更全的杂志信息网

Isobaric vapor–liquid equilibrium for ternary system of ethanol,ethyl propionate and para-xylene at 101.3 kPa☆

更新时间:2016-07-05

1.Introduction

Ethyl propionate,a kind of widely-used organic synthetic raw material and solvent,is applied in the field of pharmacy,antifungal agents,edibles,plasticizers,spice,dyes and even biomass[1,2].In industry,the traditional method of producing ethyl propionate is esterification of propanoic acid and ethanol with sulfuric acid as catalyst at 101.3 kPa,and then cut fraction from 369.15 K to 373.15 K is collected to gain pure product in distillation[3].However,the literature has reported that ethyl propionate and ethanol form an azeotrope at 101.3 kPa,which reduces the yield and purity of ethyl propionate[4].Therefore,it is a challenge for researcher to find out a way to improve the purity of ethyl propionate in the operation process.

物理教师应在课堂教学中利用各种条件,创设趣味环节激发学生的学习兴趣,激励学生自主学习的意识,产生自我学习的愿望。在实际教学中,物理课堂常见的小魔术、小游戏、小实验、趣味故事、有趣的图片等都是很好的激趣素材。

黑龙江省冰雪旅游业发展过程中存在的一个突出问题就是:冰雪旅游文化和冰雪旅游资源的融合不够深入,没有形成相互依存,相互促进的良好发展态势。这就要求科学合进地规划:首先,对冰雪文化进行宣扬,通过冰雪节、冰雕节、冰雪摄影等艺术活动对冰雪文化进行宣扬,让广大群众增强对冰雪旅游文化的认同感;其次,结合黑龙江省的发展历史和地方特色,推出一整套统一和谐的文化体系,使得冰雪旅游发展过程中的文化融合具有良好的形态;最后,政府做好顶层设计,引导黑龙江省冰雪旅游文化和冰雪旅游产业发展的深度融合,形成以文化为依托,冰雪为表现的一种持续性特色冰雪产业。

For azeotrope or similar boiling point system,extractive distillation is an effective and widely-used process to separate the mixture[5],and entrainer needs to be added into the original azeotrope system to increase the relative volatility of the azeotrope.There are several reported entrainers used for breaking binary azeotrope system,such as ionic liquid[6,7],dimethyl sulfoxide(DMSO)[8]and N,N-dimethyl formamide(DMF)[9].Because of high viscosity,ionic liquid is not widely used in extractive distillation and the extraction capacity of DMSO,and DMF is lower than para-xylene in the field of separating ethanol and ethyl propionate azeotropic system[10].Due to wide availability,low cost,high boiling point,less causticity,good thermal stability and miscibility with organic solvent[11],para-xylene has been reported as an effective additive in traditional extractive distillation,especially for the separation of mixture of ethylic acid and water[12–13].Zhang[14]selected para-xylene as solvent of methanol and trimethoxysilane in extractive distillation and found that para-xylene can break the azeotrope.However,up to now,the utilization of paraxylene as extraction agent to separate azeotropic system of ethanol+ethyl propionate has not been reported,which may be due to the lack of VLE data.The binary system VLE data,including ethanol(1)and ethyl propionate(2)and ethanol(1)and p-xylene(3),have been reported in the literature[4,15],but lack of VLE data of ethyl propionate(2)and p-xylene(3).In addition,the ternary system of ethanol(1)+ethyl propionate(2)+para-xylene(3)also has no VLE data reported openly.Since the lack of VLE data and its preferable prospect in extractive distillation process,measurement of isobaric VLE data for binary of ethyl propionate(2)+p-xylene(3)and ternary system of ethanol(1)+ethyl propionate(2)+para-xylene(3)is meaningful.

在经济新常态的背景下,作为国内经济重要组成部分的城市经济发展面临着前所未有的挑战和机遇,城市经济产业结构不合理、增长模式不科学等问题突出。依靠创新推动新旧动能转换和结构优化升级是经济新常态最核心的内容,新旧动能转换为城市经济发展提供了新的方向。

In this paper,the VLE data for binary system of ethyl propionate+para-xylene and ternary system of ethanol+ethyl propionate+para-xylene were determined at 101.3 kPa.The Wilson and UNIQUAC activity coefficient models were employed to correlate the binary VLE data and to obtain the interaction parameters,thus by use of the interaction parameters to predict the ternary VLE data.

