聚酰亚胺6FDA-mPDA及其非对称中空纤维膜的气体渗透性能

用两步法制备了聚酰亚胺2,2＇-双（3,4-二羧酸苯基）六氟丙烷二酐（6FDA）-1,3-苯二胺（mPDA）．测定了聚合物致密膜的密度、自由体积分率和玻璃化转变温度．制备了不同干纺距离下具有超薄致密皮层的聚酰亚胺中空纤维膜．制备的中空纤维膜在25℃,0．5MPa下,O2的渗透速率为19．10GPU,O2／N2分离系数为5．99,CO2的渗透速率为106．34GPU,CO2／CH4的分离系数为82．00．致密皮层的厚度约为96nm．考察了操作温度对膜性能的影响,结果表明,随着温度的升高,膜的渗透速率增大,分离系数减小．物理老化对膜性能的实验结果表明,随着老化时间的增加,膜的渗透速率减小,分离系数增大．膜的致密层厚度影响膜的老化性能．     

Matrimid®5218/PSf双层非对称中空纤维膜的制备及其气体分离性能研究

以商业化聚酰亚胺Matrimid®5218作为功能层材料, 聚砜作为支撑层材料, 采用共挤出法制备双层非对称中空纤维气体分离膜. 所制备的双层非对称中空纤维膜具有致密无缺陷的超薄皮层, 致密皮层厚度约为0.21 μm. 在25 ℃, 0.5 MPa下, CO2/CH4的选择性系数达51.39, CO2的渗透系数为46.29 GPU, O2/N2的选择性系数达到7.13, O2的渗透速率为6.38 GPU. 考察了温度和压力对膜的渗透系数和选择性系数的影响, 并考察了物理老化对膜性能的影响.     

Matrimid5218/PSf双层非对称中空纤维膜的制备及其气体分离性能研究

以商业化聚酰亚胺Matrimid5218作为功能层材料,聚砜作为支撑层材料,采用共挤出法制备双层非对称中空纤维气体分离膜.所制备的双层非对称中空纤维膜具有致密无缺陷的超薄皮层,致密皮层厚度约为0.21μm.在25℃,0.5 MPa下,CO2/CH4的选择性系数达51.39,CO2的渗透系数为46.29 GPU,O2/N2的选择性系数达到7.13,O2的渗透速率为6.38 GPU.考察了温度和压力对膜的渗透系数和选择性系数的影响,并考察了物理老化对膜性能的影响.     

多孔基体负载的碳纳米管复合膜制备及其气体渗透性能

采用改进的浮动催化法在多孔Al2O3基体上制备了垂直取向的碳纳米管阵列, 并用旋转喷涂法将聚苯乙烯填充于碳纳米管的空隙, 进一步将其制备成复合碳纳米管膜, 研究了H2和CO2单组分在碳纳米管复合膜中的渗透性能, 实验结果表明, H2/CO2的理想分离系数随着复合膜中碳管管径的减小而增大, 在管径较小的复合膜中, 气体渗透分离系数高于努森扩散限制, 达到6.25, 具有一定的分离效果. 两种气体在复合膜中的渗透率随着渗透温度的增加而减小.     

壳聚糖膜的有机物－水溶液渗透汽化分离性能

使用均质和复合壳聚糖膜对二氧六环-水和丙酮-水溶液的渗透汽化分离性能进行了研究。结果显示,该膜对两种混合物的分离有很高的选择性和渗透速率。考察料液组成和温度对均质膜分离的影响,随温度升高,分离系数与通量同时增加。从渗透速率与温度的Arrhenius关系求得总的和各组分的表现渗透活化能,复合膜在保持高选择性的同时,渗透速率大幅度提高。     

壳聚糖膜的有机物—水溶液渗透汽化分离性能

使用均质和复合壳聚糖膜对二氧六环－水和丙酮－水溶液的渗透汽化分离性能进行了研究。结果显示，该膜对两种混合物的分离有很高的选择性和渗透速度。考察料液组成和温度对均质膜分离的影响，随温度升高，分离系数与通量同时增加，从渗透速率与温度的Ａｒｒｈｅｎｉｕｓ关系求得总的和各组分的表观渗透活化能。复合膜在保持高选择性的同时，渗透速率大幅度提高。     

