현재 사용되는 전기탈이온(EDI)공정은 전기투석법과 이온교환수지법을 혼합한 공정이다. 이 공정은 전기투석을 위한 양/음이온교환막이 사용되고 두 막 사이 에 이온교환수지로 채워서 모듈을 제작한다. 전기탈이온공정은 농축수가 강한 산성과 염기성이기 때문에 전극의 손상과 같은 문제점을 초래한다. 이러한 문제 점을 해결하기 위해서 전기흡착탈이온(EAD)공정을 사용한다. 전기흡착탈이온공 정은 반대 전하 이온을 흡착시켜 제거하고 역전을 통해서 탈착시켜 이온교환기 를 재생시키는데, 이 때 재생시간이 필요하다. 따라서, 이온교환막을 Bipolar막으 로 제조하여 해결할 수 있고, 전기탈이온공정과 공통적으로 모듈을 작게 만들기 위해서 나노사이즈의 이온교환입자를 제조하여 별도의 처리과정 없이 성능을 구현하고자하였다. 본 연구는 현재 생산되고 있는 모듈보다 높은 이온교환능력 을 가지며 바인더 역할을 할 수 있는 고무상의 고분자를 합성하고 이온교환수 지대신 이온교환능을 가진 nano particle을 이용하여 복합막을 제조하였다.

전기탈이온(EDI) 공정은 전기투석법과 이온교환수지법을 혼합한 공정이다. 모듈을 제조 하는데 있어 전기투석을 위한 양이온교환막과 음이온교환막이 있으며 그사이에 이온교환수지로 채워지는 형태이다. 이온교환수지의 균질한 크기 분포도 및 당량비 또한 장치의 성능을 결정하는 매우 중요한 인자이다. 이러한 점들을 바탕으로 현재 이온교환수지를 글라인딩하여 bipolar형태의 막으로 만든 electroadsorption-deionization(EAD) 공정 모듈이 생산되고 있다. 지금 생산되고 있는 모듈보다 성능을 더 높이기 위하여 이온교환능력을 가지며 바인더 역할을 할 수 있는 고무상의 고분자를 제조 하였다.

이온교환막이 결합된 축전식 탈염공정(Membrane capacitive deionization, MCDI)을 진행하기 위하여 양이온고분자로는 Sulfonated PPO(Poly(2,6-dimethyl-1.4-phenyl oxide)를 사용하였으며 음이온고분자로써 Aminated Polysulfone을 제조하여 전극 표면에 직접 코팅하여 사용하였다. 코팅여부는 SEM 사진을 통하여 확인하였으며, 성능을 알아보기 위하여 흡/탈착실험을 진행하였다. 유속(15, 25, 30 ml./min), 흡착시간(2, 3, 5, 7 min), 유입수의 농도(100, 200, 300, 500ppm)를 변화시켰는데 그 결과 유속은 느릴수록, 흡착시간은 길어질수록, 유입수의 농도가 낮을수록 염 제거 효율이 높게 나타났다.

기존의 전기탈이온(EDI) 공정은 전기투석법과 이온교환수지법을 혼합한 공정이다. 모듈을 제조 하는데 있어 전기투석을 위한 양이온교환막과 음이온교환막이 있으며 그사이에 이온교환수지로 채워지는 형태이다. 이온교환수지의 균질한 크기 분포도 및 당량비 또한 장치의 성능을 결정하는 매우 중요한 인자이다. 이러한 점들을 바탕으로 현재 이온교환수지를 글라인딩하여 bipolar형태의 막으로 만든 electroadsorption-deionization(EAD) 공정 모듈이 생산되고 있다. 지금 생산되고 있는 모듈보다 성능을 더 높이기 위하여 이온교환능력을 가지며 바인더 역할을 할 수 있는 고무상의 고분자를 제조하였다.

In this study, cation and anion exchange process for performance evaluation was conducted. A pilot plant for the ultrpure water production was installed with the capacity of 25 m3/d. The various production rate and regeneration of ion exchange rate were tested to investigate the design parameters. The test resulst was applied to calculate the operating costs. Changing the flow rate of the ion exchange capacity of the reproduction reviewed the cation exchange process as opposed to the design value is 120 to 164% efficiency , whereas both anion exchange process is 82 to 124% efficiency, respectively. This results can be applied for more large scale plant if the scale up parameters are consdiered. The ion exchange capacity of the application in accordance with the design value characteristic upon application equipment is expected to be needed. In this study, the performance of cation and anion exchange resin process was evaluated with pilot plant(25m3/d). The ion exchange capacity along with space velocity and regeneration volume was evaluated. In results, the operation results was compared with design parameters.

