Investigation of CO2 Absorption Rate in Gas/Liquid Membrane Contactors with Inserting 3D Printing Mini-Channel Turbulence Promoters

The CO2 absorption by Monoethanolamine (MEA) solutions as chemical absorption was conducted in the membrane gas absorption module with inserting 3D mini-channel turbulence promoters of the present work. A mathematical modeling of CO2 absorption flux was analyzed by using the chemical absorption theory based on mass-transfer resistances in series. The membrane absorption module with embedding 3D mini-channel turbulence promoters in the current study indicated that the CO2 absorption rate improvement is achieved due to the diminishing concentration polarization effect nearby the membrane surfaces. A simplified regression equation of the average Sherwood number was correlated to express the enhanced mass-transfer coefficient of the CO2 absorption. The experimental results and theoretical predictions showed that the absorption flux improvement was significantly improved with implementing 3D mini-channel turbulence promoters. The experimental results of CO2 absorption fluxes were performed in good agreement with the theoretical predictions in aqueous MEA solutions. A further absorption flux enhancement up to 30.56% was accomplished as compared to the results in the previous work, which the module was inserted the promoter without mini channels. The influences of the MEA absorbent flow rates and inlet CO2 concentrations on the absorption flux and absorption flux improvement are also illustrated under both concurrent- and countercurrent-flow operations.


Introduction
The absorption rate of conventional contactors with chemical absorbents is restricted because the operational limitations of liquid channeling, flooding, entrainment, and foaming [1], which was overcome by membrane contactors with combining techniques of conventional separation technology and the presence of the membrane.The membrane contactors are membrane-based separation processes [2] such as membrane extraction [3], membrane absorption [4], ion exchange membrane [5] and membrane distillation [6] offers the advantageous features of low energy consumption, large and stable gas-liquid contact area, continuous operations, modulation arrangement and easy up-scaling [7].Membrane absorption is one of the membrane contactors applied to the undesirable gas removal such as CO 2 and H 2 S from the gas mixture for reducing greenhouse gas emission in industrial processes.The CO 2 absorption in conventional contactors with chemical absorbents is promoted and studied widely in the decade years [8] by several technologies namely membrane absorption [9], membrane adsorption [10] and membrane processes [11] as a promising technology with a higher absorption efficiency.The advantage of a higher specific area would be beneficial to absorption efficiency at the expense in the membrane contactor of an additional mass transfer resistance due to the membrane's presence [12].Membrane absorption is the one that the non-wetted microporous hydrophobic membrane serves as a barrier separating CO 2 gas feed stream and absorbent stream; the gas/liquid interface was formed at the membrane pore mouth in the gas feed stream.Moreover, Monoethanolamine (MEA) as an amine absorbent [13] has been used at high pressures [14] in the alkanolamine-based CO 2 membrane absorption process.Both chemical reaction and physical absorption occur simultaneously due to gas diffusing through the membrane into the liquid phase [15,16], as confirmed by the previous study [17] according to the diffusion-reaction model [18,19].In addition, the selective membrane materials [20] were durable and reusable [21,22] as well as the properties of absorbents [23] that examined the device performance of a successful process intensification for CO 2 absorption processes.Comprehensive understanding of the mass transfer mechanism of the CO 2 absorption rate [24] was developed with Knudsen-molecular diffusion of the dusty gas model [25] to estimate the mass flux [26,27] transporting through the membrane.
The mass-transfer boundary layers adjacent to the membrane surface results in the reduction of the concentration driving-force gradient as well as the absorption flux.The concentration polarization effect [28] plays an important role in deteriorating the concentration gradient, which leads to the decrement of transmembrane flux in the membrane contactor module, and thus the absorption rate is decreased [29].Several aspects of influencing the concentration polarization effect were assessed such as the hydrodynamic conditions and feed concentration.The absorption efficiency was augmented by inserting turbulence promoters such as spacer filaments [30] and carbon-fiber spacers [31] to diminish the concentration polarization effect, which come out with a higher convective mass-transfer coefficient due to increasing the turbulence intensity [32].An effective strategy was investigated to capture CO 2 in turbulent flow patterns [33] instead of operating a laminar flow velocity of absorbent feed stream.Turbulence intensity could be enhanced near the membrane surface with the use of eddy promoters to disrupt the mass-transfer boundary layer as well as the concentration polarization reduction.The magnitude of the concentration polarization coefficient γ m is an indicator to evaluate the device performance of the membrane absorption module.The larger the value of γ m that is obtained, the higher the mass transfer flux of CO 2 transports from the gas side to the absorbent feed stream.Moreover, an alternative configuration of reducing the turbulent boundary layer region [34] was proposed by using carbon-fiber spacers [35] into the flowing channel with avoiding overly exceptional power consumption.A higher CO 2 absorption rate enhancement at the expense of power consumption due to destroying the viscous laminar sublayer adjacent to the membrane interface was taken into account the economic consideration.A new design proposed the membrane absorption module with embedding 3D mini-channel turbulence promoters in the MEA feed channel to improve a higher CO 2 absorption efficiency in the present study.
Various amines and mixed amines [13] were used widely in chemical absorption technology for many decades to enhance the CO 2 capture rate and to attain regeneration cost down [36] as well.The one-dimensional modeling of mass-balance and chemical reaction equations was successfully developed and formulated with occurring reaction mechanisms of CO 2 absorption [37].MEA absorbents [38] were used to improve the CO 2 absorption flux in the hydrophobic microporous membrane contactor system [37].This paper examines the effects of an increasing shear rate to disturb the concentration boundary layer by implementing 3D mini-channel turbulence promoters in flat-plate membrane contactors, and to perform theoretical predictions and experimental results of the CO 2 absorption flux in parallel-plate gas/liquid PTFE/PP (polytetrafluoroethylene/polypropylene) membrane contactors with the use of MEA as an absorbent.The 3D printing technology presents a higher flexibility [39] in precisely tailoring and fabricating various complex 3D geometric shapes of turbulence promoters [40] to develop various hydrodynamic conditions.Membrane filaments were commonly employed in membrane separation modules to create eddy currents and flow disruption, which lead to the diminished concentration polarization effect and enhanced permeate flux.The influences of turbulence intensity amplification were accomplished by embedding 3D printing mini-channel turbulence promoters in the MEA feed stream, which were incorporated and regressed into the dimensionless quantities called mass-transfer enhancement factors under both cocurrent-flow and countercurrent-flow operations, respectively.
Microscale devices are a promising area of process intensification that could generate both technological and economic benefits [41].The turbulence intensity of laminar flows is increased when the fluid flows forward in the mini-channel, thereby improving the mass transfer rate of the synergy between velocity field and concentration field [42].Meanwhile, the ratio of the modified Sherwood number of turbulent flow to the Sherwood number under laminar flow was correlated in terms of various parameters such as geometric shapes of turbulence promoters, flow configurations, operation types, inlet concentrations and MEA feed flow rates.The new design achieves a considerable CO 2 absorption flux enhancement by embedding 3D printing mini-channel turbulence promoters in the MEA feed channel as compared to conducting the module with using an empty channel.Moreover, the CO 2 absorption flux improvement associated with a higher Sherwood number and the trade-off of power consumption increment was also delineated by considering the economic sense on both module designs and system operations.Actually, this study extends the previous study [43] to the membrane absorption module instead of inserting mini-channel turbulence promoters in obtaining a higher absorption efficiency and absorption flux improvement.The purpose of the present study is to discuss the effects of the geometric shapes of turbulence promoters, array configurations, flow patterns, inlet CO 2 concentrations and MEA feed flow rates on the device performance in a flat-plate membrane absorption module with inserting mini-channel turbulence promoters.