2.Experimental

2.1.Chemicals

Three chemicals are ethanol,ethyl propionate and para-xylene,respectively,which are always miscible in all measurements.Their corresponding information ab out molecular formula,purity grade and source is listed in Table 1.The purity of all the chemicals was measured by gas chromatograph(GC)with a FID detector.All the reagents were used without further purification.

Table 1 Chemical reagents information

Gas chromatography.

Component name Molecular formula Analysis instrument Ethanol C2H6O Kewei,China >99.3% GCEthyl propionate C5H10O2 Acros,China ≥99.8% GCPara-xylene C8H10 Alfa,China >99.8% GCProvider Purity/wt%

2.2.Procedure

A circulation vapor–liquid equilibrium was used to measure the isobaric VLE data of binary and ternary system[16].The volume of the chamber was about 50 ml,of which 40 ml was taken up by liquid.A mercury thermometer below the liquid level was used to detect experimental temperature.The accuracy of the mercury thermometer is±0.1 K.The pressure was measured by a transducer(Digiquartz 2300A)connected to a Digiuartz 740 intelligent display unit(Paroscientific)whose accuracy is 0.01%.More details about the apparatus were referred to our previous papers[17,18].

About 40-ml liquid samples were fed into the chamber during each experiment,then heated at 101.3 kPa.The system was considered to reach equilibrium state when the temperature of the mercury thermometer was not change for about 1 h.Then,the samples of vapor and liquid phase were collected at the same time for analysis.To minimize the effect of sample amount on the equilibrium,three analyses were in parallel conducted and the amounts of the analyses were taken at 0.1 ml.

2.3.Analysis

Component analysis of the equilibrium vapor and liquid phase were conducted by GC2060 with a FID detector and SE-54 column(30 m×0.32 mm × 0.5 μm).High purity nitrogen was carrier gas at flow rate of 30 ml·min−1.The temperatures of injector,detector and oven were 473.15 K,473.15 K and 393.15 K,respectively.Standard solutions were applied to calibrate the GC,which were prepared gravimetrically by an electronic balance(FA2004N,uncertainty of±0.0001 g).In addition,calibration factor of pure substance was determined ahead of time.The final composition of each sample was determined upon the average of three analyses.

3.Results and Discussion

3.1.Experimental data

The VLE data for binary systems,including ethanol(1)+ethyl propionate(2)and ethanol(1)+para-xylene(3),are measured at 101.3 kPa.The activity coefficient(γi)is determined by the following equation[19–20]:

where xi and yi represent the liquid and vapor content of component i,respectively;obtained according to the extended Antoine equation,is the saturation vapor pressure of pure component i; is the liquid molar volume of pure liquid i and R is the gas constant;φi and are the fugacity coefficient of component i in the heterogeneous vapor phase and in homogeneous saturated vapor phase,separately.At low pressure,the gas phase can be regarded as ideal gas,andis approximately equal to 1.Meanwhile,φi and are equal to 1,respectively[21,22],so the activity coefficient equation can be simplified as follows:

The extended Antoine equation is defined by Eq.(3).

where C1,i−C7,i,T min and T max are pure component constants which are listed in Table 2.

Table 2 The constants C1,i-C7,i,T min and T max for the pure components

Taken from Aspen Plus physical properties databanks.

Component Ethanol Ethyl propionate Para-xylene C1 66.3962 98.7322 81.8122 C2 −7122.30 −8007.00 −7741.20 C3 0.0 0.0 0.0 C4 0.0 0.0 0.0 C5 −7.1424 −12.4770 −9.8693 C6 2.8853×10−6 9.0000×10−6 6.0770×10−6 C7 2.00 2.00 2.00 T min/K 159.05 199.25 286.41 T max/K 514.00 546.00 616.20

The Van Ness test method,a point consistency method put forward by Fredenslund et al.[27],was quoted to verify the reliability of experimental data[28].The criterion is expressed by the following eq.[29]:

Table 3 VLE data and activity coefficients for the binary system of ethanol(1)+ethyl propionate(2)at 101.3 kPa

The standard uncertainty is u(T)=0.1 K,u(P)=0.1 kPa,and u(x1)=u(y1)=0.004.

