hydrates of hydrocarbons 151-200页
(完整版)油气储运专业英语(英汉互译)
The complex nature of wellstreams is responsible for the complex processing of the produced fluids (gas, oil ，water,and solids).The hydrocarbon portion must be separated into products that can be stored and/or transported.The nonhydrocarbon contaminants must be removed as much as feasible to meet storage, transport, reinjection, and disposal specifications. Ultimate disposal of the various waste streams depends on factors such as the location of the field and the applicable environmental regulations. The overriding criterion for product selection, construction, and operation decisions is economics.油气井井流的复杂性质，决定了所产流体(气、油、水和固体)的加工十分复杂。
必须分出井流中的烃类，使之成为能储存和/或能输送的各种产品;必须尽可能地脱除井流中的非烃杂质，以满足储存、输送、回注和排放的规范。
各类废弃物的最终处置取决于各种因素，如油气田所处地域和所采用的环保规定等。
经济性是决定油气田产品设计、建筑和操作决策的最重要准则。
Fig. 1-1 is a comprehensive picture of the individual unit operations carried out in field processing. All the various modules shown will not all be present in every system. Furthermore, the modules used in a given application may not be arranged in the exact sequence shown, although the sequence is ，in general, correct. The selection and sequencing of modules is determined during the design phase of field development.图1-1表示在矿场进行的各种单元操作的综合图。
水合物抑制剂聚N-甲氧基-N-甲基丙烯酰胺的研究
第43卷第 10 期2023年10月Vol.43 No.10Oct.，2023 工业水处理Industrial Water TreatmentDOI：10.19965/ki.iwt.2022-1078水合物抑制剂聚N-甲氧基-N-甲基丙烯酰胺的研究史言康1，李志元2，刘丽强3，滕厚开3，徐慧2，王素芳2，赵清顺4，韩恩山1（1.河北工业大学化工学院，天津 300401；2.中海油（天津）油田化工有限公司，天津 300452；3.中海油天津化工研究设计院有限公司，天津 300131；4.北京中天兰清环境科技有限公司，北京 100102）[ 摘要]深海油田开采过程由于存在低温高压条件，管道中会因形成水合物而造成堵塞。
设计并合成了新型水合抑制剂聚N-甲氧基-N-甲基丙烯酰胺（polyMEHAMs），以实现延缓水合物形成的目的。
结果表明，polyMEHAMs在相对分子质量达到2.51×106（polyMEHAMs-6）时，具有明显的抑制水合物效果，其在去离子水中的浊点为63 ℃；在烷烃水体积比为1∶4、polyMEHAMs-6抑制剂投加量为2 500 mg/L、初始压力为4.0 MPa条件下，过冷度为10.8 ℃和12.3 ℃时polyMEHAMs-6抑制水合物的诱导时间分别为10.7 h和13.7 h，其在过冷度12.3 ℃下对水合物的抑制性能优于10.8 ℃。
机理探索实验表明，疏水性—OCH3基团与酰胺O==C—NHCH3基团形成的O==C—NCH3—OCH3结构具有延缓水合物形成的能力。
［关键词］天然气水合物；水合物抑制剂；丙烯酰胺聚合物［中图分类号］X703 ［文献标识码］A ［文章编号］1005-829X（2023）10-0157-06Study on poly-N-methoxy-N-methylacrylamide as hydrate inhibitor SHI Yankang1，LI Zhiyuan2，LIU Liqiang3，TENG Houkai3，XU Hui2，WANG Sufang2，ZHAO Qingshun4，HAN Enshan1（1.College of Chemical Engineering，Hebei University of Technology，Tianjin 300401，China；OOC（Tianjin） Oilfield Chemical Co.，L td.，T ianjin 300452，China；3.CenerTech TianjinChemical Research & Design Institute Co.，L td.，T ianjin 300131，China；4.Beijing ZhongtianLanqing Environment Technology Co.，L td.，B eijing 100102，China；）Abstract：In the process of deep-sea oil field exploitation，due to the existence of low-temperature and high-pressure conditions，hydrates can form in the pipeline，causing blockage. A new type of hydration inhibitor poly（N-methoxy-N-methylacrylamide）（polyMEHAMs）was designed and synthesized to delay the formation of hydrates. The results showed that when the polyMEHAMs had a relative molecular weight of 2.51×106（polyMEHAMs-6），it had a signifi⁃cant inhibitory effect on hydrates，with a cloud point of 63 ℃ in deionized water. Under the conditions of alkane and water volume ratio of 1∶4，polyMEHAMs-6 inhibitor dosage of 2 500 mg/L and initial pressure of 4.0 MPa，the induction time of polyMEHAMs-6 inhibiting hydrates at subcooling of 10.8 ℃ and 12.3 ℃ were 10.7 hours and 13.7 hours，and the inhibition performance of inhibitors at subcooling of 12.3 ℃ was better than that at sub⁃cooling of 10.8 ℃. The mechanism exploration experiment showed that the hydrophobic —OCH3 group and the amide O==C—NHCH3 group formed O==C—NCH3—OCH3 structure，which had the ability to delay hydrates formation.Key words：natural gas hydrate；hydrate inhibitor；acrylamide polymer天然气水合物是由各种低沸点烃类分子（如甲烷、CO2等）在高压低温及水分子作用下形成的笼型化合物〔1〕。
镁铝水滑石催化剂英文
