巯基改性活性炭对水溶液中汞的吸附性能研究

利用活性炭与巯基乙酸间的酯化反应，制备了巯基改性活性炭AC-SH，并通过静态吸附实验研究了该材料对水溶液中汞的吸附性能。研究结果表明，该改性方法可以在活性炭上嫁接2.31 mmol/g的巯基，AC-SH对汞的最大吸附容量高达556 mg/g；AC-SH的适用pH值范围非常广，在pH 1.5～10.5范围内其对汞的吸附去除率均达到90％以上，最佳吸附pH值范围为3～7；氯离子对AC-SH的吸附性能具有一定的抑制作用，原因在于它能和汞离子络合形成一系列吸附性能较差的Hg-Cl络合物。     

改性污泥活性炭对水中镉离子的吸附性能

以城市污水处理厂的剩余污泥为原料,氯化锌为活化剂制备污泥活性炭,对一部分污泥活性炭用6.0 mol/L的硝酸进行改性,并研究了未改性和改性的污泥活性炭对Cd2＋的吸附行为的影响。结果表明,在pH为5.0、Cd2＋初始浓度为100 mg/L、吸附剂投加量为2.0 g/L、反应温度为25℃时,未改性的污泥活性炭吸附容量为8.45 mg/g,硝酸改性的污泥活性炭吸附容量达到了23.35 mg/g。改性和未改性的污泥活性炭对Cd2＋都有较好的吸附容量,硝酸改性大幅度提高了污泥活性炭对Cd2＋的吸附性能。常温下改性污泥活性炭对Cd2＋的吸附符合Langmuir吸附等温式。     

常压制备秸秆活性炭对水溶液中磷元素的吸附

开发了非真空制备秸秆活性炭的新方法,以稻草秸秆为原料,醋酸钙和氯化锌为活化剂,经热处理,一步合成改性秸秆活性炭。XRD图谱显示,产物为碳酸钙改性活性炭;SEM和TEM的表征结果显示,该活性炭具有微米-纳米多维孔结构,碳酸钙颗粒均匀分布在活性炭的表面和基体中;BET比表面积实验测得不同浓度碳酸钙改性活性炭的比表面积在324~846 m2/g之间。含磷水溶液吸附实验表明,当改性活性炭中碳酸钙含量为1.5%时,活性炭具有最大吸附速率1.76 L/mg;碳酸钙含量为2.0%时,活性炭具有最大吸附容量3.21 mg/g。改性活性炭对磷元素的吸附过程符合Langmuir模型,说明改性活性炭对磷的吸附为单分子层吸附。     

竹材加工剩余物制备竹活性炭及其对Pb^2＋的吸附性能

利用竹材加工剩余物竹蔸、竹节和竹枝制备竹炭,再以H3PO4为活化剂,在活化温度为700 ℃和不同的H3PO4浓度下进行活化制备竹活性炭,测定了吸附性能最强的竹活性炭在不同吸附时间和Pb2+初始浓度下对Pb2+的吸附率,并进行了结构表征.结果表明,当H3PO4溶液质量分数为45%时,所制备的竹活性炭吸附性能最强,其中竹蔸活性炭的Pb2+吸附性能接近于商品活性炭;竹蔸活性炭吸附Pb2+的吸附时间在120～180 min为佳;根据Langmuir最大吸附量计算公式求得竹蔸活性炭最大吸附量为91.1 mg/g.竹枝炭、竹节炭与竹篼炭的孔隙度分别为0.656、0.698和0.740,竹枝活性炭、竹节活性炭与竹篼活性炭的孔隙度分别为0.690、0.715和0.755;竹篼炭和竹篼活性炭比表面积分别为110.354、462.069 m2/g,孔容分别为0.090、0.235 cm3/g,平均孔径分别为31.552、20.368 .     

