五种酯类化合物极微蒸气压的扭转法测定

<正> 引言 物质的饱和蒸气压是最重要的物性数据之一.在化工设计、生产与科学研究中,如农药、化肥的储存,香料的挥发速度,橡胶、塑料中增塑剂的有效寿命等,对有机酯类化合物低蒸气压数据要求迫切.由于测定难度以及数据准确性等问题,目前极微蒸气压的数据非常缺乏.测定方法主要有Knudsen隙透法和同位素示踪法,后者由于实验条件苛刻而很少     

松节油体系组分饱和蒸气压研究进展

本文综述了松节油体系组分的饱和蒸气压研究现状,根据松节油由双环单萜和倍半萜组成的特性,提出了适用于松节油体系组分饱和蒸气压的测定原理、测量方法、数据关联及估算方法。松节油体系组分是沸点相近的萜类同分异构体,难以分离得到纯度很高的松节油组分,利用稀溶液溶剂符合Raoult定律的原理,间接测定蒎烷、顺式蒎烷、对孟烷和长叶烯的饱和蒸气压。Antoine方程的三参数形式适用于松节油组分饱和蒸气压与温度的关联;对应态基团贡献法可应用于松节油组分饱和蒸气压数据的估算。     

气相色谱内标法测定正三十烷醇

植物生长调节剂正三十烷醇,对农作物的增产具有显著效果,因此正三十烷醇的生产越来越受到人们重视,与生产相适应的分析方法的研究,就显得甚为迫切。就目前所见资料来看,国内测定正三十烷醇均采用气相色谱归一化法,但由于制取正三十烷醇的方法和纯制措施各异,所要分析试样的纯度及共存组分亦不相同,且归一化法的应用需要有一定的先决条件,而某些三十烷醇产品不能满足归一法的先决条件,若仍用归一法测定,必然引起很大偏差。本文提出使用内标法以更广泛地适用于各种三十烷醇试样的直接测定。对内标物的选择进行了探讨,结果认为以邻苯二甲酸二正辛酯或癸二酸二异辛酯作为内标法测定正三十烷醇的内标物最适宜。     

真空下C_(10)与DMP体系汽液相平衡的研究

在7.36 k Pa下采用汽液相平衡釜测定了正癸烷-1-癸烯、正癸烷-邻苯二甲酸二甲酯(DMP)、1-癸烯-邻苯二甲酸二甲酯(DMP)和正癸烷-1-癸烯-邻苯二甲酸二甲酯的等压汽液相平衡数据。二元体系的实验数据通过了Herington面积法和热力学一致性校验,利用NRTL模型、Wilson模型和UNIQUAC模型对实验数据进行关联,得到相应的模型参数和关联偏差。实验结果表明:正癸烷-1-癸烯、正癸烷-邻苯二甲酸二甲酯和1-癸烯-邻苯二甲酸二甲酯二组分物系均不形成共沸物,模拟结果与实验值接近。最后用关联得到的模型参数预测了三元体系的汽液平衡数据。实验值与预测值吻合,可满足萃取精馏工艺设计的需要。     

食品接触材料及制品欧盟6种邻苯二甲酸酯特殊迁移量的测定

建立了气相色谱-质谱联用仪(GC-MS)快速测定食品接触材料及制品欧盟6种邻苯二甲酸酯类特殊迁移量的测定方法。采用GC-MS对邻苯二甲酸二正丁酯、邻苯二甲酸丁基苄基酯、邻苯二甲酸二(2-乙基)己酯、邻苯二甲酸二正辛酯、邻苯二甲酸二异壬酯、邻苯二甲酸二异癸酯6种邻苯二甲酸酯类的特殊迁移量进行研究,分别用两种不同的有机溶剂(乙醇和95%正己烷)作模拟液进行线性曲线测定,比较两种模拟液对曲线及方法的影响。研究发现乙醇模拟液的线性相关系数和灵敏度比95%正己烷模拟液高,重现性更好。该方法简单、可靠,指出了模拟液对迁移量测定的影响,有助于进一步完善邻苯二甲酸酯类迁移量的测定方法。     

多孔硝铵添加剂——十八烷胺含量测定

大连化工厂曾采用甲基橙作显色剂,分光光度法测定工业氯化铵中添加剂——十六烷胺含量。此法同样适用于测定多孔硝铵添加剂十八烷胺。十八烷胺用醋酸溶解,加热至60℃,混溶于硝铵溶液中。但此醋酸溶液常温下不溶于水。本方法用无水乙醇溶解十八烷胺醋酸溶液,甲基橙显色。用分光光度法测定时,标准曲线线性好,甲基橙与十八烷胺生成的黄色络合物组份稳定,克分子比     