T/K x1 y1 γ1 γ2 351.41 1 1 1.0000 –351.52 0.9228 0.9224 0.9985 2.0166 351.63 0.8986 0.9017 0.9984 1.9379 351.72 0.8839 0.8907 0.9987 1.8753 351.90 0.8602 0.8765 1.0019 1.7472 352.41 0.6761 0.7723 1.1014 1.3659 353.80 0.5274 0.6959 1.2048 1.1901 354.80 0.4530 0.6550 1.2702 1.1264 355.61 0.4112 0.6260 1.2970 1.1033 356.80 0.3606 0.5872 1.3252 1.0760 358.32 0.2938 0.5540 1.4500 1.0000 360.64 0.2382 0.4902 1.4523 0.9805 363.23 0.1746 0.4247 1.5602 0.9368 367.20 0.0713 0.2807 2.1870 0.9143 372.50 0 0–1.0000

Table 4 VLE data and activity coefficients for the binary system of ethanol(1)+para-xylene(3)at 101.3 kPa

The standard uncertainty is u(T)=0.1 K,u(P)=0.1 kPa,and u(x1)=u(y1)=0.004.

T/K x1 y1 γ1 γ3 351.31 1 1 1.0000 –351.63 0.9390 0.9500 1.0054 5.6269 352.70 0.8780 0.9011 0.9780 5.3447 353.45 0.8140 0.9152 1.0404 2.9243 353.79 0.7500 0.9060 1.1034 2.3749 354.28 0.5412 0.8732 1.4463 1.7152 354.58 0.5733 0.8790 1.4556 1.5948 356.39 0.4071 0.8850 1.7974 1.1099 357.30 0.3391 0.8581 2.0211 1.1882 361.22 0.1862 0.8350 3.0963 0.9702 366.03 0.1134 0.7850 4.0234 0.9764 376.40 0.0720 0.6811 3.8267 0.9720 400.20 0.0130 0.2730 4.0512 1.0030 404.93 0.0060 0.1791 5.0288 0.9844 410.00 0 0–1.0000

Fig.1.T vs x1,y1 diagram for the ethanol(1)+ethyl propionate(2)system at 101.3 kPa(●,experimental vapor phase composition y1; ■,experimental liquid phase composition x1;—,literature liquid phase composition x1;…,literature vapor phase composition y1[4]).

Fig.2.T vs x1,y1 diagram for the ethanol(1)+para-xylene(3)system at 101.3 kPa(●,experimental vapor phase composition y1;■,experimental liquid phase composition x1;—,literature liquid phase composition x1;…,literature vapor phase composition y1[15]).

Table 5 The mean absolute and relative deviations of vapor phase mole fraction and equilibrium temperature for system of ethanol(1)+ethyl propionate(2)and ethanol(1)+para-xylene(3)

ΔT=where n is the number of data points,T is the system temperature. Δy=where n is the number of data points,y is the composition of vapor phase. δT=where n is the number of data points,T is the system temperature. δy=where n is the number of data points,y is the composition of vapor phase.

?

F term defined by Eq.(6)

Table 6 VLE data and activity coefficients for the binary system of ethyl propionate(2)+paraxylene(3)at 101.3 kPa

The standard uncertainty is u(T)=0.1 K,u(P)=0.1 kPa,and u(x1)=u(y1)=0.004.

T/K x2 y2 γ2 γ3 372.25 1 1 1.0000 –374.45 0.9222 0.9780 0.9980 0.8559 376.35 0.8383 0.9498 1.0065 0.8822 379.72 0.7069 0.8932 1.0151 0.9275 382.25 0.6340 0.8540 1.0049 0.9363 383.30 0.5897 0.8245 1.0119 0.9711 387.14 0.4806 0.7470 1.0083 0.9809 390.01 0.3994 0.6795 1.0187 0.9843 393.71 0.3245 0.5945 0.9913 0.9909 397.52 0.2414 0.4862 0.9843 0.9999 399.34 0.2051 0.4284 0.9730 1.0073 403.58 0.1268 0.2844 0.9365 1.0180 407.82 0.0580 0.1390 0.8992 1.0099 411.65 0 0–1.0000

In extractive distillation,relative volatility is an important factor to evaluate the performance of extraction agent[24,25].When the relative volatility is greater than 1,the two components can be separated by distillation[21].Table 7 shows that the minimum relative volatility of ethyl alcohol to ethyl propionate is 3.4141 after para-xylene was added,which demonstrates the complete separation of ethanol and ethyl propionate can be achieved by extractive distillation.