Experimental Setup
The fabrication structure of a flat-plate membrane contactor module for CO 2 absorption by the MEA absorbent with implementing 3D mini-channel turbulence promoter is illustrated in Figure 1 with flow paths indicated in red and blue dash lines and arrows.The printing material of turbulence promoters was made with polyester elastomer and stuck onto the hydrophobic membrane surface.The average molecular weight of the polyester elastomer (Polylactic Acid, PLA) ranges between 1000 and 60,000 with density of 1180 kg/m 3 .Two shapes of turbulence promoters were fabricated with 1 mm height by a 3D printer (ATOM 2.5EX, Hsinchu County, Taiwan), say Circle and Dimond types, and inserted in the flowing channel for conducting experiments.The detail of the 3D printing protocol of the fabricated turbulence promoters of two geometric shapes with dimensions, say Circle and Diamond shapes, and cross-sectional views of various sectors were embedded into MEA absorbent flow channel, as shown in Figures 2 and 3, respectively.The Circle type was made of a diameter of 30.00 mm and the Diamond type was made of 28.61 mm with each length, which the printing promoter icon hindering permeate passages and deteriorating gas permeate flux due to turbulence promoter coverage of the membrane surface area.Two array configurations were arranged, say Type A and Type B, as shown in F 4. The 3D printing technology presents a higher flexibility in designing various com geometric shapes of turbulence promoters in precisely tailoring through a layer-bymachining process by a 3D printer (ATOM 2.5EX, Mastech Machine Co., Ltd., New T Two array configurations were arranged, say Type A and Type B, as shown in Figure 4.The 3D printing technology presents a higher flexibility in designing various complex geometric shapes of turbulence promoters in precisely tailoring through a layer-by-layer machining process by a 3D printer (ATOM 2.5EX, Mastech Machine Co., Ltd., New Taipei, Taiwan).Those turbulence promoters were manufactured and submerged into the MEA solution with a total durability test time of 48 h to ensure that they are resistant and stable to corrosion before conducting the experiments runs.Meanwhile, about 13% occupation of the printing turbulence promoter icons on the membrane surface was counted the effective permeate flux area in the calculation procedure due to blocking permeate flux through the membrane.The flat-plate membrane contactor module contains two flow channels with embedding 3D mini-channel turbulence promoters onto the MEA absorbent feed stream, and the other empty channel for CO 2 /N 2 gas mixture with winding nylon fiber of 0.2 mm diameter upon the hydrophobic membrane surface as a supporting material to prevent from vibration and wrinkling.Two 1 mm-thick silicon rubbers were sealed between the hydrophobic composite membrane and the acrylic plate for both absorbent and gas feed sides, respectively, to build up flow channels and to prevent leakage.The 3D printing turbulence promoters of 1 mm-thick were fabricated the mini-channel flow path and glued with Cyanoacrylate Adhesive (Chang Chun Plastics Co., Ltd., Taipei, Taiwan) on the acrylic plate of the MEA absorbent feed side in contact with the hydrophobic membrane surface to create the eddy motion around those impediments.A parallel conduit (L = 0.21 m, W = 0.29 m, H = 2.0 mm) to conduct two flow channels separated by inserting a hydrophobic composite membrane made of PTFE/PP (ADVANTEC) as the permeating medium with a nominal pore size of 0.2 µm, a porosity of 0.72, and a total thickness of 130 µm (PTFE 98 µm and PP 32 µm).The experiments were conducted for controlling various 30 wt% MEA (5.0 × 10 3 mol/m 3 ) MEA absorbent feed flow rates (5.0, 6.67, 8.33, 10.0 cm 3 /s) regulated by a flow meter (MB15GH-4-1, Fong-Jei, New Taipei, Taiwan) as the liquid absorbent pumping from a reservoir.Meanwhile, a gas mixture containing CO 2/ N 2 was pumped from the gas mixing tank (EW-06065-02, Cole Parmer Company, Vernon Hills, IL, USA) by using the mass flow controller (N12031501PC-540, Protec, Brooks Instrument, Hatfield, PA, USA) at 5 cm 3/ s with various CO 2 concentrations of 30%, 35% and 40%, respectively.The schematic detailed configuration of flat-plate membrane contactor modules for CO 2 absorption by MEA absorbent are illustrated in Figure 5 under both cocurrent-and countercurrent-flow operations.A photo of the operating experimental setup of a flat-plate gas membrane absor system is shown in Figure 6 with acrylic plates as outside walls.Comparisons were of CO2 absorption flux under various operation conditions between the flat-plate m brane contactor modules with/without inserting 3D printing mini-channel turbu promoters.The outlet CO2 sample was collected and injected into the column heatin A photo of the operating experimental setup of a flat-plate gas membrane absorption system is shown in Figure 6 with acrylic plates as outside walls.Comparisons were made of CO 2 absorption flux under various operation conditions between the flat-plate membrane contactor modules with/without inserting 3D printing mini-channel turbulence promoters.The outlet CO 2 sample was collected and injected into the column heating systems for rapid heating of the sample-collection capillary tube, which was measured by using the gas chromatography with helium as a carrier gas (Model HY 3000, China Chromatograph Co., Ltd., Xinzhuang, New Taipei, Taiwan) to analyze the CO 2 concentrations including conventional thermal conductivity detector (TCD) devices.

Concentration Polarization
The concentration at the membrane surface affecting the CO2 concentration drivingforce gradient across the membrane, consequently influencing the absorption flux.A mass-transfer behavior analysis is studied to describe the concentration gradient between both membrane surfaces of CO2/N2 gas feed side and MEA absorbent feed side.A representation of the mass-transfer behavior in the membrane gas/liquid contactor module is depicted in Figure 7a,b of macroscopic description and microscopic descriptions, respectively.
(a) Macroscopic description of CO2 concentration variations

Concentration Polarization
The concentration at the membrane surface affecting the CO 2 concentration drivingforce gradient across the membrane, consequently influencing the absorption flux.A masstransfer behavior analysis is studied to describe the concentration gradient between both membrane surfaces of CO 2 /N 2 gas feed side and MEA absorbent feed side.A representation of the mass-transfer behavior in the membrane gas/liquid contactor module is depicted in Figure 7a,b of macroscopic description and microscopic descriptions, respectively.