近期实施的涂料系列标准

<正>1)GB/T 30646—2014《涂料中邻苯二甲酸酯含量的测定气相色谱/质谱联用法》。规定了采用气相色谱/质谱联用法测定涂料中邻苯二甲酸酯的含量。适用于涂料及涂料用原材料中各种邻苯二甲酸酯含量的测定。包括但不限于列举的邻苯二甲酸酯,如邻苯二甲酸二丁酯(DBP)、邻苯二甲酸丁苄酯(BBP)、邻苯二甲酸二异辛酯(DEHP)、邻苯二甲酸二辛酯(DNOP)、邻苯二甲酸二异壬酯(DINP)、邻苯二甲酸二异癸酯     

顺丁烯二酸酐在六氢化邻苯二甲酸二异丁酯,六氢化邻苯二？…

本文测定了顺酐在六氢化邻苯二甲酸二异丁酯、六氢化邻苯二甲酸二乙酯中的溶解度数据,并采用经验方程、l h方程、Wilson 方程对数据进行了关联.     

顺丁烯二酸酐在六氢化邻苯二甲酸二异丁酯、六氢化邻苯二甲酸二乙酯中溶解度的研究

本文测定了顺酐在六氢化邻苯二甲酸二异丁酯、六氢化邻苯二甲酸二乙酯中的溶解度数据,并采用经验方程、l h方程、Wilson 方程对数据进行了关联.     

环氧树脂含氯量分析的研究

本文采用沉淀滴定法测定环氧树脂氯含量,用邻苯二甲酸二甲酯代替剧毒的硝基苯作为AgCl沉淀的保护剂。同时,把AgNO_3标准溶液和NH_4CN标准溶液配得较稀,使得对含氯量极微的环氧树脂中氯值的分析更为准确。     

几种有机物极微蒸汽压数据的测定

几种有机物极微蒸汽压数据的测定梁英华＊＊马沛生＊＊＊阮永嗣（天津大学化学工程系，天津３０００７２）关键词极微蒸汽压Ｋｎｕｄｓｅｎ隙透物性测量１前言纯物质的蒸汽压是重要的化工基础数据，其测定方法通常分为静态法、沸点法、流动法、Ｌａｎｇｍｉｕｒ法和Ｋｎ...     

Isothermal vapor-liquid equilibria for the binary systems of ethylene glycol monopropyl ether with 2,2-dimethylbutane and 2,3-dimethylbutane

Isothermal vapor liquid equilibria for the binary system of ethylene glycol monopropyl ether with 2,2-dimehylbutane and 2,3-dimethylbutane were measured in a circulating water bath at 303.15, 318.15, and 333.15 K. The apparatus was in-house designed and manufactured. Consistency testing of the apparatus was done by comparing the measured vapor pressures to the calculated vapor pressures from the Antoine equation. The measured systems were correlated with a Peng-Robinson equation of state (PR) combined with Wong-Sandler mixing rule for the vapor phase, and NRTL, UNIQUAC, and Wilson activity coefficient models for the liquid phase. All the measured systems showed good agreement with the correlation results.     

环己烷、正丁醇、甲苯有关二元体系加压相平衡

以环已烷、正丁醇、甲苯为代表,进一步研究了烷烃、芳烃和低级醇在加压下的相平衡规律。测定了有关3个二元体系在101.3、304.0、506.6、709.3、911.9kPa下汽液平衡数据,对实测数据进行了统一关联,计算结果与实测值符合良好。环己烷-正丁醇、正丁醇-甲苯体系在所测压力下均形成最低共沸点。     

Measurement and Prediction of Vapor Pressure for H2O+CH3OH/C2H5OH+[BMIM][DBP] Ternary Working Fluids

The ionic liquid, 1-butyl-3-methylimidazolium dibutylphosphate ([BMIM][DBP]) was prepared and the vapor pressures of three set of binary solutions H2O(1)/CH3OH(1)/C2H5OH(1)+[BMIM][DBP](2) were measured...     