Table 7 VLE data for the ternary system of ethanol(1)+ethylpropionate(2)+para-xylene(3)at 101.3 kPa

The standard uncertainty is u(T)=0.1 K,u(P)=0.1 kPa,and u(x1)=u(y1)=0.004.

?

3.2.Data regression

The acquired VLEdata was correlated with the Wilson and UNIQUAC models by Aspen Plus to gain the interaction parameters of the ternary system of ethanol(1)+ethyl propionate(2)+para-xylene(3)[26].To obtain the minimizing maximum likelihood objective function,the binary VLE data was regressed,which was described as:

2.3.1 药物-化合物-靶点网络(H-C-T) 根据钩藤散中10种中药、64个活性化合物与473个靶点之间的相互作用关系构建了H-C-T网络图(图1)。该网络由535个节点(nodes)和2 874条边(edges)组成,位于外圈的靶点与至少2个化合物连接,内圈的靶点则与更多的化合物相连,平均每个节点都与7.87个相邻节点存在联系。64个活性化合物中,33个化合物都具有20个以上的作用靶点,提示这些成分可能在钩藤散药效中起主要作用。

To investigate the effect of with and with out para-xylene on the system of ethanol(1)+ethyl propionate(2),isobaric VLE data of the binary system are presented in Fig.5.As shown in Fig.5,one can note that the azeotropic phenomenon is disappeared when the mole ratio of para-xylene and binary system of ethanol and ethyl propionate is 1:1.The reason why para-xylene can change the relative volatility of azeotrope in our work may be explained by the fact that attraction of para-xylene for alcohols is larger than that for esters[34],which demonstrates that para-xylene is a potential extraction agent for this system.

The correlated parameters and the root-mean-square deviations(RMSD)of temperature and vapor phase mole fraction are given in Table 8.Meanwhile,the contradistinction between experimental data and calculated data is presented in Fig.3,revealing that all the values calculated by the two models fit well with the experimental data.

Table 8 Correlated parameters and RMSD for systems of ethanol(1)+ethyl propionate(2),ethanol(1)+para-xylene(3)and ethyl propionate(2)+para-xylene(3)

σT σyi= Wilson,ln Aij=aij+bij/T. UNIQUAC,τij=exp(aij+bij/T).

?

3.3.Consistency tests of experimental data

The isobaric VLE data for ethanol(1)+ethyl propionate(2)and ethanol(1)+para-xylene(3)are presented in Tables 3 and 4.To check the stability of experimental device,the experimental VLE data were compared with literature data[4,15],which are shown in Figs.1and 2.Meanwhile,the absolute and relative errors in temperature and vapor phase mole fraction are listed in Table 5.Obviously,the experiment results show a good agreement with literature data.Therefore,it is confirmed that the experimental device and operation process are reliable.

Fig.3.T vs x2,y2 diagram for the ethyl propionate(2)+para-xylene(3)system at 101.3 kPa(■,□ experimental data;…,calculated data with Wilson model;—,calculated data with UNIQUAC model).

where n is the number of experimental data points;the superscript exp represents experimental data;the superscript cal represents values determined by Wilson and UNIQUAC models.If the value of Δyi is lower than 1,the VLE data can be confirmed to be thermodynamically consistent.Table 9 shows the results of binary and ternary systems applying the above expression,revealing that all the experimental data obtained in this work is thermodynamically consistent.