Concentration Polarization
The concentration at the membrane surface affecting the CO2 concentration drivingforce gradient across the membrane, consequently influencing the absorption flux.A mass-transfer behavior analysis is studied to describe the concentration gradient between both membrane surfaces of CO2/N2 gas feed side and MEA absorbent feed side.A representation of the mass-transfer behavior in the membrane gas/liquid contactor module is depicted in Figure 7a    ( ) and  ( ) indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure 7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1): Hc (1) Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences ( −  ) [44] and membrane permeation coefficient ( ) [45] according to dusty gas model [17], in which,  is the overall mass transfer coefficient of membrane, the CO2 concentration on the membrane/liquid interface by using the dimensionless Henry's law constant  =  / = 0.73 [37].The reduced C 1(g) and C 2(g) indicate the membrane surface concentrations of the CO 2 /N 2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure 7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.
Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1):   1() and  2() indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure 7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.
Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1): Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient (  ) [45] according to dusty gas model [17], in which,   is the overall mass transfer coefficient of membrane, the CO2 concentration on the membrane/liquid interface by using the dimensionless Henry's law constant   =  2 / 1 = 0.73 [37].The reduced   1() and  2() indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure 7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1): Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient (  ) [45] according to dusty gas model [17], in which,   is the overall mass transfer coefficient of membrane, the CO2 concentration on the membrane/liquid interface by using the dimensionless Henry's law constant   =  2 / 1 = 0.73 [37].The reduced Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO 2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO 2 /N 2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows:  stream and MEA absorbent feed stream, respectively, as seen from Figure 7b.The tration differences between both streams near the membrane surfaces and thos bulk stream are used to estimate the temperature polarization coefficient.Concentration polarization is enumerated by the ratio of the concentration di across the membrane to the concentration difference of both bulk streams, as is ca concentration polarization coefficient is Equation (1): Declining concentration gradients between the bulk streams and membrane s as seen in Figure 7b, results in decreasing the mass-transfer driving force, and t CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption pro curs within three regions according to the schematic diagram of the membrane ga contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophob brane and (iii) the MEA absorbent feed stream.The influence of the absorptio dominated by the concentration difference for each mass transfer region, which represented in Equations ( 2)-( 4) under the steady-state operation as follows: Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO 2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences (P 1 − P 2 ) [44] and membrane permeation coefficient (c m ) [45] according to dusty gas model [17], in which, K m is the overall mass transfer coefficient of membrane, the CO 2 concentration on the membrane/liquid interface by using the dimensionless Henry's law constant H C = C 2 /C 1 = 0.73 [37].The reduced equilibrium constant at T = 298 K [45] and the membrane permeation coefficient [46] with the tortuosity τ = 1/ε [47] were determined as follows: Flux permeating through the CO 2 /N 2 stream, the microporous hydrophobic membrane and the MEA stream for the modules with/without embedding 3D mini-channel turbulence promoters is shown in Figure 8. Equating the amount of mass flux by the conservation law among three regions, one may obtain the following:  1() and  2() indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure 7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.
Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1): Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient (  ) [45] according to dusty gas model [17], in which,   is the overall mass transfer coefficient of membrane, the CO2 concentration on the membrane/liquid interface by using the dimensionless Henry's law constant   =  2 / 1 = 0.73 [37].The reduced i = promoter, empty Membranes 2023, 13, x FOR PEER REVIEW 10 of 25 equilibrium constant at  = 298 K [45] and the membrane permeation coefficient [46] with the tortuosity  = 1/ [47] were determined as follows: ′ =  MEA /  ,  = MEACOO  / CO MEA = 1.25 × 10 (5) Flux permeating through the CO2/N2 stream, the microporous hydrophobic membrane and the MEA stream for the modules with/without embedding 3D mini-channel turbulence promoters is shown in Figure 8. Equating the amount of mass flux by the conservation law among three regions, one may obtain the following:

Concentration Distributions
Balances of mass flux due to mass diffusion and chemical reaction by the mass conservation were formulated simultaneously.The steady-state isothermal diffusion-reaction process in the gas/liquid membrane contactor module causes the trans-membrane mass flux of CO 2 and were formulated by balancing mass flux conservation presented in a finite control element under concurrent-flow and countercurrent-flow operations in Figure 9a,b, respectively.
Membranes 2023, 13, x FOR PEER REVIEW 10 of 25 equilibrium constant at  = 298 K [45] and the membrane permeation coefficient [46] with the tortuosity  = 1/ [47] were determined as follows: ′ =  MEA /  ,  = MEACOO  / CO MEA = 1.25 × 10 (5) Flux permeating through the CO2/N2 stream, the microporous hydrophobic membrane and the MEA stream for the modules with/without embedding 3D mini-channel turbulence promoters is shown in Figure 8. Equating the amount of mass flux by the conservation law among three regions, one may obtain the following:

Concentration Distributions
, cocurrent-flow operation ( 8) , countercurrent-flow operation (9) 1() and  2() indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure 7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.
Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1): Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient (  ) [45] according to dusty gas model [17], in which,   is the overall mass transfer coefficient of membrane, the CO2 concentration on the membrane/liquid interface by using the dimensionless Henry's law constant , cocurrent-flow operation (8)   1() and  2() indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure 7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.
Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1): Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient (  ) [45] according to dusty gas model [17], in which,   is the overall mass transfer coefficient of membrane, the CO2 concentration on the membrane/liquid interface by using the dimensionless Henry's law constant   =  2 / 1 = 0.73 [37].The reduced , countercurrent-flow operation ( 9) in which z is the coordinate along with the flowing direction (positive direction), and the concentration polarization coefficient γ m was derived and obtained by equating Equations ( 2) and (4) (J m = J g ) and Equations ( 3) and (4) (J m = J ), respectively, as follows: Then, a simplified form of γ m expressed in terms of the mass-transfer coefficient as (b) Microscopic description of CO2 concentration variations  1() and  2() indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure 7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.
Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1): Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient (  ) [45] according to dusty gas model [17], in which,   is the overall mass transfer coefficient of membrane, the CO2 concentration on the membrane/liquid interface by using the dimensionless Henry's law constant   =  2 / 1 = 0.73 [37].The reduced   1() and  2() indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure 7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.
Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1): Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient (  ) [45] according to dusty gas model [17], in which,   is the overall mass transfer coefficient of membrane, the CO2 concentration on the membrane/liquid interface by using the dimensionless Henry's law constant   =  2 / 1 = 0.73 [37].The reduced The procedure for calculating theoretical predictions of the mass transfer coefficient was performed using continuous iterating C 1(g) and C 2(g) from Equations ( 11) and (12) within the convergence tolerance.The calculated convective mass-transfer coefficients were delivered to obtain the concentration distributions of both the CO 2 /N 2 gas feed stream and the MEA absorbent feed stream by solving two simultaneous ordinary differential equations of Equations ( 8) and (10) for cocurrent-flow operation (or Equations ( 9) and (10) for countercurrent-flow operation) by marching the fourth-order Runge-Kutta method along the flow direction, as shown in Figure 9.