镁铝水滑石催化剂英文Magnesium-Aluminum Layered Double Hydroxide (LDH) CatalystsMagnesium-Aluminum Layered Double Hydroxides (LDHs) have emerged as promising catalysts due to their unique structure and properties. These materials are composed of positively charged hydroxide layers analogous to brucite (Mg(OH)2), which are intercalated with various anions or anion clusters. The versatility of LDHs lies in their ability to incorporate a wide range of anions into their layers, making them suitable for various catalytic applications.The structure of LDH consists of an alternating stacking of brucite-like layers and interlayer spacing that accommodates anions. This structure allows LDHs to exhibit tunable physicochemical properties, such as surface area, pore volume, and acid-base properties, which can be tailored to optimize catalytic performance.LDHs are often used as catalysts or catalytic supports due to their high surface area, excellent thermal stability, and ability to resist sintering at high temperatures. They can be activated by incorporating transition metals or transition metal oxides into their layers, which can significantly enhance their catalytic activity.One of the primary applications of magnesium-aluminum LDH catalysts is in the catalytic reforming of refinery by-products. LDHs can effectively catalyze the cracking of heavy hydrocarbons, facilitating the production of valuable light hydrocarbons, such as gasoline and jet fuel. This catalytic process is achieved under conditions of moderate temperatures and pressures, making it economically viable.Additionally, LDHs have been studied for their role in the catalytic hydrolysis of cellulose, a major component of biomass. The catalytic hydrolysis of cellulose represents a significant step towards the production of sustainable biofuels. LDHs areconsidered potential catalysts in this process due to their ability to facilitate cellulose breakdown through the activation of acid sites.The synthesis of magnesium-aluminum LDH catalysts can be achieved through various methods, including coprecipitation, hydrothermal synthesis, and sol-gel methods. The choice of synthesis method can significantly influence the physicochemical properties of the resulting LDH catalyst.In conclusion, magnesium-aluminum LDH catalysts are versatile materials with significant potential for industrial applications, particularly in the refining of fuels and the production of biofuels. The ability to tailor the properties of LDHs through their synthesis and modification offers an excellent opportunity for developing efficient and environmentally friendly catalytic processes. Future research is expected to explore further the potential of LDHs in catalytic applications and to develop new synthesis strategies to enhance their catalyticperformance.。
化学专业英语(化学专业名词)
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• 3） Anions containing hydrogen（含氢 阴离子）：hydrogen + 去掉氢的离子名 称 • • 例：HCO3-：hydrogen carbonate ion
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3. Names of Acids（酸的命名）：酸根 离子中非氧元素名称的词干 + -ic acid
4
2） Polyatomic Cations（多原子阳离子）： 原子团名称 + ion
例: Na+：sodium ion；Ag+：silver ion； Ca2+：calcium ion；Al3+：aluminum ion； Fe+：iron（I）ion；Fe2+：iron（II）ion；Fe3+： iron（III）ion； 例：
* 如果某元素能形成一种以上的含氧酸，则按以 下规则：
a. 高（过）* 酸：per- + 酸根离子中非氧元素名 称的词干 + -ic acid
b. * 酸：酸根离子中非氧元素名称的词干 + - ic acid
c. 亚 * 酸：酸根离子中非氧元素名称的词干 + ous acid d. 次 * 酸：hypo- + 酸根离子中非氧元素名称的 词干 + -ous acid
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5. Names of Salts（盐的命名）：
不带“ion”的阳离子名称 + 不带“ion” 的阴离子名称
* 阳 离 子 的 电 荷 数 用 斯 托 克 数 字 （ Stock number）来表示（只形成一种阳离子的元素 不必用）. 例：CuCl：copper（I）chloride； CuCl2：copper（II）chloride； CuSO4：copper（II）sulfate； KClO4：potassium perchlorate
油气储运工程专业英语-复习资料
中国石油大学（北京）远程教育学院期末考试卷油气储运工程英语》复习资料答案一、填空1、 ___ are solid compounds that form as crystals and resemble snow in appearance考生答案： Hydrates2、 Natural gas with H2S or other sulfur ___ present is called “ _____考生答案： compounds3、 Most oil and gas pipelines fall into one of three groups: ___ , ______ , or _____ .考生答案： gathering trunk/transmission/distribution4、 All ____ t anks have a cover that floats on the surface of the liquid考生答案： floating-roof5、 Natural gas ____ is highly dependent on weather.考生答案： demand6、 Energy is supplied to the liquid through the pump by the pump ' sd river -anor an electric _____ .考生答案： engine/urbine/motor7、 To form a stable emulsion of crude oil and _____________ ,an emulsifying _______ must考生答案： water/agent8、 Most pipelines are coated on the exterior to prevent ____ .考生答案： corrosion9、 Natural gas with only CO2 is called “ ________ g as ”.考生答案： sweet10、 The hydrocarbons contain only ___ and _____ .考生答案： carbon / hydrogen11、 Centrifugal pump consists of an ___ and a ____ .