Table 9 The results of thermodynamic consistency test of Van Ness method for the binary and ternary systems

Systems Wilson UNIQUAC Results Ethyl propionate(2)+para-xylene(3)△y1 0.480 0.358 passed△y2 0.480 0.358 passed Ethanol(1)+ethyl propionate(2)+para-xylene(3)△y1 0.311 0.438 passed△y2 0.289 0.280 passed△y3 0.344 0.319 passed

3.4.Data prediction

Isobaric VLE data of the binary system ethyl propionate+para-xylene and ternary system of ethanol+ethyl propionate+para-xylene were determined at 101.3 kPa.The thermodynamic consistency test indicated that both binary and ternary VLE data passed the Van Ness test.Wilson and UNIQUAC activity coefficient models were used to correlate experimental data to obtain binary interaction parameters.The comparison between the experimental data and VLE data predicted by the two models reveals that predicted data fits well with experimental date.The azeotropic phenomenon vanishes when the mole ratio of the azeotrope and para-xylene is 1:1.The experimental and prediction results imply that para-xylene is an available additive to separate the binary system of ethanol and ethyl propionate in extractive distillation.

Table 10 Maximum and mean absolute deviations of equilibrium temperature and vapor-phase mole fraction for system of ethanol(1)+ethyl propionate(2)+para-xylene(3)

Δmax T=max ➁ Δmax yi=max ΔT= Δyi=

Model Maximum absolute deviations Mean absolute deviations Δmax T/K Δmax y1 Δmax y2 Δmax y3 ΔT/K Δy1 Δy2 Δy3➃Wilson 0.48 0.009 0.007 0.008 0.24 0.003 0.003 0.003 UNIQUAC 0.79 0.010 0.009 0.007 0.36 0.004 0.003 0.003

Fig.4.Residue curves of the ternary system ethanol(1)+ethyl propionate(2)+paraxylene(3)(■,experimental liquid phase composition;○,experimental vapor phase composition;—,pairs of VLE data;…,residue curves).

Fig.5.x1 vs y1 diagram for the comparison of VLE behavior of binary system ethanol(1)+ethyl propionate(2)with and without para-xylene(▲,experimental VLE data without para-xylene;●,experimental VLE data with para-xylene).

where σ is the standard deviation of the corresponding parameters.The standard deviations of pressure σP,temperature σT,liquid composition σx and vapor composition σy used in this VLE data correlation are 0.1013 kPa,0.1 K,0.001 and 0.001,respectively.

4.Conclusions

The ternary VLE data of ethanol(1)+ethyl propionate(2)+para-xylene(3)were predicted with the correlated binary parameters which were obtained by Wilson and UNIQUAC models.The maximum and mean absolute deviations of equilibrium temperature and vapor mole fraction for each system are listed in Table 10.The results illustrate that the predicted data agrees well with the experimental data,which indicate that both Wilson and UNIQUAC models can predict the experimental data accurately.A vapor–liquid residue curve map is constructed by residue in a simple distillation in time,which is a geometric analysis method for distillation system to explain the composition of an azeotropic system[30,31].In order to further check ternary system VLE data,the residue curve of the ternary system was predictedby UNIQUAC model using correlated binary parameters,which was shown in Fig.4.The connecting lines of the vapor phase points and liquid phase points are tangent very well with the residue curves atthe liquid phase points,indicating that the prediction data are coincident with experimental data[32,33].

Nomenclature

高校内部审计部门很少从事内部控制检查工作,极少对内部控制建设及执行过程进行有效监督,专业性的内部监督检查机制缺乏。同时,财政部仅要求高校进行内部控制建设和自我评价,缺乏必要的外部监督检查、绩效考评机制。

aij,aji,bij,bji the correlated parameters of Wilson and UNIQUAC models

C1,i−C7,i pure component constants

The isobaric VLEdata for the binary system of ethyl propionate(2)+para-xylene(3)and ternary system of ethanol(1)+ethyl propionate(2)+para-xylene(3)were obtained at 101.3 kPa,which are listed in Tables 6 and 7.For the ternary system,para-xylene was added into the still at a constant content(50 mol%).In Table 7,x′and y′denote the mole fraction of corresponding liquid and vapor phase on the basis of free para-xylene,respectively.The relative volatility of ethanol to ethyl propionate is determined by the following equation[23]:

n the number of experimental data points

P the total pressure,kPa

saturated vapor pressure of pure component i,kPa

R universal gas constant

A0((uh,i,Bh,i), (v,s)) + A1((uh,i, Bh,i),(uh,i,Bh,i),(v,s)) - b((v,s),ph,i)+b((uh,i, Bh,i),q) = (F,(v,s)), ∀((v,s),q)∈Xh×Wh×Qh。