Mass-Transfer Rate Enhancement
The 3D printing mini-channel turbulence promoters are inserted in the conduit of the MEA feed stream instead of using the module of empty channel (without embedding turbulence promoters).The enhancement factor α E depending on the geometric shapes and array configurations was regressed to calculate the enhanced convective mass-transfer coefficients in gas/liquid membrane contactor modules with inserting the 3D printing mini-channel turbulence promoters [33] as follows: where D h,promoter and D h,empty are the equivalent diameters of modules with embedding 3D mini-channel turbulence promoters and the empty channel in the MEA absorbent feed stream, respectively.The equivalent diameters of modules with embedding 3D turbulence promoters D h,promoter was calctlated by the wetted area A and wetted perimeter P, say 4A/P, as shown in Figure 10.In which, W 1 is the average width of the promoter, W 2 is the punched hole diameter designed by one-third promoter diameter, and W 3 is the the average width of the punched hole inside the promoter.Meanwhile, the average diameters of mini-channel turbulence promoters were estimated by averaging various sections of both Circle and Diamond shapes, as shown in Figure 11.
promoters  , was calctlated by the wetted area  and wetted perimeter , say 4/, as shown in Figure 10.In which,  is the average width of the promoter,  is the punched hole diameter designed by one-third promoter diameter, and  is the the average width of the punched hole inside the promoter.Meanwhile, the average diameters of mini-channel turbulence promoters were estimated by averaging various sections of both Circle and Diamond shapes, as shown in Figure 11.stream, respectively.The equivalent diameters of modules with embedding 3D turbulence promoters  , was calctlated by the wetted area  and wetted perimeter , say 4/, as shown in Figure 10.In which,  is the average width of the promoter,  is the punched hole diameter designed by one-third promoter diameter, and  is the the average width of the punched hole inside the promoter.Meanwhile, the average diameters of mini-channel turbulence promoters were estimated by averaging various sections of both Circle and Diamond shapes, as shown in Figure 11.

Flux Improvement by Inserting Min-Channel Turbulence Promoters in Membrane Modules
The morphology and water contact angle of the PTFE/PP membranes were characterized by using Scanning Electron Microscopic (SEM, Zeiss sigma 300, Jena, Germany) and Contact angle system (First Ten Angstrom FTA-125, Portsmouth, NH, USA). Figure 12 shows the morphology of the fresh and used membranes of experimental runs.The SEM images were completed by applying a beam of high-energy electrons, which indicated that the presence of the 3D printing mini-channel turbulence promoter of no fouling or scaling in conducting experimental runs.Moreover, the hydrophobic membrane surface wettability can be portrayed with water contact measurements by establishing the tangent (angle) of a liquid drop on a solid surface at the base, which is defined by the mechanical equilibrium of the liquid drop under the action of three interfacial tensions.The water contact angles of the hydrophobic composite membrane made of PTFE/PP were shown in Figure 13.The PTFE/PP membranes presented different surface wettability in the range of 128-132 • (water contact angle of 130.3 ± 2.0 • ) with the confirmation of the surface hydrophobicity of the hydrophobic membrane.
face wettability can be portrayed with water contact measurements by establishing the tangent (angle) of a liquid drop on a solid surface at the base, which is defined by the mechanical equilibrium of the liquid drop under the action of three interfacial tensions.The water contact angles of the hydrophobic composite membrane made of PTFE/PP were shown in Figure 13.The PTFE/PP membranes presented different surface wettability in the range of 128-132° (water contact angle of 130.3 ± 2.0°) with the confirmation of the surface hydrophobicity of the hydrophobic membrane.The absorption flux is dependent on the concentration gradients between both membrane surfaces in the gas/liquid membrane contactor modules.The modules with inserting mini-channel turbulence promoters of various geometric shapes and array configurations to diminish concentration polarization effect due to reducing of the mass-transfer boundary-layer thickness.The absorption flux improvement with respect to the MEA feed flow rates and inlet feed CO2 concentrations are more substantial in concurrent-flow operations than those in countercurrent-flow operations regarding to the effects of the geometric shapes, array configurations and flow patterns with embedding mini-channel turbulence promoters.The accuracy deviation [48] was calculated between the experimental results and theoretical predictions as follows: The absorption flux is dependent on the concentration gradients between both membrane surfaces in the gas/liquid membrane contactor modules.The modules with inserting mini-channel turbulence promoters of various geometric shapes and array configurations to diminish concentration polarization effect due to reducing of the mass-transfer boundarylayer thickness.The absorption flux improvement with respect to the MEA feed flow rates and inlet feed CO 2 concentrations are more substantial in concurrent-flow operations than those in countercurrent-flow operations regarding to the effects of the geometric shapes, array configurations and flow patterns with embedding mini-channel turbulence promoters.The accuracy deviation [48] was calculated between the experimental results and theoretical predictions as follows: Moffat [48] determined the experimental uncertainty for each individual measurement from the experimental runs as follows: The mean value of the resulting uncertainty of the experimental measurements was defined by where N exp , J exp,i and J theo,i are the number of experimental data, theoretical predictions and experimental results of absorption fluxes, respectively.The accuracy deviations and mean uncertainty were calculated within 3.2 × 10 −3 ≤ Er ≤ 5.23 × 10 −2 and 5.21 × 10 −3 ≤ S J exp ≤ 8.32 × 10 −3 for both cocurrent-and countercurrent-flow operations.
The good agreement was expected between the theoretical predictions and experimental results.Implementing 3D printing mini-channel turbulence promoters with two geometric shapes of Circle and Diamond and two array configurations produces the augmented turbulence intensity, which results in the higher absorption flux under both cocurrentand countercurrent-flow operations.The mass transfer coefficients of the module with inserting mini-channel turbulence promoters in the flow channel can be incorporated into the correlated Sherwood number, as referred to Equation ( 14), and determined by using Buckingham's π theorem for cocurrent-and countercurrent-flow operations, respectively, as presented in Equations ( 18) and (19) as well as in Figure 14a,b.Embedding turbulence promoters plays a significant role in inducing a higher turbulence intensity to disrupt the mass-transfer boundary layer as well as to reduce masstransfer resistance, which comes out the absorption flux improvement.The correlated Sherwood numbers indicate that the mass transfer coefficient of the module with embedding mini-channel Diamond turbulence promoters achieves a higher value than those of the modules using the empty channel and embedding Circle turbulence promoters, as shown in Figure 14a,b.The results showed that the module with inserting mini-channel Diamond turbulence promoters into flow channels boosts more intensive vortices and eddies due to a non-smooth curvature shape of obstacles than those in the module with inserting Circle turbulence promoters.Moreover, the correlated Sherwood numbers in countercurrent-flow operations are higher than those in cocurrent-flow operations.Good agreement was obtained in comparisons of both theoretical predictions and experimental results of the modules with embedding 3D printing mini-channel turbulence promoters, as demonstrated in Figure 15.The results showed that the CO 2 absorption flux for the module with inserting 3D printing mini-channel turbulence promoter with both geometric shapes of Circle and Diamond turbulence promoters in both cocurrent-and countercurrent-flow operations, produces a larger turbulence intensity, and thus yields the higher mass transfer flux.Moreover, the CO 2 permeates flux through the hydrophobic membrane in the module by embedding turbulence promoters and is more considerable in countercurrent-flow operations than that in concurrent-flow operations.
countercurrent-flow operations.The mass transfer coefficients of the module with inserting mini-channel turbulence promoters in the flow channel can be incorporated into the correlated Sherwood number, as referred to Equation ( 14), and determined by using Buckingham's  theorem for cocurrent-and countercurrent-flow operations, respectively, as presented in Equations ( 18) and ( 19) as well as in Figure 14a,b.