다공성 전극표면에 이온교환고분자를 직접 casting하여 만들어진 복합탄소전극의 성능을 알아보기 위해서 NaCl 수용액을 이용하여 흡착시간, 공급액 농도, 유속, 탈착전압에 따라 흡/탈착실험을 진행하였다. 유입수가 100 mg/L일 때 동일 조건에서 흡착시간이 3분에서 5분으로 증가하면서 제거율이 3% 증가하였는데 이는 유입수의 셀 내부 잔류시간의 증가로 인 한 것으로 사료되며 또한 유속이 15 mL/min에서 23 mL/min 증가하면서 효율이 12% 정도 낮음을 보인 것은 유속이 상승하 면서 유입수의 셀 내부 잔류시간이 짧아지면서 나타나는 영향으로 사료된다. 유입수의 농도를 200 mg/L로 증가하였을 때 효 율은 100 mg/L보다 10~15% 정도 낮은 값을 보였는데, 이는 탈착구간에서 완전탈착이 되지 않아 나타나는 것으로 판단된다.

The reduction of setup time is very important in a lot production system. A punch press is a typical system of lot production. This paper describes a case study to reduce setup time of a punch press manufacturing system. Especially, this case study reduce

In this study, an enthalpy exchanger was coated by silver nano particles via spark discharge method and its antimicrobial and heat exchange efficiencies were evaluated. A method utilizing thermophoretic force was used to improve coating efficiency. Four spark discharge systems were parallel connected and generated silver nano aerosol particles (number concentration of 1.65×10⁸ particles/cc, mode diameter of 31 nm). The coating efficiency was evaluated according to various face velocities (V=0.25~1 m/s) and temperature gradients ((T_hot-T_cold)/T_hot=0~0.09). The maximum coating efficiency was 90.8 % when the face velocity was 0.25 m/s and the temperature gradient was 0.09 (Thot=30℃, Tcold=2℃). Silver nano particles were coated onto the enthalpy exchange element and two different coating amounts of silver nano particles (0.11 ㎍/cm³ , 0.22 ㎍/cm³ ) were tested. For evaluation of antimicrobial efficiency, the suspension test method with E. coli was used. After the suspension test method, CFU(colony forming unit)s of each test sample were counted and colony ratio was calculated. The colony ratio was decreased more quickly when the amount of coated silver particles was increased. When the contact time between each sample and suspension was over 3 hours, antimicrobial efficiencies of coated samples were more over 99.9 % for both amount of silver nano particle(0.11 ㎍/cm³ , 0.22 ㎍/cm³ ). The coating of silver nano particles did not affect the heat exchange efficiency.

HF purification performance of an ion exchange membrane(IEM) was evaluated with 0.5% HF spiked with 10ppb of Fe, Ni and Cu nitrates. The result show that after less than five turnovers through an IEM, the metallic impurity concentration drops below 1ppb. The decrease rate can be fitted to a model assuming the experimental tanks to be continuously stirred tank reaction and that the metallic impurity concentration after the IEM is a function of the single-pass purification efficiency of the membrane, the concentration before purification and the metals desorbed form the IEM. The Concentration after purification was investigated up to a cumulative Fe loading of 300ppb in the 23 liter recirculated loop. It increases linearly vs. cumulative loading and can be explained by the Langmuir theory resulting in a purification efficiency at the equilibrium of close to 99.5% in this loading regime.

Functionalized organic polymers have been used as supports for heterogenized homogeneous catalytic process[1]. Sprcific advantages of using these resins as support reagents have been reviewed[2-4]. These include: -ease of by-product separation from the main reaction product usuallyby simple filtration. -prevention of intermolecular reaction of reactive species or functional groups by simulating high dilution conditions[5]. -utility of the "fish-hook" principle in which a minor component in fished out of a large excess substrate by the insoluble polymer[6]. -the possibility of reusing recovered reagents as well as eliminating the use of volatile or noxious substances[7]. Catalysis by ion-exchange membranes is perhaps one of the latest examples of the use of a polymer-supported species. Conceptually, catalysts on membrane supports offer several possible advantages over traditional powder type systems. They are: (1) Membranes immobilize the catalyst, preventing agglomeration. (2) Filtration is unnecessary for the catalyst separation and so complete catalyst recovery is facilitated. (3) Catalytyic and separation processes can be combined, allowing membrane supported catalysts for the continous flow reactors. reactors.