T tempreture,K

ΔT mean absolute deviations of equilibrium temperature

δT relative deviations of equilibrium temperature

根据因子分析结果,对各公共因子进行经济含义界定,将23个指标重新划分为7个指标。其中投入角度的指标为运营投入、管理投入、固定资产投入、技术投入、服务开展5个评价指标;产出角度的指标为经营效果、服务评价效果指标。进一步,将效果导向的绩效评价指标确定为经营效果、服务评价效果两个评价维度,从而确定医养结合养老服务绩效评价指标体系(见表3)。

u standard uncertainty

在预防方面,大家都会结合养殖场实际情况或多或少使用消毒药进行杀毒灭菌,切断传播途径,保护养殖畜禽。特别是常见疫病高发季节,流行地区,新病流行阶段(如非洲猪瘟),日常消毒工作更加凸显重要性。但是大家对消毒药的使用真的用对了吗?下面给大家介绍一下常用消毒药的性质及正确使用方法。

liquid molar volume of pure liquid i,m3·mol−1

Δy mean absolute deviations of vapor-phase mole fraction

xi,yi liquid and vapor content of component i,respectively

1.1 病毒及药品 CVB3(Nancy株)由武汉大学医学院病毒研究所提供,在HeLa细胞上传代、分装、冻存,测得半数组织感染量为10-6TCID 50/mL。PC由美国Sigma-aldrich公司生产,货号52468。

δy mean relative deviations of vapor phase mole fraction

σy root-mean-square deviations of vapor phase mole fraction

α12 relative volatility of ethanol to ethyl propionate

宗主国通过向殖民地强行输出法律规则的方式,实现了宗主国与殖民地“国内法”层面的法律趋同,从而使两地的社会秩序得以在法律的框架下维持。

1.把课堂交给学生,让课堂变成学堂,最大限度地开放课堂,使课堂开放化,针对疑难问题,师生相互切磋,相互辩论,使问题水到渠成,同时,教师要鼓励学生敢于创新,不拘于教材,充分发挥自己的潜能。

γ liquid activity coefficient

2)自动化控制系统。地面控制系统均为撬装OCS控制器独立运行,地面压力信号与现场井口BB井控系统进行联锁。当地面撬装设备压力高于设定值时自动关井,具有紧急关井联锁功能,从而确保运行安全可靠。地面各撬装采用就地控制与中控室控制相融合,撬块上的各重要工艺参数的显示、控制、报警以及各相关逻辑联锁保护控制均由中控室DCS+PC系统进行远程监控。

σ the standard deviation

fugacity coefficient of component i in the mixture vapor phase and pure saturated vapor

References

[1]D.C.Rennard,P.J.Dauenhauer,S.A.Tupy,L.D.Schmidt,Autothermal catalytic partial oxidation of bio-oil functional groups:esters and acids,Energy Fuels 22(2)(2008)1318–1327.

[2]S.S.Kanwar,H.K.Verma,R.K.Kaushal,R.Gupta,S.S.Chimni,Y.Kumar,Effect of solvents and kinetic parameters on synthesis of ethyl propionate catalysed by poly(AAc-co-HPMA-cl-MBAm)-matrix-immobilized lipase of Pseudomonas aeruginosa BTS-2,World J.Microbiol.Biotechnol.21(6-7)(2005)1037–1044.

[3]S.J.Lin,Y.Z.Sun,Catalytic synthesis of ethyl propionate with p-toluene sulfonic acid,J.Beijing Inst.Petrochem.Technol.13(1)(2005)49–52(in Chinese).

[4]J.Ortega,J.Ocon,J.Peña,C.D.Alfonso,M.Paz-Andrade,J.Fernandez,Vapor-liquid equilibrium of the binary mixtures C n H2n+1(OH)(n=2,3,4)+propyl ethanoate and+ethyl propanoate,Can.J.Chem.Eng.65(1987)982–990.