2.245
Re 0.351 Cocurrent-flow operations ( 18)  Embedding turbulence promoters plays a significant role in inducing a higher turbulence intensity to disrupt the mass-transfer boundary layer as well as to reduce masstransfer resistance, which comes out the absorption flux improvement.The correlated Sherwood numbers indicate that the mass transfer coefficient of the module with embedding mini-channel Diamond turbulence promoters achieves a higher value than those of the modules using the empty channel and embedding Circle turbulence promoters, as shown in Figure 14a,b.The results showed that the module with inserting mini-channel Diamond turbulence promoters into flow channels boosts more intensive vortices and eddies due to a non-smooth curvature shape of obstacles than those in the module with inserting Circle turbulence promoters.Moreover, the correlated Sherwood numbers in countercurrent-flow operations are higher than those in cocurrent-flow operations.Good agreement was obtained in comparisons of both theoretical predictions and experimental results of the modules with embedding 3D printing mini-channel turbulence promoters, as demonstrated in Figure 15.The results showed that the CO2 absorption flux for the module with inserting 3D printing mini-channel turbulence promoter with both  The CO2 absorption flux in the module with embedding 3D printing mini-channel turbulence promoters were presented graphically with the Reynolds number of the MEA feed rate, geometric shape, array configuration and flow pattern as parameters, as delineated in Figures 16-19  The CO 2 absorption flux in the module with embedding 3D printing mini-channel turbulence promoters were presented graphically with the Reynolds number of the MEA feed rate, geometric shape, array configuration and flow pattern as parameters, as delineated in Figures 16-19

Absorption Flux Improvement and Further Absorption Flux Enhancement
The present work extends the previous study except for embedding 3D printing mini-channel turbulence promoters instead of inserting turbulence promoters without fabricating mini-channels [43] for both concurrent-and countercurrent-flow operations, as shown in Figure 20.The present study illustrates why the present design of fabricating 3D mini-channel turbulence promoters is preferred regarding technical feasibility and comes out with a considerably larger absorption flux than that in our previous work [43].

Absorption Flux Improvement and Further Absorption Flux Enhancement
The present work extends the previous study except for embedding 3D printing mini-channel turbulence promoters instead of inserting turbulence promoters without fabricating mini-channels [43] for both concurrent-and countercurrent-flow operations, as shown in Figure 20.The present study illustrates why the present design of fabricating 3D mini-channel turbulence promoters is preferred regarding technical feasibility and comes out with a considerably larger absorption flux than that in our previous work [43].
Restated, a relative permeated flux improvement, say I E , was evaluated by the percentage increase in the device with inserting 3D turbulence promoters, based on the device of the empty channel (wound with nylon fiber) under countercurrent-flow operations as an illustration, which are two kinds of turbulence promoters with inserting mini-channels (the present device) and without inserting mini-channels (the module used in Ref. [43]), respectively.

Absorption Flux Improvement and Further Absorption Flux Enhancement
The present work extends the previous study except for embedding 3D printing mini-channel turbulence promoters instead of inserting turbulence promoters without fabricating mini-channels [43] for both concurrent-and countercurrent-flow operations, as shown in Figure 20.The present study illustrates why the present design of fabricating 3D mini-channel turbulence promoters is preferred regarding technical feasibility and comes out with a considerably larger absorption flux than that in our previous work [43].Restated, a relative permeated flux improvement, say  , was evaluated by the percentage increase in the device with inserting 3D turbulence promoters, based on the device of the empty channel (wound with nylon fiber) under countercurrent-flow operations as an illustration, which are two kinds of turbulence promoters with inserting mini-channels (the present device) and without inserting mini-channels (the module used in Ref. [43]), respectively.
I CT E,MC (%) = J CT E,MC −J CO empty J CO empty × 100, Module with mini-channel in countercurrent flow (22) where I CT E,p and I CT E,MC are the absorption flux improvement in the module of Ref. [43] and the module with embedding 3D printing mini-channel turbulence promoters for countercurrent-flow operations, respectively.Meanwhile, the subscripts E and empty denote the modules with/without embedding 3D turbulence promoters, respectively, while MC means the module with the mini-channel, and the superscripts CO and CT denote concurrent-and countercurrent-flow operations, respectively.Generally, the permeated flux augmented by inserting 3D turbulence promoters is more significant in countercurrentflow operations than that in concurrent-flow operations.The further absorption flux enhancement E p of CO 2 absorption in membrane contactors by embedding 3D Circle turbulence promoters is calculated based on the device of the same working dimensions performed in the previous work [43] under countercurrent-flow operations as follows: where J CT E,p and J CT E,MC are the absorption flux in the module of Ref. [43] and the module with embedding 3D printing mini-channel turbulence promoters for countercurrent-flow operations, respectively.A percentage increment of absorption flux improvement and further absorption flux enhancement was evaluated for the module with embedding minichannel turbulence promoter, which was compared to the absorption flux in the module by embedding turbulence promoter without the mini-channel for Circle turbulence promoters under two array configurations, respectively, as seen from Table 1.The theoretical predictions show that the further absorption flux enhancement up to 30.56% is obtained with embedding Circle turbulence promoters of Type B array configurations, as demonstrated in Table 1.Generally, the further absorption flux enhancement of the module with embedding the mini-channel turbulence promoter decreases with the inlet feed CO 2 concentration and the MEA feed flow rate.Meanwhile, a larger further absorption flux enhancement in operating the Circle turbulence promoter under Type B array configurations is achieved as compared to Type A array configurations at the lower MEA feed flow rate.