Korea Atomic Energy Research Institute’s Post Irradiated Examination Facility safely stores spent nuclear fuel using a wet storage method to conduct research. Here, in order to remove the radioactivity released into the water, the stored water is passed through an ion exchange resin tower, and the radionuclides are exchanged with the bead-shaped ion exchange resin filled inside to lower the radioactivity concentration. At this time, because the stored water passes in one direction, clogging of the ion exchange resin occurs. If this phenomenon continues, the flow rate of the water treatment process decreases and operation efficiency decreases, so a backwashing process is necessary to re-mix the ion exchange resin and secure the flow rate again. In this study, the flow rate reduction trend according to the lifespan of the ion exchange resin and the flow rate recovery according to the backwash process operation amount were analyzed. The flow rate reduction trend of the ion exchange process was analyzed immediately after the backwashing process was started. In addition, the amount of flow recovery according to the backwash process operation amount was evaluated by the amount of waste generated during the backwash process and the number of days of operation until the backwash process was needed again. As a result, the flow rate of the ion exchange process decreased rapidly right after the backwash process until the position of the ion exchange resins was stabilized, and then stabilized. After that, it gradually decreased and reached the point where the backwash process was necessary. However, the decline trend was analyzed to be the same regardless of the lifespan of the ion exchange resin. In addition, the amount of waste generated during the operation of the backwash process was increased in the order of 400 L, 600 L, 1,100 L, 1,400 L, 3,500 L, and 4,200 L to increase the amount of operation of the backwash process. As a result, the number of days of ion exchange resin operation was 285 days, 338 days, and 342 days, was analyzed as 422 days, 322 days, and 720 days. Based on this study, it was confirmed that the flow rate reduction trend is the same regardless of the lifespan of the ion exchange resin, and as the backwash process operation increases, the number of days the ion exchange process can be operated increases, but there is a turning point where the waste treatment cost exceeds the number of days of operation.

A simulation model was developed for heavy water pre-enrichment and detritiation by the Combined Electrolysis and Catalytic Exchange (CECE) process. In the CECE process, heavy water enrichment and detritiation are based on the principle that concentrated in to water phase through an isotopic exchange reaction between water vapor and hydrogen gas produced by a water electrolysis. An operational analysis for a liquid phase catalytic exchange column was carried out by the model equations, composed of a material balance and combined equilibrium relationships for a scrubbing and catalyst bed, respectively. As a result of simulation, the optimum flow ratio of water to the rising hydrogen gas in contact with the down-coming water was predicted as the key variables in the separation performance analysis at a given feed flow rate and isotopic composition. From a graphical approach based on this model, the operating conditions can be determined within the range where the operating line does not meet the combined equilibrium line before reaching the specified target concentration.

This study proposes a method to define Information Delivery Manual (IDM) for effective assembly process of modular steel bridge. Assembly process is identified according to assembly step then process algorithm for defining Exchange Requirement (ER) is proposed.

Nitrate-selective ion exchange resin which have bulky tertiary amine as functional group have been synthesized by the reaction of chloromethylated polystyrene-divinylbenzene copolymer and the corresponding tertiary amine [NR3=NEt3 1, N(C2H4OH)3 2] in ethanol, while commercial resin has NMe3 as functional group. The fundamental properties such as bulk density, water content, appearance index, exchange capacity, effective size, uniformity coefficient of synthesized anion exchange resin (1) have been measured. The ion exchange resin (1) and (2) exhibited the better selectivity for nitrate than sulfate in both batch and continuous column experiments.

A kinetic study for nitrate removal by anion exchange resin was performed using continuous column reactors. Kinetic approach from the packed bed showed the reaction rate constant k1 was 0.07∼0.17 ℓ/㎎·hr and maximum exchange quantity q0 was 27.75∼31.81 ㎎/g. The results from the continuous column well agreed with that from the batch reactor. An economic analysis of the water treatment plant by anion exchange resin with a regenerating system was performed to design plant and process. Based on the treatment of 20 ㎎/ℓ nitrate-contained wastewater of 10,000 gallons per day to 2 ㎎/ℓ , total capital cost and total annual cost are estimated to be 836 million wons and 211 million wons, respectively.

A kinetic study for anion exchange was performed for commercially available Cl- type anion exchange resin in use to remove nitrate in water. The obtained results from the batch reactor were applied to the Langmuir and Freundlich models. The constants for Langmuir model were qmax=29.82 and b=0.202, and for Freundlich model were K=5.509 and n=1.772. Langmuir model showed better fit than Frendlich model for the experimental results. Ion exchange reaction rate was also calculated and the approximate first-order reaction, rate constant k1 was 0.16 L/㎎·hr. Effective diffusion coefficient was obtained in the range from 9.67×10 exp (-8) to 1.67×10 exp (-6) ㎠/sec for initial concentration change, and from 6.09×10 exp (-7) to 3.98×10 exp (-6) ㎠/sec for reaction temperature change. Activation energy during the diffusion was calculated as 36 ㎉/㏖.