单质硫改性介孔炭对水溶液中汞的吸附性能研究

对介孔炭CMK-3进行单质硫改性得到OMC-S，并通过静态吸附实验研究了该材料对水溶液中汞的吸附性能。研究结果表明：单质硫改性可以在介孔炭上负载12.33%的硫，从而使得介孔炭对汞的吸附容量从185 mg/g提高到476 mg/g；OMC-S具有较广的适用pH值范围，在pH 3～11.5范围内其对汞的吸附去除率均达到92%以上；氯离子对OMC-S的吸附性能具有一定的抑制作用，原因在于它能和汞离子络合形成一系列吸附性能较差的Hg-Cl络合物，而腐殖酸在所研究的范围内对OMC-S的吸附性能无明显影响。     

银负载对活性炭纤维汞吸附性能的影响

银氨溶液浸渍活性炭纤维制得载银量14.07%的载银活性炭纤维.以筒状吸附体吸附气态Hg0的方式研究活性炭纤维银载前后的汞吸附性能,结果表明,载银后活性炭纤维汞吸附性能明显提高.实验还发现:随吸附温度升高,活性炭纤维的汞吸附效率随先增加后降低,而载银活性炭纤维的汞吸附效率随吸附温度升高而一直降低;延长停留时间和添加H2O(g)对两者汞吸附均有利.采用片状吸附体对2种吸附剂的汞饱和吸附量进行了测定,实验得出:70℃下活性炭纤维汞饱和吸附量为29.4 mg/g,载银活性炭纤维汞饱和吸附量为192.3 mg/g,即活性炭纤维载银后汞饱和吸附量提高到原来的6.54倍.扫描电镜分析发现:活性炭纤维上物理吸附汞占绝大多数,化学吸附汞很少;负载银后汞只吸附在活性炭纤维的含银活性点上,银粒子与汞结合生成银汞齐后形状趋于规则,且主要分布于活性炭纤维微晶的晶棱交界处.     

TEMPO氧化微晶纤维素和马来酸酐接枝微晶纤维素的制备及对Cu~(2+)的吸附

通过马来酸酐(MA)固相接枝和四甲基哌啶(TEMPO)氧化体系改性微晶纤维素(MCC)制备了两种重金属离子吸附剂,对比了MA和TEMPO氧化体系对MCC的改性后对铜离子的吸附效果。结果表明:两者对MCC的改性都有效果,在铜离子浓度小于500 mg/L时,经TEMPO改性的MCC吸附容量和吸附率明显大于MA改性的MCC。经TEMPO改性后的MCC对铜离子的吸附性能提高,在室温条件下,0.22 g改性后MCC对pH=5.77,浓度为20 mg/L的铜离子溶液最大吸附率为90.56%,最大吸附容量为9.1 mg/g。     

改性活性炭对废水中铬离子的吸附

改性活性炭被广泛应用于吸附水体中重金属离子,但关于铁改性活性炭吸附性能的研究报道甚少。本研究对活性炭进行铁改性处理,并将之应用于水中的铬离子吸附,考察了吸附时间、溶液p H对改性活性炭吸附Cr(Ⅵ)效果的影响。实验结果表明,在25℃下,p H为3,吸附时间为300 min时,其对Cr(Ⅵ)的去除率为91.4%。铁改性活性炭对铬离子的吸附机理服从准二级动力学方程,该吸附剂吸附等温线服从Langmuir方程,饱和吸附量为28.82 mg/g。     

三价铁改性活性炭对水中微量砷的吸附特性

研究了三价铁改性对不同活性炭(颗粒和粉末)对水中砷的吸附特性的影响。结果表明,三价铁改性有效提高了活性炭对不同形态砷的吸附性能。其中,对于2种活性炭,As(Ⅲ)和As(Ⅴ)的最佳铁离子改性浓度分别为0.1和0.05 mol/L。此时,通过Langmuir等温线方程拟合得到:粉末和颗粒活性炭对As(Ⅲ)的最大吸附量qm分别为2.38 mg/g和9.39 mg/g;而对As(Ⅴ)的qm分别为5.12 mg/g和2.32 mg/g。此外,当溶液的p H从3升高到9的过程中,吸附量先增加后有所下降,当p H为7时,改性前后的活性炭对砷的吸附量达到最高。     