Power Consumption Increment
The power consumption increment is necessitated due to the increased frictional loss by embedding mini-channel turbulence promoters in the MEA absorbent feed stream of the parallel-plate gas/liquid membrane contactor modules, which were determined by only the friction losses to walls by using Fanning friction factor f F [49]:   1() and  2() indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure 7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.
Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1): Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient (  ) [45] according to dusty gas model [17], in which,   is the overall mass transfer coefficient of membrane, the CO2 concentration on the membrane/liquid interface by using the dimensionless Henry's law constant   =  2 / 1 = 0.73 [37].The reduced   Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1): Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient (  ) [45] according to dusty gas model [17], in which,   is the overall mass transfer coefficient of membrane, the CO2 concentration on the membrane/liquid interface by using the dimensionless Henry's law constant   =  2 / 1 = 0.73 [37].The reduced   Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1): Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient (  ) [45] according to dusty gas model [17], in which,   is the overall mass transfer coefficient of membrane, the CO2 concentration on the membrane/liquid interface by using the dimensionless Henry's law constant  =  / = 0.73 [37].The reduced   Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1): Declining concentration gradients between the bulk streams and membrane surfaces, as seen in Figure 7b, results in decreasing the mass-transfer driving force, and thus, the CO2 absorption flux is reduced.Mass transfer in a membrane gas absorption process occurs within three regions according to the schematic diagram of the membrane gas/liquid contactor module: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic membrane and (iii) the MEA absorbent feed stream.The influence of the absorption flux is dominated by the concentration difference for each mass transfer region, which may be represented in Equations ( 2)-( 4) under the steady-state operation as follows: The mass flux of CO2 diffusing through the trans-membrane was evaluated using the saturation partial pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient in which the average velocity is calculated with the volumetric flow rate divided by the wetted area.The relative extents I H of the power consumption increment was illustrated based on the device of using the empty channel by calculating the percentage increment in the module with embedding 3D min-channel turbulence promoters as where the subscripts of promoter and empty represent the flow channels with and without embedding 3D printing mini-channel turbulence promoters, respectively.The efficacy of membrane turbulence promoters in terms of both desirable absorption flux improvement and the undesirable power consumption increment was assessed with an economic viewpoint for optimal operations, as referred to the ratio of I E /I H . Restated, utilizing turbulence promoters to diminish the concentration polarization effect could compensate the friction loss increment within a certain extent.Embedding 3D printing min-channel turbulence promoters in the MEA feed channel performed a better absorption flux improvement at the expense of a larger value of friction loss increment, which the effects on I E /I H with geometric shapes of turbulence promoters, inlet feed CO 2 concentrations, flow patterns and MEA flow rates as parameters are shown in Figure 21 with Type B array configuration as an illustration for the higher absorption flux improvement.

Conclusions
The designs of 3D printing min-channel turbulence promoters were applied to the membrane absorption module, which could swirl the flow stream so as to enhance the turbulence intensity in enhancing the mass transfer rate.The theoretical predictions and experimental results indicated that the device performance of embedding mini-channel turbulence promoters was boosted effectively owing to creating the secondary flow pattern and augmenting the turbulence intensity.The present study serves as a groundwork investigation of the important findings for utilizing min-channel turbulence promoters for MD application.The conclusions are drawn in this proof-of-design study as follows:

Conclusions
The designs of 3D printing min-channel turbulence promoters were applied to the membrane absorption module, which could swirl the flow stream so as to enhance the turbulence intensity in enhancing the mass transfer rate.The theoretical predictions and experimental results indicated that the device performance of embedding mini-channel turbulence promoters was boosted effectively owing to creating the secondary flow pattern and augmenting the turbulence intensity.The present study serves as a groundwork investigation of the important findings for utilizing min-channel turbulence promoters for MD application.The conclusions are drawn in this proof-of-design study as follows: (a) Operating MD module by embedding 3D printing mini-channel turbulence promoters with various geometric promoter-shapes and array configurations resulted in enhanced absorption flux performance in comparison with the module with using the empty channel due to generating vortexes and eddies.
(b) The theoretical predictions show that the further absorption flux enhancement up to 30.56% is obtained with embedding Circle mini-channel turbulence promoters of Type B array configurations as compared to that in the module without inserting mini-channel turbulence promoters.Meanwhile, the higher absorption flux improvement is obtained by embedding turbulence promoters of Type B configuration compared to Type A configuration.
(c) The improved absorption fluxes by embedding mini-channel turbulence promoters were augmented and represented with a simplified expression of the correlated Sherwood number.The correlated Sherwood numbers obtained in the module with embedding 3D mini-channel Diamond turbulence promoters achieved a higher value than those of the devices with the empty channel and embedding Circle turbulence promoters.Moreover, the correlated Sherwood numbers in the module under countercurrent-flow operations are higher than those in operating cocurrent-flow patterns.
(d) The power consumption increment was increased due to embedding the 3D minichannel turbulence promoter to cause a drop in fluid pressure.The economic viewpoint was examined in terms of the ratio of the absorption flux improvement to power the consumption increment, say I E /I P .The results indicated that the ratio I E /I P for Type B configuration is higher than that of Type A configuration.
The present study only explores two specific geometric shapes and two array configurations under the specific dimension designs.Embedding 3D printing min-channel turbulence promoters to the gas/liquid membrane absorption module with the use of MEA absorbent shows a great potential to considerably enhance the absorption flux.A new design in this study includes the advantage effect of reinforcing the turbulence intensity as an alternative tactic on the absorption flux in the membrane absorption module with embedding 3D mini-channel turbulence promoters.However, there still exists many more possibilities to other designs of mini-channel turbulence promoters in finding an optimal device performance with considering the economic viewpoint for membrane absorption processes. 2() indicate the membrane surface concentrations of the CO2/N2 gas feed absorbent feed stream, respectively, as seen from Figure 7b.The concences between both streams near the membrane surfaces and those of the used to estimate the temperature polarization coefficient.ion polarization is enumerated by the ratio of the concentration difference brane to the concentration difference of both bulk streams, as is called the olarization coefficient is Equation (1): H c (1) oncentration gradients between the bulk streams and membrane surfaces, re 7b, results in decreasing the mass-transfer driving force, and thus, the flux is reduced.Mass transfer in a membrane gas absorption process oce regions according to the schematic diagram of the membrane gas/liquid le: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic memthe MEA absorbent feed stream.The influence of the absorption flux is he concentration difference for each mass transfer region, which may be quations ( 2)-( 4) under the steady-state operation as follows: lux of CO2 diffusing through the trans-membrane was evaluated using the al pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient ing to dusty gas model [17], in which,   is the overall mass transfer cobrane, the CO2 concentration on the membrane/liquid interface by using less Henry's law constant   =  2 / 1 = 0.73 H c (1) ing concentration gradients between the bulk streams and membrane surfaces, igure 7b, results in decreasing the mass-transfer driving force, and thus, the tion flux is reduced.Mass transfer in a membrane gas absorption process octhree regions according to the schematic diagram of the membrane gas/liquid odule: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic mem-(iii) the MEA absorbent feed stream.The influence of the absorption flux is by the concentration difference for each mass transfer region, which may be in Equations ( 2)-( 4) under the steady-state operation as follows: J g =k a �C a(g) − C 1(g) � (2) ass flux of CO2 diffusing through the trans-membrane was evaluated using the artial pressure differences ( 1 −  2 ) [44] and membrane permeation coefficient cording to dusty gas model [17], in which,   is the overall mass transfer comembrane, the CO2 concentration on the membrane/liquid interface by using sionless Henry's law constant   =  2 / 1 = 0.73 s flux of CO2 diffusing through the trans-membrane was evaluated using the rtial pressure differences ( −  ) [44] and membrane permeation coefficient  H c (1) oncentration gradients between the bulk streams and membrane surfaces, re 7b, results in decreasing the mass-transfer driving force, and thus, the flux is reduced.Mass transfer in a membrane gas absorption process oce regions according to the schematic diagram of the membrane gas/liquid le: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic memthe MEA absorbent feed stream.The influence of the absorption flux is he concentration difference for each mass transfer region, which may be quations ( 2)-( 4) under the steady-state operation as follows: MEA feed side out At the outlet promoter Channel embedding 3D mini-channel turbulence promoters theo Theoretical predictions

Figure 1 .Figure 1 .
Figure 1.Fabrication structure of components in a flat-plate membrane contactor module.Figure 1. Fabrication structure of components in a flat-plate membrane contactor module.