酒石酸酯立体选择性萃取分离功夫菊酸对映体

研究了功夫菊酸对映体在含有手性选择剂酒石酸酯的水-有机相双相体系中的萃取分配行为,考察了水相的pH、酒石酸酯的浓度、磷酸盐浓度、温度和酒石酸酯烷基链长度对分配系数(K)和分离因子(α)的影响.研究结果表明:分配系数(K)随pH的升高而降低,随着酒石酸酯浓度的增大而增大,分离因子(α)随pH的升高和酒石酸酯浓度的增大先增加后降低,pH和酒石酸酯浓度分别为5.50和0.30 mol/L时取得较好的分离效果;分配系数(K)和分离因子(α)都随磷酸盐浓度增大而减小;温度、取代烷基链长对分配系数(K)和分离因子(α)亦有较大影响.     

自支撑NH2-MIL-125/聚噁二唑复合正渗透膜的制备及性能

合成了高强度亲水性含羧基聚噁二唑材料(POD-COOH)和含氨基金属有机框架材料(NH₂-MIL-125), 以NH₂-MIL-125为填料, 与POD-COOH基体材料进行溶液共混, 并通过溶液浇铸法制备系列新型自支撑复合正渗透膜, 研究NH₂-MIL-125的引入对复合正渗透膜结构和性能的影响. 研究结果表明, 所制备的系列复合正渗透膜均呈致密结构, 且随着NH₂-MIL-125含量的增加, 复合膜的表面亲水性增加、 电负性增强, 并保持良好的机械性能. 以去离子水为进料液, 1.5 mol/L硫酸钠溶液为汲取液, 对上述自支撑复合膜进行正渗透性能测试, 发现由于消除了传统正渗透膜支撑层的内浓差极化现象, 该新型复合正渗透膜在分离过程中具有优异的正渗透性能.     

自支撑NH_2-MIL-125/聚■二唑复合正渗透膜的制备及性能

合成了高强度亲水性含羧基聚■二唑材料(POD-COOH)和含氨基金属有机框架材料(NH_2-MIL-125),以NH_2-MIL-125为填料,与POD-COOH基体材料进行溶液共混,并通过溶液浇铸法制备系列新型自支撑复合正渗透膜,研究NH_2-MIL-125的引入对复合正渗透膜结构和性能的影响.研究结果表明,所制备的系列复合正渗透膜均呈致密结构,且随着NH2-MIL-125含量的增加,复合膜的表面亲水性增加、电负性增强,并保持良好的机械性能.以去离子水为进料液,1. 5 mol/L硫酸钠溶液为汲取液,对上述自支撑复合膜进行正渗透性能测试,发现由于消除了传统正渗透膜支撑层的内浓差极化现象,该新型复合正渗透膜在分离过程中具有优异的正渗透性能.     

立体选择性萃取分离反式DV菊酸对映体

研究了反式DV菊酸对映体在含有手性选择体酒石酸酯的水-有机相双相体系中的萃取分配行为,考察了有机稀释剂种类、酒石酸酯的浓度、温度、水相的pH值、酒石酸酯烷基链长度对分配系数(D)和分配因子(α)的影响.研究表明:三氯甲烷作稀释剂时萃取分离效果较好;温度升高使分配系数增大,分离因子减小;分配系数随pH的升高而降低,随着酒石酸酯浓度的增大而增大,分离因子随pH的升高和酒石酸酯浓度的增大先增加后降低,pH和酒石酸酯浓度分别为4.50和0.40mol/L时取得较好的分离效果;取代烷基链长对分配系数(D)和分离因子(α)亦有较大影响.     