考生答案： impeller/ casing12、 The distance between compressors varies, depending on the _____________ of gas,and other factors.考生答案： volume/ size课程编号：gas a _____ be present. the line ______13、In designing a pipeline system, the ____________ of pump stations must be determined as wellas ____ of individual pumps within each station.考生答案：location/size14、The type of information gathered by smart pigs includes the pipeline _________________ , curvature, bends, temperature and _____ , as well as ____ or metal loss.考生答案：diameter pressure/corrosion15、____ is short for American Petroleum Institute.考生答案：API16、The two categories of floating-roof tanks are _______________ floating roof and ____________ f loating roof.考生答案：external/internal17、Gas is moved through a gas pipeline by ___ .考生答案：compressors18、____ i s always necessary for hydrate formation.考生答案：Water19、The pressure in the pipeline decreases due to ___ and ______ losses.考生答案：friction /elevation20、Most pipelines are tested with water ( ____________ testing) either in sections or over theentire _____ .考生答案：hydrostati/length21、The position of ____ and the extent of mixing can be monitored at points along theline by measuring the ____ of the fluid in the line.考生答案：batch /density22、All pipelines are tested for ____________ following ____ before the line is put into service.考生答案：leaks/ construction23、Well fluids are often a complex mixture of ___ ,gas,and some ______ ．考生答案：liquid hydrocarbons <mpuritie24、The individual phases (gas, ________ , ______ , and solids) should be separated from each other as early as practical.考生答案：liquid hydrocarbon /liquid water25、Launcher (at the end of a station to launch _______________ t o downstream station) is requiredat the _____ of the section.考生答案：pig/ upstream26、An emulsion is a combination of __________ ,or liquids that do not mix together under normal conditions ．27、Products pipeline often must operate at ______________ pressure than crude pipelines becausethe material being transported is _____ than crude.考生答案：higher lighter28、Shipping emulsified oil wastes costly ___ occupied by valueless water.考生答案：transportation capacities29、When no physical barrier is used between different products in products pipeline,the _____ of the two materials maintains the separation.考生答案：difference in density30、Reciprocating compressor unit includes ____ and _____ .考生答案：compressor driver compressor31、Two general types of line pipe are manufactured: ____ and _____ .考生答案：seamless welded32、In pumping any liquid, the goal is to add energy to the liquid to cause it to movethrough a pipeline by overcoming the _____ and changes in _____ .考生答案：friction elevation33、The ____ of the substance stored determines the shape and type of tank.考生答案：vapor pressure34、Standing storage losses result from evaporative losses through ___________________ ,______ , and/or deck seam.考生答案：rim seals deck fitting35、There is 8~12in gap between the __________ and _______ , so the floating roof does not bindas it moves up and down with the liquid level.36、Many crude storage tanks are equipped with ____ that capture light hydrocarbonsthat evaporate from the crude and would otherwise be lost to the atmosphere.考生答案：vapor recovery systems37、Many different corrosion ___ and ______ of corrosion can be at work on the sametank at the same time.考生答案：mechanisms38、Mass-flow meters directly measure the mass of the fluid passing through the meter,no intermediate temperature or pressure ______________ are required and __________ is about the same as PD or turbine meters.考生答案：measurements39、Most pipelines are constructed by ___ short lengths or _____ of pipe together考生答案：welding joints40、NGL is short for ___ .考生答案：atural Liquids41、ESD is short for ___ .考生答案：emergency shutdown42、LNG is short for ___ .考生答案：Liquefied atural43、EFR is short for ___ .考生答案： E xternal F loating R Roof44、LACT unit is short for ___ .考生答案：ease automatic custody transfer unit45、IFR is short for ____ .考生答案：I nternal F loating Roof46、PD meters are short for ____ .考生答案：positive-displacement meters47、PV Valves is short for ___ .考生答案：pressure vacuum vent valves翻译题48、Oil-in-water emulsion考生答案：水包油乳状液49、Emulsion考生答案：乳状液50、Well fluids are often a complex mixture of liquid hydrocarbons,gas,and some impurities ．考生答案：井流通常是液态烃、气体和某些杂质的复杂混合物。