Figure 1 .
Figure 1.Fabrication structure of components in a flat-plate membrane contactor module.

Figure 2 .
Figure 2. Front view of two shapes of 3D mini-channel turbulence promoters.Figure 2. Front view of two shapes of 3D mini-channel turbulence promoters.

Figure 2 . 5 Figure 3 .
Figure 2. Front view of two shapes of 3D mini-channel turbulence promoters.Figure 2. Front view of two shapes of 3D mini-channel turbulence promoters.Membranes 2023, 13, x FOR PEER REVIEW 5

Figure 3 .
Figure 3. Cross-sectional views of various sectors of 3D mini-channel turbulence promoters.

Membranes 2023 ,
13, x FOR PEER REVIEW 6 of 25(a) Circle shape (Type A) (b) Circle shape (Type B) (c) Diamond shape (Type A) (d) Diamond shape (Type B)

Figure 4 .
Figure 4. Photos of two shapes and two configurations of 3D mini-channel turbulence promoters.

Membranes 2023 , 25 Figure 6 .
Figure 6.A photo of an experimental apparatus of a flat-plate gas membrane absorption system.

Figure 6 .
Figure 6.A photo of an experimental apparatus of a flat-plate gas membrane absorption system.

Membranes 2023 , 25 Figure 6 .
Figure 6.A photo of an experimental apparatus of a flat-plate gas membrane absorption system.

Membranes 2023 ,
13, x FOR PEER REVIEW 9 of 25 (b) Microscopic description of CO2 concentration variations

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.

Membranes 2023 ,
13, x FOR PEER REVIEW 9 of 25 (b) Microscopic description of CO2 concentration variations

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.
Membranes 2023, 13, x FOR PEER REVIEW 9 of 25 (b) Microscopic description of CO2 concentration variations

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.

Membranes 2023 ,
13, x FOR PEER REVIEW (b) Microscopic description of CO2 concentration variations

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane con  1() and  2() indicate the membrane surface concentrations of the CO2/N2

3, 13 ,
x FOR PEER REVIEW 9 of 25 (b) Microscopic description of CO2 concentration variations

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.1() and  2() indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.Concentration polarization is enumerated by the ratio of the concentration difference across the membrane to the concentration difference of both bulk streams, as is called the concentration polarization coefficient is Equation (1):

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.

Figure 8 .
Figure 8. Schematic mass transfer resistances for three mass transfer regions of membrane contactor.
Balances of mass flux due to mass diffusion and chemical reaction by the mass conservation were formulated simultaneously.The steady-state isothermal diffusion-reaction process in the gas/liquid membrane contactor module causes the trans-membrane mass flux of CO2 and were formulated by balancing mass flux conservation presented in a finite control element under concurrent-flow and countercurrent-flow operations in Figure 9a,b, respectively.(a) Cocurrent-flow operations

Figure 8 .
Figure 8. Schematic mass transfer resistances for three mass transfer regions of membrane contactor.

Figure 8 .
Figure 8. Schematic mass transfer resistances for three mass transfer regions of membrane contactor.
Balances of mass flux due to mass diffusion and chemical reaction by the mass conservation were formulated simultaneously.The steady-state isothermal diffusion-reaction process in the gas/liquid membrane contactor module causes the trans-membrane mass flux of CO2 and were formulated by balancing mass flux conservation presented in a finite control element under concurrent-flow and countercurrent-flow operations in Figure 9a,b, respectively.(a) Cocurrent-flow operations Membranes 2023, 13, x FOR PEER REVIEW 11 of 25 (b) Countercurrent-flow operations

Figure 9 .
Figure 9.The mass balances made within a finite fluid element.

Figure 9 .
Figure 9.The mass balances made within a finite fluid element. dC b) Microscopic description of CO2 concentration variations

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.
Microscopic description of CO2 concentration variations

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.

Figure 10 .
Figure 10.The equivalent diameters of 3D printing mini-channel turbulence promoters.

Figure 11 .
Figure 11.The average diameters of Circle-shape and Diamond-shape turbulence promoters.

Figure 10 .
Figure 10.The equivalent diameters of 3D printing mini-channel turbulence promoters.

Figure 11 .
Figure 11.The average diameters of Circle-shape and Diamond-shape turbulence promoters.Figure 11.The average diameters of Circle-shape and Diamond-shape turbulence promoters.

Figure 12 .
Figure 12.SEM images of the PTFE/PP membrane for fresh and used membranes of experimental runs.

Figure 12 .
Figure 12.SEM images of the PTFE/PP membrane for fresh and used membranes of experimental runs.Membranes 2023, 13, x FOR PEER REVIEW 14 of 25

Figure 14 .
Figure 14.Comparison of correlated and experimental Sherwood numbers for various array configurations of 3D printing min-channel turbulence promoters.

Figure 14 .
Figure 14.Comparison of correlated and experimental Sherwood numbers for various array configurations of 3D printing min-channel turbulence promoters.

Figure 15 .
Figure 15.Effects of MEA flow rate and array configurations on absorption fluxes.
. The agreement of the theoretical results with those obtained from experimental results is apparently good.The extent of the CO2 absorption flux of both theoretical predictions and experimental results increases with the MEA feed flow rate and inlet feed CO2 concentration.The magnitude is in the order: Diamond Type B Diamond Type A Circle Type B Circle Type A, as seen in Figures16-19.Embedding turbulence promoters play an important role in interrupting the concentration boundary layer by inducing a higher turbulence intensity on the membrane surface, and thus, the absorption flux improvement was boosted due to diminishing mass-transfer resistance.

Figure 15 .
Figure 15.Effects of MEA flow rate and array configurations on absorption fluxes.

Figure 16 .
Figure 16.Effects of inlet CO2 concentrations with Circle promoters on the CO2 absorption flux.

Figure 17 .
Figure 17.Effects of inlet CO2 concentrations with Circle promoters on the CO2 absorption flux.

Figure 16 .Figure 16 .
Figure 16.Effects of inlet CO 2 concentrations with Circle promoters on the CO 2 absorption flux.

Figure 17 .
Figure 17.Effects of inlet CO2 concentrations with Circle promoters on the CO2 absorption flux.Figure 17.Effects of inlet CO 2 concentrations with Circle promoters on the CO 2 absorption flux.