Preparation of composite poly（ether block amide） membrane for CO2 capture

In this study, a poly（ether block amide） （Pebax 1657） composite membrane applied for COa capture was prepared by coating Pebax 1657 solution on polyacrylonitrile （PAN） ultrafiltration membrane. Ethanol/water mixture was used as the solvent of Pebax and the effects of ethanol/water mass ratios and Pebax concentration on the permeation properties of composite membrane were studied. To enhance the com- posite membrane permeance, the gutter layer, made from reactive amino silicone crosslinking with potydimethylsiloxane （PDMS）, was de- signed. The influence of crosslinldng degree of the gutter layer on membrane performance was investigated. As a result, a Pebardamino- PDMS/PAN multilayer membrane with hexane resistance was developed, showing CO2 permeance of 350 GPU and CO2/N2 selectivity over 50. The blend of polyethylene glycol dimethyl ether （PEG-DME） with Pebax as coating material was studied to further improve the membrane performance. After being combined with PEG-DME additive, CO2 permeance of the final Pebax-PEG-DME/amino-PDMS/PAN composite membrane reached 400 GPU above with CO2/Na selectivity over 65.     

Formation of integrally skinned asymmetric polysulfone gas separation membranes by supercritical CO2

Integrally skinned asymmetric polysulfone membranes were prepared from originally dense films inducing asymmetry by the formation of the porous layer adding to one side of the membranes chloroform and supercritical CO₂ (SCCO₂), and then allowing the SCCO₂ expansion to occur. The influence of the chloroform/polysulfone mass ratio (g CH₃Cl/g PSF), SCCO₂ density and depressurization rate over the thickness of both the porous and the dense skin layers, the morphology of the porous support and the pure O₂ and N₂ permeability and selectivity performance were studied.The results show that it is possible to induce a very-controlled asymmetry in a dense film following the procedure described in this work and as expected, the thickness of the porous layer increases while the dense skin layer decreases as the chloroform/polysulfone mass ratio increases. Images of the porous layer show that the average-pore size decreases at high SCCO₂ densities and slightly decreases with increasing the CO₂ depressurization rates. The O₂ and N₂ permeability coefficients, measured at 35 °C and 2 bar, for the polysulfone asymmetric membranes are practically the same of those determined in dense films, suggesting that the dense skins are essentially defect-free of pinholes.     

Preparation of composite poly(ether block amide)membrane for CO_2 capture

In this study, a poly(ether block amide)(Pebax 1657) composite membrane applied for CO2 capture was prepared by coating Pebax 1657 solution on polyacrylonitrile(PAN) ultrafiltration membrane. Ethanol/water mixture was used as the solvent of Pebax and the effects of ethanol/water mass ratios and Pebax concentration on the permeation properties of composite membrane were studied. To enhance the composite membrane permeance, the gutter layer, made from reactive amino silicone crosslinking with polydimethylsiloxane(PDMS), was designed. The influence of crosslinking degree of the gutter layer on membrane performance was investigated. As a result, a Pebax/aminoPDMS/PAN multilayer membrane with hexane resistance was developed, showing CO2 permeance of 350 GPU and CO2/N2 selectivity over50. The blend of polyethylene glycol dimethyl ether(PEG-DME) with Pebax as coating material was studied to further improve the membrane performance. After being combined with PEG-DME additive, CO2 permeance of the final Pebax-PEG-DME/amino-PDMS/PAN composite membrane reached 400 GPU above with CO2/N2 selectivity over 65.     

