration method may have the potential to reduce the regeneration energy requirement.