美国科尔斯化学有限公司产品说明书：氨水氧化物
Hydrazine monohydrate Product Number H 0883 Store at Room TemperatureProduct DescriptionMolecular Formula: N2H4 • H2OMolecular Weight: 50.06CAS Number: 7803-57-8Density: 1.03 g/ml (21 °C)1Boiling Point: 118-119 °C (740 torr)1This liquid is 100% hydrazine hydrate, which is equivalent to 64% hydrazine by weight.Hydrazine is a strong base that is used as a reducing agent and a solvent for inorganic materials.1 In molecular biology, hydrazine is utilized in the chemical sequencing of DNA, such as in the Maxam-Gilbert method.2,3 Hydrazine specifically targets thymine in DNA by opening the 6-membered ring, which subsequently recyclizes to a five-membered structure that is eventually released from the sugar backbone.4 Salts can interfere with the reaction of hydrazine and thymine, and thus DNA samples to be sequenced using hydrazine should not be dissolved in either TE buffer or any solution with salt.3Hydrazine hydrate has been utilized in the preparation of trans-7,cis-9 octadecadienoic acid and other conjugated linoleic acid (CLA) isomers by base conjugation of partially hydrogenated γ-linolenic acid.5 The use of hydrazine hydrate to prepare a precursor for a polymer-supported coupling reagent derived from 1-hydroxybenzotriazole synthesis has been reported.6 The preparation of non-immunogenicsialyl-T-glycopeptides on solid phase, with hydrazine hydrate incorporated in the deprotection procedure, has been described.7Precautions and DisclaimerFor Laboratory Use Only. Not for drug, household or other uses.Preparation InstructionsThis product is miscible in water and in alcohol. It is insoluble in chloroform and ether.1References1. The Merck Index, 12th ed., Entry# 4810.2. Maxam, A. M., and Gilbert, W., A new method forsequencing DNA. Proc. Natl. Acad. Sci. USA,74(2), 560-564 (1977).3. Molecular Cloning: A Laboratory Manual, 3rd ed.,Sambrook, J. F., et al., Cold Spring HarborLaboratory Press (Cold Spring Harbor, NY: 2001), pp. 12.61-12.65, 12.68, 12.71, 12.73.4. Maxam, A. M., and Gilbert, W., Sequencing end-labeled DNA with base-specific chemicalcleavages. Methods Enzymol., 65(1), 499-560(1980).5. Delmonte, P., et al., Synthesis and isolation oftrans-7,cis-9 octadecadienoic acid and other CLA isomers by base conjugation of partiallyhydrogenated γ-linolenic acid. Lipids, 38(5),579-583 (2003).6. Pop, I. E., et al., Versatile Acylation ofN-Nucleophiles using a new polymer-supported1-hydroxybenzotriazole derivative. J. Org. Chem., 62(8), 2594-2603 (1997).7. Komba, S., et al., Synthesis of tumor associatedsialyl-T-glycopeptides and their immunogenicity.J. Pept. Sci., 6(12), 585-593 (2000).GCY/CRF 12/03Sigma brand products are sold through Sigma-Aldrich, Inc.Sigma-Aldrich, Inc. warrants that its products conform to the information contained in this and other Sigma-Aldrich publications. Purchaser must determine the suitability of the product(s) for their particular use. Additional terms and conditions may apply. Please see reverse side ofthe invoice or packing slip.。
Solubility of Hydrogen in Heavy n-Alkanes Experiments and SAFT Modeling
Solubility of Hydrogen in Heavy n-Alkanes: Experiments and SAFT ModelingL.J.Florusse and C.J.PetersLaboratory of Applied Thermodynamics and Phase Equilibria,Faculty of Applied Sciences,Delft University of Technology,Julianalaan136,2628BL,Delft,The NetherlandsJ.C.Pamies and Lourdes F.Vega`Dept.d’Enginyeria Quımica,ETSEQ,Universitat Rovira i Virgili,Avinguda dels Paısos Catalans,´¨26,43007,Tarragona,SpainH.MeijerShell Global Solutions International B.V.,1030BN,Amsterdam,The NetherlandsNew experimental measurements on the solubility of hydrogen in se®eral normal al-kanes,ranging from decane and up to hexatetracontane,are presented.Data co®er atemperature range from280K to450K,and pressures up to16MPa were applied.Hydrogen solubilities of up to30mol%were measured.These mixtures are describedthrough a molecular-based equation of state based on the statistical associating fluid()theory SAFT.In the SAFT approach,all the compounds are modeled as homonu-clear chains of united-atom sites interacting through a Lennard-Jones potential.Opti-mized®alues