Composite hollow fiber membranes for CO2 capture

Composite hollow fibers membranes were prepared by coating poly(phenylene oxide) (PPO) and polysulfone (PSf) hollow fibers with high molecular polyvinylamine (PVAm). Two procedures of coating hollow fibers outside and respective inside were investigated with respect to intrinsic PVAm solution properties and hollow fibers geometry and material.The influence of operating mode (sweep or vacuum) on the performances of membranes was investigated. Vacuum operating mode gave better results than using sweep because part of the sweep gas permeated into feed and induced an extra resistance to the most permeable gas the CO₂. The composite PVAm/PSf HF membranes having a 0.7–1.5 μm PVAm selective layer, showed CO₂/N₂ selectivity between 100 and 230. The selectivity was attributed to the CO₂ facilitated transport imposed by PVAm selective layer. The CO₂ permeance changed from 0.006 to 0.022 m³(STP)/(m² bar h) in direct correlation with CO₂ permeance and separation mechanism of the individual porous supports used for membrane fabrication. The multilayer PVAm/PPO membrane using as support PPO hollow fibers with a 40 nm PPO dense skin layer, surprisingly presented an increase in selectivity with the increase in CO₂ partial pressure. This trend was opposite to the facilitated transport characteristic behaviour of PVAm/porous PSf. This indicated that PVAm/PPO membrane represents a new membrane, with new properties and a hybrid mechanism, extremely stable at high pressure ratios. The CO₂/N₂ selectivity ranged between 20 and 500 and the CO₂ permeance from 0.11 to 2.3 m³(STP)/(m² bar h) depending on the operating conditions.For both PVAm/PSf and PVAm/PPO membranes, the CO₂ permeance was similar with the CO₂ permeance of uncoated hollow fiber supports, confirming that the CO₂ diffusion rate limiting step resides in the properties of the relatively thick support, not at the level of 1.2 μm thin and water swollen PVAm selective layer. A dynamic transfer of the CO₂ diffusion rate limiting step between PVAm top layer and PPO support was observed by changing the feed relative humidity (RH%). The CO₂ diffusion rate was controlled by the PPO support when using humid feed. At low feed humidity the 1.2 μm PVAm top layer becomes the CO₂ diffusion rate limiting step.     

Preparation of silica–alumina composite membranes for hydrogen separation by multi-step pore modifications

In the present paper, a silica–alumina composite membrane for hydrogen separation was prepared within an α-alumina support by the multi-step pore modification. The α-alumina support has an asymmetric structure composed of a thin dense skin layer and a thick coarse layer and the average pore size of its skin layer is 80 nm. The composite membrane layer was formed in the vicinity of the interphase between the two layers of the support by two consecutive steps; namely, in situ silica sol–gel reaction and soaking and vapor deposition. In order to enhance the hydrogen selectivity, palladium (Pd) particles were impregnated in the final step utilizing Pd-acetate as a Pd precursor. Although both silica and Pd induced the surface diffusion, Pd was more effective for selective hydrogen adsorption than silica. This multi-step method produced a porous membrane with moderate hydrogen selectivity and satisfactory hydrogen permeance at high temperature and at high transmembrane pressure. The separation factor of hydrogen relative to nitrogen was maintained at about 10 even when the transmembrane pressure was as high as 110 kPa, and the hydrogen permeance was still much higher than that of non-porous polymeric membranes. In addition, the microstructural distributions of Si and Pd within the intermediate membrane layer were examined by a scanning electron microscopy (SEM) and an energy dispersive X-ray analysis (EDX)     

负载型CuO/TiO2催化剂催化CO2加氢制甲醇

采用浸渍法制备了CuO/TiO₂负载型催化剂,并将其用于CO₂加氢制甲醇反应。重点考察了铜的负载量对催化剂性能的影响,并对其物化性能和催化性能之间的关系进行了讨论。结果发现,随着铜负载量的增加,催化剂中金属铜的比表面先增加后减小,当铜的负载量为10%（质量百分数）时达到最大值。催化剂的表面碱性位数量随铜含量的增加持续减小,中等碱位和强碱位的强度下降。当铜的负载量不高于10%时,CO₂的转化率与铜的比表面积呈线性关系。甲醇选择性与催化剂的表面碱位性质有关,过强的碱性位会降低甲醇选择性。     

负载型CuO/TiO2催化剂催化CO2加氢制甲醇

采用浸渍法制备了CuO/TiO_2负载型催化剂,并将其用于CO2加氢制甲醇反应。重点考察了铜的负载量对催化剂性能的影响,并对其物化性能和催化性能之间的关系进行了讨论。结果发现,随着铜负载量的增加,催化剂中金属铜的比表面先增加后减小,当铜的负载量为10%(质量百分数)时达到最大值。催化剂的表面碱性位数量随铜含量的增加持续减小,中等碱位和强碱位的强度下降。当铜的负载量不高于10%时,CO2的转化率与铜的比表面积呈线性关系。甲醇选择性与催化剂的表面碱位性质有关,过强的碱性位会降低甲醇选择性。     

Fabrication and characterization of γ-Al2O3–clay composite ultrafiltration membrane for the separation of electrolytes from its aqueous solution