脱灰煤基活性炭吸附处理含镉废水简

考察了硝酸脱灰煤样自制活性炭对Cd（Ⅱ）的吸附去除特征。结果表明，随煤样粒径的减小，活性炭的吸附能力增强，吸附过程符合分形动力学特征；随着镉浓度的升高，活性炭对镉的吸附量增加，活性炭吸附镉符合Langmuir 等温方程，镉离子在活性炭上的吸附属单分子层吸附；煤基活性炭适宜的吸附除镉条件为粒径0.054 mm、Cd（Ⅱ）初始浓度35 mg/L、活性炭用量0.05 g、吸附时间1 h，此时的吸附容量达40 mg/g。     

过渡金属浸渍改性ACF去除H_2S研究

为探讨活性炭纤维（ACF）去除恶臭气体H2S的性能,采用过渡金属浸渍改性ACF吸附H2S,揭示出改性ACF前后吸附H2S的性能差异及浸渍剂的浓度和种类对ACF吸附性能的影响。结果表明,通过过渡金属改性后的ACF吸附性能有显著提高,对H2S吸附是物理吸附和化学吸附共同作用的结果,改性后的ACF硫容量大小依次为：5%硝酸铜改性ACF〉5%硝酸钴改性ACF〉5%硝酸锰改性ACF。不同浓度浸渍剂改性后的ACF吸附H2S性能有所不同,硫容量呈现出随着浓度升高先增大后减小的趋势。不同浸渍剂改性后的ACF吸附穿透曲线也不同,穿透时间依次为：TCu-ACF〉TCo-ACF〉TMn-ACF。混合金属溶液改性ACF吸附H2S,5%硝酸铜-3%硝酸钴溶液改性ACF吸附性能最佳,硫容量可达166.7 mg/g;而5%硝酸铜-3%硝酸钴-1%硝酸锰溶液改性的ACF效果最差,硫容量仅为83.3 mg/g。     

脱灰煤基活性炭吸附处理含镉废水

考察了硝酸脱灰煤样自制活性炭对Cd（Ⅱ）的吸附去除特征。结果表明，随煤样粒径的减小，活性炭的吸附能力增强，吸附过程符合分形动力学特征；随着镉浓度的升高，活性炭对镉的吸附量增加，活性炭吸附镉符合Langmuir等温方程，镉离子在活性炭上的吸附属单分子层吸附；煤基活性炭适宜的吸附除镉条件为粒径0．054mm、Cd（Ⅱ）初始浓度35mg／L、活性炭用量0．05g、吸附时间1h，此时的吸附容量达40mg／g。     

高温载硫活性炭的制备及脱汞能力研究

研究了载硫温度、硫炭比(简称S/C),吸附温度等因素对载硫活性炭的硫含量、脱汞能力以及硫损失的影响,探讨载硫活性炭制备的工艺条件优化。结果表明,不同载硫温度下制备的载硫活性炭的气态Hg0吸附能力远强于原料活性炭;载硫温度不同时,负载到活性炭孔隙或表面上的硫的形态不同,导致了脱汞能力的差异,较合适的载硫温度为350℃;S/C为5%(质量分数,下同)时,随着吸附温度的升高,载硫活性炭的气态Hg0吸附量降低;在一定的载硫温度下,原料中S/C越高时,制备的载硫活性炭的硫含量越高、气态Hg0吸附能力越强,但其硫损失率也越高,从实际的使用效果来看,较合适的S/C为10%。     