离子液体[BMIM][DBP]+水+甲醇/乙醇三元工质溶液蒸汽压的测量和预测(英文)

The ionic liquid, 1-butyl-3-methylimidazolium dibutylphosphate ([BMIM][DBP]) was prepared and the vapor pressures of three set of binary solutions H2O(1)/CH3OH(1)/C2H5OH(1) + [BMIM][DBP](2) were measured at different temperature and in the ILs mole fraction range from 0.1 to 0.6 with a static equilibrium apparatus. The measured vapor pressures were correlated with Non-Random Two Liquid (NRTL) activity coefficient model and the average relative deviations (ARD) between experimental and correlated vapor pressures for these binary solutions were 3.19%, 2.42% and 2.95%, respectively. Then, the vapor pressures of two set of ternary solutions H2O(1) + CH3OH(2)/C2H5OH(2) + [BMIM][DBP](3) were measured with an inclined boiling apparatus and further predicted with NRTL activity coefficient model based on the binary interaction parameters coming from fitting the vapor pressures of the binary solutions. The results indicated that the ternary solutions containing [BMIM][DBP] were shown a strong negative deviation from Raoult’s Law when the mole fraction of [BMIM][DBP] was larger than 0.2, which meant that ternary solutions could absorb the refrigerant vapors at the same or below solution temperature. Meanwhile, the average relative deviations between experimental and predicted vapor pressures for ternary solutions were 2.92% and 3.06%, respectively. Consequently, the NRTL active coefficient model used for non-electrolyte solutions was still valid for predicting vapor-liquid equilibrium of binary or ternary solutions containing ILs.     

Vapor–liquid equilibria for benzene/polybutadiene and cyclohexane/polybutadiene systems at 333, 355, and 373 K using gas chromatography

A perturbation chromatography apparatus has been designed and constructed for determining the vapor–liquid equilibrium between a two-component (solvent/helium) vapor phase and a two-component (polymer/solvent) liquid phase. The apparatus performed very well, giving reproducible and reliable results that agree with independent, previously reported studies. All tests of the equipment indicated that it was successful in meeting the conditions of low column pressure drop, small perturbations, and slow flow rate that are required for perturbation chromatography. Binary polymer/solvent data were obtained for polybutadiene (PBD)/benzene or polybutadiene/cyclohexane systems at solvent partial pressures to 40 kPa and for n-hexane at infinite dilution, all at the three temperatures of 333.15, 355.00, and 373.15 K. The experimental data for each system can be represented within experimental error by the Flory–Huggins polymer solution theory using a single binary interaction parameter that is independent of temperature and concentration.     

Vapor-liquid equilibria of carbon dioxide+n-propanol at elevated pressure

High-pressure vapor-liquid equilibrium data were measured for the binary mixtures of CO₂+n-propanol at various isotherms (313.15–343.15 K). The vapor and liquid compositions and pressures were measured in a circulation-type apparatus. To facilitate easy equilibration, both vapor and liquid phases were circulated separately in the experimental apparatus and the equilibrium composition was analyzed by an on-line gas chromatograph. The experimental data were compared with literature results and correlated with the Peng-Robinson (PR) equations of state using the Wong-Sandler mixing rules. Calculated results with PR EOS showed good agreement with our experimental data.     

High-pressure vapor-liquid equilibrium measurement for the binary mixtures of carbon dioxide+n-butanol

High-pressure vapor-liquid equilibrium data for the binary mixtures of CO₂+n-butanol were measured at various isotherms of (313.15, 323.15, 333.15 and 343.15) K, respectively. The equilibrium compositions of vapor and liquid phases and pressures at each temperature were measured in a circulation-type equilibrium apparatus. To facilitate easy equilibration, both vapor and liquid phases were circulated separately in the experimental apparatus and the equilibrium composition was analyzed by an on-line gas chromatograph. The experimental data were compared with literature results and correlated with the Peng-Robinson (PR) equations of state using the Wong-Sandler mixing rules. Calculated results with the PR EOS showed good agreement with our experimental data.     

Vapor pressure measurements on saturated biodiesel fuel esters by the concatenated gas saturation method

The purpose of this work was to determine vapor pressures for saturated biodiesel esters at the low-temperature end of their liquid range. A “concatenated” gas saturation apparatus capable of simultaneous measurements on 18 samples was used for measurements on methyl palmitate, ethyl palmitate, methyl stearate, ethyl stearate, and eicosane (C₂₀H₄₂) over the temperature range 323.15 K-343.15 K. Eicosane, a linear alkane with a well known vapor pressure curve (in the same range as the biodiesel esters), was included as a control compound. Importantly, the measured vapor pressures for eicosane are in excellent agreement with reference values, which is good evidence of the low uncertainty of the measurements on the biodiesel esters. Over this temperature range, the measured vapor pressure ranges were 0.145 Pa-1.11 Pa for methyl palmitate, 0.0687 Pa-0.616 Pa for ethyl palmitate, 0.0159 Pa-0.183 Pa for methyl stearate, and 0.00704 Pa-0.0912 Pa for ethyl stearate. The combined standard uncertainty in the vapor pressure measurements ranged from 8% to 15%.