In this paper, we have reported the preparation of low cost γ-Al₂O₃ membrane on a macroporous clay support by dip-coating method. For the synthesis of γ-Al₂O₃ top layer on the support, a stable boehmite sol is prepared using aluminium chloride salt as a starting material by sol–gel route. The structural properties of the composite membrane as well as γ-Al₂O₃ powder is carried out using scanning electron microscopy (SEM), X-ray diffraction (XRD), nitrogen adsorption–desorption isotherm data, Fourier transform infrared analysis (FTIR) and dynamic light scattering (DLS) analysis. The mean particle size of the boehmite sol used for coating is found to be 30.9 nm. The pore size distribution of the γ-Al₂O₃–clay composite membrane is found to be in the range of 5.4–13.6 nm. Separation performance of the membrane in terms of flux and rejection of single salts solution such as MgCl₂ and AlCl₃ as a function of pH, salt concentration and applied pressure is also studied. The rejection and flux behavior are found to be strongly dependent on electrostatic interaction between the charged molecules and γ-Al₂O₃–clay composite membrane. The intrinsic rejection has been determined by calculating the concentration at membrane surface (C_m) using Speigler–Kedem model. It is found that the observed rejection shows anomalous trend with increase in applied pressure and the intrinsic rejection increases with increase in applied pressure, a trend typical of the separation of electrolyte through charged membranes. At acidic pH, both the salt solution shows higher rejection. With increase in the salt concentration, observed rejection of salt decreases due to the enhanced concentration polarization. The maximum rejection of MgCl₂ and AlCl₃ is found to be 72% and 88%, respectively for salt concentration of 3000 ppm.     

Fabrication of polymer/fluoride-containing salts blend composite membranes for CO2 separation

Poly (N, N-dimethylaminoethyl methacrylate)-poly (ethylene glycol methyl ether methacrylate) (PDMAEMA-PEGMEMA) and cesium fluoride (CsF) were blended and used as the separation material of composite membranes. Hollow fiber composite membranes were fabricated by coating the blend on polysulfone (PSf) hollow fiber substrate. Introduction of fluorine ion improved the separation performance of the membrane. The concentration of coating solution was adjusted to obtain a membrane with high permeance. The composite membrane showed good performance with the CO2 permeance of 30.4 GPU (1 GPU = 10^-6 cm³(STP)/(cm²·s·cmHg)), and selectivities to CO2/N2, CO2/CH4, CO2/H2 and O2/N2 of 47.2, 37.6, 1.75 and 4.70, respectively. Potassium fluoride (KF), due to its low cost, was also used as a substitute of CsF to prepare composite membrane and the permeation data showed that CsF can be replaced by KF. The effect of operating temperature on the permeation properties of the composite membrane was also investigated.     

Pebax/TSIL blend thin film composite membranes for CO_2 separation

In this study a thin film composite (TFC) membrane with a Pebax/Task-specific ionic liquid (TSIL) blend selective layer was prepared. Defect-free Pebax/TSIL layers were coated successfully on a polysulfone ultrafiltration porous support with a polydimethylsiloxane (PDMS) gutter layer. Different parameters in the membrane preparation (e.g. concentration, coating time) were investigated and optimized. The morphology of the membranes was studied by scanning electron microscopy (SEM), while the thermal properties and chemical structures of the membrane materials were investigated by thermo-gravimetric analyzer (TGA), differential scanning calorimetry (DSC) and Fourier transform infrared spectroscopy (FTIR). The CO₂ separation performance of the membrane was evaluated using a mixed gas permeation test. Experimental results show that the incorporation of TSIL into the Pebax matrix can significantly increase both CO₂ permeance and CO₂/N₂ selectivity. With the presence of water vapor, the membrane exhibits the best CO₂/N₂ selectivity at a relative humidity of around 75%, where a CO₂ permeance of around 500 GPU and a CO₂/N₂ selectivity of 46 were documented. A further increase in the relative humidity resulted in higher CO₂ permeance but decreased CO₂/N₂ selectivity. Experiments also show that CO₂ permeance decreases with a CO₂ partial pressure increase, which is considered a characteristic in facilitated transport membranes.