Removal of carbonyl sulfide using activated carbon adsorption

Wastewater treatment plant odors are caused by compounds such as hydrogen sulfide (H2S), methyl mercaptans, and carbonyl sulfide (COS). One of the most efficient odor control processes is activated carbon adsorption; however, very few studies have been conducted on COS adsorption. COS is not only an odor causing compound but is also listed in the Clean Air Act as a hazardous air pollutant. Objectives of this study were to determine the following: (1) the adsorption capacity of 3 different carbons for COS removal; (2) the impact of relative humidity (RH) on COS adsorption; (3) the extent of competitive adsorption of COS in the presence of H2S; and (4) whether ammonia injection would increase COS adsorption capacity. Vapor phase react (VPR; reactivated), BPL (bituminous coal-based), and Centaur (physically modified to enhance H2S adsorption) carbons manufactured by Calgon Carbon Corp. were tested in three laboratory-scale columns, 6 in. in depth and 1 in. in diameter. Inlet COS concentrations varied from 35 to 49 ppmv (86-120 mg/m3). RHs of 17%, 30%, 50%, and 90% were tested. For competitive adsorption studies, H2S was tested at 60 ppmv, with COS at 30 ppmv. COS, RH, H2S, and ammonia concentrations were measured using an International Sensor Technology Model IQ-350 solid state sensor, Cole-Parmer humidity stick, Interscan Corp. 1000 series portable analyzer, and Drager Accuro ammonia sensor, respectively. It was found that the adsorption capacity of Centaur carbon for COS was higher than the other two carbons, regardless of RH. As humidity increased, the percentage of decrease in adsorption capacity of Centaur carbon, however, was greater than the other two carbons. The carbon adsorption capacity for COS decreased in proportion to the percentage of H2S in the gas stream. More adsorption sites appear to be available to H2S, a smaller molecule. Ammonia, which has been found to increase H2S adsorption capacity, did not increase the capacity for COS.     

Preparation of activated carbon using low temperature carbonisation and physical activation of high ash raw bagasse for acid dye adsorption

Activated carbons were prepared from bagasse through a low temperature (160 degrees C) chemical carbonisation treatment and gasification with carbon dioxide at 900 degrees C. The merit of low temperature chemical carbonisation in preparing chars for activation was assessed by comparing the physical and chemical properties of activated carbons developed by this technique to conventional methods involving the use of thermal and vacuum pyrolysis of bagasse. In addition, the adsorption properties (acid blue dye) of these bagasse activated carbons were also compared with a commercial activated carbon. The results suggest that despite the high ash content of the precursor, high surface areas (614-1433 m2 g(-1)) and microporous (median pore size from 0.45 to 1.2 nm) activated carbons can be generated through chemical carbonisation and gasification. The micropore area of the activated carbon developed from chars prepared by the low temperature chemical carbonisation provides favourable adsorption sites to acid blue dye (391 mg g(-1) of carbon). The alkalinity of the carbon surface and total surface area were shown to have complementary effects in promoting the adsorption of acid blue dye. Adsorption of the anionic coloured component of the acid dye was shown to be promoted in carbon exhibiting alkaline or positively charged surfaces. This study demonstrates that activated carbons with high acid dye adsorption capacities can be prepared from high ash bagasse based on low temperature chemical carbonisation and gasification.     

Enhanced mercuric chloride adsorption onto sulfur-modified activated carbons derived from waste tires

A number of activated carbons derived from waste tires were further impregnated by gaseous elemental sulfur at temperatures of 400 and 650 degrees C, with a carbon and sulfur mass ratio of 1:3. The capabilities of sulfur diffusing into the micropores of the activated carbons were significantly different between 400 and 650 degrees C, resulting in obvious dissimilarities in the sulfur content of the activated carbons. The sulfur-impregnated activated carbons were examined for the adsorptive capacity of gas-phase mercuric chloride (HgC1) by thermogravimetric analysis (TGA). The analytical precision of TGA was up to 10(-6) g at the inlet HgCl2 concentrations of 100, 300, and 500 microg/m3, for an adsorption time of 3 hr and an adsorption temperature of 150 degrees C, simulating the flue gas emitted from municipal solid waste (MSW) incinerators. Experimental results showed that sulfur modification can slightly reduce the specific surface area of activated carbons. High-surface-area activated carbons after sulfur modification had abundant mesopores and micropores, whereas low-surface-area activated carbons had abundant macropores and mesopores. Sulfur molecules were evenly distributed on the surface of the inner pores after sulfur modification, and the sulfur content of the activated carbons increased from 2-2.5% to 5-11%. After sulfur modification, the adsorptive capacity of HgCl2 for high-surface-area sulfurized activated carbons reached 1.557 mg/g (22 times higher than the virgin activated carbons). The injection of activated carbons was followed by fabric filtration, which is commonly used to remove HgCl2 from MSW incinerators. The residence time of activated carbons collected in the fabric filter is commonly about 1 hr, but the time required to achieve equilibrium is less than 10 min. Consequently, it is worthwhile to compare the adsorption rates of HgCl2 in the time intervals of < 10 and 10-60 min.     