[5]W.F.Shen,H.Benyounes,V.Gerbaud,Extractive distillation:recent advances in operation strategies,Rev.Chem.Eng.31(1)(2015)13–26.

[6]Z.Y.Zhu,Y.S.Ri,M.Li,H.Jia,Y.K.Wang,Extractive distillation forethanoldehydration using imidazolium-based ionic liquids as solvents,Chem.Eng.Process.109(2016)190–198.

[7]Y.Xiao,P.Bai,Z.K.Jiang,Vapour-liquid equilibrium for systems containing ionic liquids,Asian J.Chem.24(9)(2012)3775–3780.

[8]H.Ding,Y.J.Gao,J.Q.Li,H.Zhou,S.J.Liu,X.Han,Vapor–liquid equilibria for ternary mixtures of isopropyl alcohol,isopropyl acetate,and DMSO at 101.3 kPa,J.Chem.Eng.Data 61(9)(2017)3013–3019.

[9]Q.Y.Wang,B.R.Yu,C.J.Xu,Design and control of distillation system for methylal/methanol separation.Part 1:extractive distillation using dmf as an entrainer,Ind.Eng.Chem.Res.51(3)(2012)1281–1292.

[10]H.Zhou,H.Ding,J.B.Quan,Extractive distillation of ethanol-ethyl propionate azeotrope with para-xylene,Chem.Ind.Eng.34(2017)25–34(in Chinese).

[11]K.Xu,Handbook ofFine Organic ChemicalRaw Materials and Intermediates,Chemical Industry Press,Beijing,1998 34–36(in Chinese).

[12]M.Corbetta,C.Pirola,F.Galli,F.Manenti,Robustoptimization of the heteroextractive distillation column for the purification of water/acetic acid mixtures using p-xylene as entrainer,Comput.Chem.Eng.95(2016)161–169.

[13]C.Pirola,F.Galli,F.Manenti,M.Corbetta,C.L.Bianchi,Simulation and related experimental validation of acetic acid/water distillation using p-xylene as entrainer,Ind.Eng.Chem.Res.53(46)(2014)18063–18070.

[14]H.Zhang,H.Xu,X.Dai,H.Yu,Q.Ye,Simulation and optimization of extractive distillation for separating methanol and trimethoxysilane,Mod.Chem.Ind.35(1)(2015)163–167(in Chinese).

[15]M.D.Sanchez-Russinyol,A.Aucejo,S.Loras,Isobaric vapor-liquid equilibria for binary and ternary mixtures of ethanol,methylcyclohexane,and p-xylene,J.Chem.Eng.Data 49(5)(2004)1258–1262.

[16]Q.S.Li,F.Y.Xing,Z.G.Lei,B.H.Wang,Q.L.Chang,Isobaric vapor-liquid equilibrium for isopropanol+water+1-ethyl-3-methylimidazolium tetra fluoroborate,J.Chem.Eng.Data 53(1)(2008)275–279.

[17]J.Hou,S.M.Xu,H.Ding,T.Sun,Isobaric vapor–liquid equilibrium of the mixture of methyl palmitate and methyl stearate at 0.1 kPa,1 kPa,5 kPa,and 10 kPa,J.Chem.Eng.Data 57(10)(2012)2632–2639.

[18]G.W.Tang,H.Ding,J.Hou,S.M.Xu,Isobaric vapor–liquid equilibrium forbinary system of ethyl myristate+ethyl palmitate at 0.5,1.0 and 1.5 kPa,Fluid Phase Equilib.347(2013)8–14.

[19]J.M.Smith,H.C.Van Ness,M.M.Abbott,Introduction to Chemical Engineering Thermodynamics,McGraw-Hill Education,Boston,New York,2005 338-369,430-442,545-546.

[20]J.M.Prausnitz,R.N.Lichtenthaler,E.G.D.Azevedo,Molecular Thermodynamics of Fluid-Phase Equilibria,Vols.1–22,Pearson Education,NJ,1998 42–45(in Chinese).