Figure 17 .Figure 17 .Figure 18 .
Figure 17.Effects of inlet CO2 concentrations with Circle promoters on the CO2 absorption flux.Figure 17.Effects of inlet CO 2 concentrations with Circle promoters on the CO 2 absorption flux.

Figure 18 .Figure 19 .
Figure 18.Effects of inlet CO2 concentrations with Diamond promoters on the CO2 absorption flux.Figure 18.Effects of inlet CO 2 concentrations with Diamond promoters on the CO 2 absorption flux.Membranes 2023, 13, x FOR PEER REVIEW 18 of 25

Figure 19 .
Figure 19.Effects of inlet CO 2 concentrations with Diamond promoters on the CO 2 absorption flux.

Figure 20 .
Figure 20.Comparisons of theoretical CO 2 absorption flux of embedding 3D printing turbulence promoters with/without fabricating mini channels [43].

C in q b ×10 6 (
Microscopic description of CO2 concentration variations

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.
w f ,CO 2 + Q b ρ MEA Membranes 2023, 13, x FOR PEER REVIEW 9 of 25 (b) Microscopic description of CO2 concentration variations

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.

𝐶𝐶 1 (
) and  2() indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.

23, 13 ,
x FOR PEER REVIEW 9 of 25 (b) Microscopic description of CO2 concentration variations

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.

𝐶𝐶 1 (
) and  2() indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.

, 13 ,
x FOR PEER REVIEW 9 of 25 (b) Microscopic description of CO2 concentration variations

Figure 7 .
Figure 7. Schematic mass transfer resistances and concentration profiles of membrane contactor.

𝐶𝐶 1 (
) and  2() indicate the membrane surface concentrations of the CO2/N2 gas feed stream and MEA absorbent feed stream, respectively, as seen from Figure7b.The concentration differences between both streams near the membrane surfaces and those of the bulk stream are used to estimate the temperature polarization coefficient.

Figure 21 .
Figure 21.Effects of shapes of turbulence promoters with or without mini channels on  / .

Figure 21 shows
Figure 21 shows that the countercurrent-flow operations accomplish relatively larger  / values than those of the cocurrent-flow operations with respect to the economic consideration.Meanwhile, the order of the ratio of  / is expected with the same trend of the absorption fluxes with Diamond Type B Circle Type B.

Figure 21 .
Figure 21.Effects of shapes of turbulence promoters with or without mini channels on I E /I P .

Figure 21
Figure 21 shows that the countercurrent-flow operations accomplish relatively larger I E /I H values than those of the cocurrent-flow operations with respect to the economic consideration.Meanwhile, the order of the ratio of I P /I H is expected with the same trend of the absorption fluxes with Diamond Type B > Circle Type B.
Equivalent hydraulic diameter of channel (m), i = promoter empty E P Further absorption flux enhancement Er Accuracy deviation of experimental results from the theoretical predictions f F Fanning friction factor H C Dimensionless Henry's constant H Channel height (m) H i Hydraulic dissipate energy (J kg −1 ), i = carbon, empty I E Absorption flux enhancement I H Power consumption relative index J Absorption flux (mol m −2 s −1 ) k a Mass transfer coefficient in the CO 2 /N 2 stream (m s −1 ) k b Mass transfer coefficient in the MEA absorbent stream (m s −1 ) K ex Equilibrium constant K ex Reduced equilibrium constant K m Overall mass transfer coefficient of membrane (m s −1 ) description of CO2 concentration variations tic mass transfer resistances and concentration profiles of membrane contactor.
[37].The reduced w f ,j Friction loss (J kg −1 ), j = CO 2 , MEA L Channel length (m) M W Molecular weight of water (kg mol −1 ) N exp Number of experimental measurements P Wetted perimeter (m) P 1 Saturation vapor pressure in the CO 2 /N 2 stream (Pa) P 2 Saturation vapor pressure in the MEA absorbent stream (Pa) Q a Volumetric flow rate of the gas feed stream (m 3 s −1 ) Q b Volumetric flow rate of the MEA absorbent side (m 3 s −1 ) R Gas constant (8.314J mol −1 K −1 ) Re Reynolds number Sh promoter Enhanced dimensionless Sherwood number Sh lam Sherwood number for laminar flow W 1 Average width of the promoter (m) W 2 The punched hole diameter (m) W 3 The average width of the punched hole inside the promoter (m) |Y m | 9 of 25 opic description of CO2 concentration variations ematic mass transfer resistances and concentration profiles of membrane contactor.nd 2() indicate the membrane surface concentrations of the CO2/N2 gas feed MEA absorbent feed stream, respectively, as seen from Figure7b.The concenerences between both streams near the membrane surfaces and those of the are used to estimate the temperature polarization coefficient.ntration polarization is enumerated by the ratio of the concentration difference embrane to the concentration difference of both bulk streams, as is called the on polarization coefficient is Equation (1): [37].The reduced n Natural log mean CO 2 mole fraction in the membrane z Axial coordinate along the flow direction (m) Greek letters α E Enhancement factor δ m Thickness of membrane (µm) ε Membrane porosity ν Average velocity (m 3 s −1 ) ρ i Density (Kg m −3 ), i = CO 2 , MEA γ m of CO2 concentration variations atic mass transfer resistances and concentration profiles of membrane contactor.

𝐶𝐶 2 (
) indicate the membrane surface concentrations of the CO2/N2 gas feed EA absorbent feed stream, respectively, as seen from Figure7b.The concennces between both streams near the membrane surfaces and those of the re used to estimate the temperature polarization coefficient.ration polarization is enumerated by the ratio of the concentration difference mbrane to the concentration difference of both bulk streams, as is called the polarization coefficient is Equation (1): between the bulk streams and membrane surfaces, ure 7b, results in decreasing the mass-transfer driving force, and thus, the n flux is reduced.Mass transfer in a membrane gas absorption process ocree regions according to the schematic diagram of the membrane gas/liquid dule: (i) the CO2/N2 feed stream; (ii) the microporous hydrophobic memi) the MEA absorbent feed stream.The influence of the absorption flux is the concentration difference for each mass transfer region, which may be n Equations (2)-(4) under the steady-state operation as follows:J g =k a �C a(g) − C 1(g) � (2) ℓ =k b � K ' ex C 2(l)

)
Membrane surface on MEA side 2 ( g) Membrane surface on CO 2 /N 2 side a CO 2 /N 2 feed flow channel b MEA absorbent flow channel cal Calculated results empty Channel without embedding turbulence promoters exp Experimental results g CO 2 /N 2 feed side in At the inlet 9 of 25 description of CO2 concentration variations tic mass transfer resistances and concentration profiles of membrane contactor.

𝐶𝐶 2 (
) indicate the membrane surface concentrations of the CO2/N2 gas feed absorbent feed stream, respectively, as seen from Figure7b.The concences between both streams near the membrane surfaces and those of the used to estimate the temperature polarization coefficient.ion polarization is enumerated by the ratio of the concentration difference brane to the concentration difference of both bulk streams, as is called the olarization coefficient is Equation (1):