Physico-chemical treatments for the complete removal of non-ionic surfactants from effluents

Adsorption isotherms for a selection of non-ionic surfactants on activated carbons indicated the effectiveness of the latter in the removal of these pollutants from secondary effluents. The removal efficiencies were found to be improved when the secondary effluent was first flocculated with ferric chloride. This effectively removed some 80% of the non-ionic surfactant in the effluent. Batch adsorption experiments with powdered activated carbon removed 97% of the surfactant at low carbon dosage. A granular carbon with the best adsorption capacity was selected for continuous-flow operation in which non-ionic surfactants, COD and anionic surfactant alkyl benzene sulphonate were monitored. The breakthrough capacity for the non-ionic surfactants was in excess of 6000 bed volumes throughput of flocculated, sand-filtered effluent in a laboratory scale carbon column. Such a procedure is suggested for the complete removal of such pollutants from effluents.     

双氯芬酸的吸附去除过程与机制

研究了非甾体抗炎药双氯芬酸的吸附去除过程与机制。对吸附处理效果较好的活性炭与纳米羟基氧化铁（α-FeOOH）进行了比表面积、Zeta电位等表面特性的表征，研究比较了双氯芬酸在活性炭与α—FeOOH2种材料上的吸附去除效果与吸附机制。结果表明，在相同的实验条件下，活性炭与α-FeOOH对双氯芬酸吸附去除率可分别达到97．9％和84．3％；双氯芬酸在活性炭上的吸附主要是由于活性炭较大的比表面积与疏水分配作用，在α-FeOOH上的吸附主要是由于静电引力作用；活性炭与α-FeOOH对双氯芬酸的吸附去除效果均随pH的升高而降低；在pH=6时，活性炭与α-FeOOH对双氯芬酸钠的吸附等温线均符合Langmuir方程，单位饱和吸附量分别为109．98mg／g和58．96mg／g；活性炭对双氯芬酸具有更强的吸附能力。     

Activated carbon from industrial solid waste as an adsorbent for the removal of Rhodamine-B from aqueous solution: kinetic and equilibrium studies

The activated carbon was prepared using industrial solid waste called sago waste and physico-chemical properties of carbon were carried out to explore adsorption process. The effectiveness of carbon prepared from sago waste in adsorbing Rhodamine-B from aqueous solution has been studied as a function of agitation time, adsorbent dosage, initial dye concentration, pH and desorption. Adsorption equilibrium studies were carried out in order to optimize the experimental conditions. The adsorption of Rhodamine-B onto carbon followed second order kinetic model. Adsorption data were modeled using both Langmuir and Freundlich classical adsorption isotherms. The adsorption capacity Q0 was 16.12 mg g(-1) at initial pH 5.7 for the particle size 125-250 microm. The equilibrium time was found to be 150 min for 10, 20 mg l(-1) and 210 min for 30, 40 mg l(-1) dye concentrations, respectively. A maximum removal of 91% was obtained at natural pH 5.7 for an adsorbent dose of 100mg/50 ml of 10 mg l(-1) dye concentration and 100% removal was obtained when the pH was increased to 7 for an adsorbent dose of 275 mg/50 ml of 20 mg l(-1) dye concentration. Desorption studies were carried out in water medium by varying the pH from 2 to 10. Desorption studies were performed with dilute HCl and show that ion exchange is predominant dye adsorption mechanism. This adsorbent was found to be both effective and economically viable.