[21]T.E.Tan,M.Dou,M.H.Zhou,Principles of Chemical Engineering,3rd.ed.Vols.74–75,Chemical Industry Press,Beijing,2006 157–158(in Chinese).

[22]X.D.Zhang,D.P.Hu,Z.C.Zhao,Measurement and prediction of vapor pressure for H2O+CH3OH/C2H5OH+[BMIM][DBP]ternary working fluids,Chin.J.Chem.Eng.21(8)(2013)886–893.

[23]M.T.G.Jongmans,J.I.W.Maassen,A.J.Luijks,B.Schuur,A.B.de Haan,Isobaric lowpressure vapor–liquid equilibrium data for ethyl benzene+styrene+sulfolane and the three constituent binary systems,J.Chem.Eng.Data 56(9)(2011)3510–3517.

[24]Z.G.Lei,C.Y.Li,B.H.Chen,Behaviour of tributylamine as entrainer for the separation of water and acetic acid with reactive extractive distillation,Chin.J.Chem.Eng.11(5)(2003)515–519.

[25]D.B.Kaymak,W.L.Luyben,O.J.Smith,Effect of relative volatility on the quantitative comparison of reactive distillation and conventional multi-unit systems,Ind.Eng.Chem.Res.43(12)(2004)3151–3162.

[26]Aspentech,Aspen Property System:Physical Property Systems Methods and Models 11.1.,Aspen Technology,Inc.,Burlington,2001 20–33.

[27]A.Fredenslund,J.Gmehling,P.Rasmussen,Vapor-liquid Equilibria Using UNIFAC:A Group Contribution Method,Elsevier,Amsterdam,1977.

[28]P.L.Jackson,R.A.Wilsak,Thermodynamic consistency tests based on the Gibbs-Duhem equation applied to isothermal,binary vapor-liquid equilibrium data:data evaluation and model testing,Fluid Phase Equilib.103(1995)155–197.

[29]J.W.Kang,V.Diky,R.D.Chirico,J.W.Magee,C.D.Muzny,A.F.Kazakov,K.Kroenlein,M.Frenkel,Algorithmic framework for quality assessment of phase equilibrium data,J.Chem.Eng.Data 59(7)(2014)2283–2293.

[30]R.E.Rooks,V.Julka,M.F.Doherty,M.F.Malone,Structure of distillation regions for multicomponent azeotropic mixtures,AIChE J.44(6)(1998)1382–1391.

[31]S.Widagdo,W.D.Seider,Azeotropic distillation,AIChE J.42(1)(1996)96–130.

[32]X.M.Zhang,Y.X.Liu,C.G.Jian,F.Wei,H.P.Liu,Experimental isobaric vapor-liquid equilibrium for ternary system of sec-butyl alcohol+sec-butyl acetate+N,N-dimethyl formamide at 101.3 kPa,Fluid Phase Equilib.383(2014)5–10.

[33]X.M.Zhang,H.P.Liu,Y.X.Liu,C.G.Jian,W.Wang,Experimental isobaric vapor-liquid equilibrium for the binary and ternary systems with methanol,methyl acetate and dimethyl sulfoxide at 101.3 kPa,Fluid Phase Equilib.408(2016)52–57.

[34]A.Fredenslund,J.Gmehling,P.Rasmussen,Vapor–liquid Equilibria Using UNIFAC:A Group Contribution Method,Vols.68–84,Elsevier,Amsterdam,1977 150–155.

Zhongpeng Xing,Yujie Gao,Hui Ding,Xianqin Wang,Lujun Li,Hang Zhou
《Chinese Journal of Chemical Engineering》2018年第3期文献

服务严谨可靠 7×14小时在线支持 支持宝特邀商家 不满意退款

本站非杂志社官网,上千家国家级期刊、省级期刊、北大核心、南大核心、专业的职称论文发表网站。
职称论文发表、杂志论文发表、期刊征稿、期刊投稿,论文发表指导正规机构。是您首选最可靠,最快速的期刊论文发表网站。
免责声明:本网站部分资源、信息来源于网络,完全免费共享,仅供学习和研究使用,版权和著作权归原作者所有
如有不愿意被转载的情况,请通知我们删除已转载的信息 粤ICP备2023046998号