for the chain length,Lennard-Jones diameter,and dispersi®e energy char-acterize the hydrogen molecule.In the case of n-alkanes,a correlation for these molecu-lar parameters is used.Two additional parameters,independent of the thermodynamic®ariables,were fitted to the experimental data of a single isopleth for each particularmixture.The agreement between the measured and predicted solubilities is excellent()o®erall AAD-1.5%in all the thermodynamic range,and does not significantly worsenas the molecular weight of the compound increases.IntroductionHydrogen is a key compound in the production of fuels for the automotive industry and will acquire much more impor-tance in the future,as the free carbon sources of energy tend to emerge for pollution and environmentally evident reasons. Nowadays,hydrogen is mainly obtained from the catalytic steam reforming of nafta and natural gas,but renewable sources of energy seem to be promising for the near future. In many industrial processes where molecular hydrogen plays an important role,its solubility in different hydrocarbon solu-Ž.tions such as fuels is among the major factors required for design and optimal operation of these processes.It is also a key parameter in process models,such as the ones used inCorrespondence concerning this article should be addressed to L.F.Vega.hydrogenation and hydrotreatment processes,where hydro-gen solubility in selected liquid hydrocarbons is a good esti-mation of the hydrogen concentration in the liquid phase,a variable that is often related to kinetics.It is well known that empirical and semiempirical models, like traditional cubic equations of state,have limited predic-tive capabilities,particularly outside the range where their parameters were fitted.On the contrary,parameters of molecular models based on statistical mechanics,like the sta-Ž.tistical associating fluid theory SAFT,have physical mean-ing and are independent of the thermodynamic conditions. Another important advantage of using a molecular-based theory vs.simple mean-field approaches,is that one can ex-plicitly consider intramolecular as well as intermolecular in-teractions among the chain molecules involved.Furthermore,Table 1.Molecular Parameters for the Pure Compounds⑀r k B Ž.Ž.mnm K H 0.48740.424433.852n -C 4.2590.3983272.710n -C 6.4070.4015285.016n -C 10.700.4041294.728n -C 13.570.4049297.836n -C 17.860.4056300.646the details of the applied intermolecular potential will be re-flected in the accuracy of the thermodynamic properties cal-culated by using the theory.The goal of this work is to provide a reliable model for the prediction of vapor ᎐liquid equilibria and solubility of hydro-gen in n -alkanes.To this end,experimental and theoretical work has been carried out in the following binary hydrogen q n -alkane systems:H q n -C ,H q n -C ,H q n -C ,210216228H q n -C ,and H q n -C .236246Experimental MethodMeasurements were performed at the DelftUniversity of Technology,using a Cailletet apparatus.Experimental data cover a temperature region from about 280K to 450K,and pressures up to 16MPa were applied.We measured hydro-gen solubilities of up to a mole fraction of 30%.The Cailletet apparatus operates according to the synthetic method.At any desired temperature,the pressure is variedFigure 1.Coexisting saturated densities of pure hydro -gen.Symbols are experimental data from the NIST chemistry Ž.Webbook http:r r r chemistry and the line corresponds to predictions of SAFT with optimized parame-ters for the subcritical region.for a sample of constant overall composition until a phase change is observed visually.A sample of fixed and known composition is confined over mercury in the sealed end of a thick-walled Pyrex glass tube.The open end of the tube is placed in an autoclave and immersed in mercury.Thus,mer-cury is used for both a sealing and a fluid for transmitting pressure to the sample.The sample is stirred by means of a moving stainless steel ball whose movement is activated by reciprocating magnets.The autoclave is connected to a hy-draulic oil system that generates the pressure by means of a screw-type hand pump.The temperature of the sample is kept constant by circulating the thermostat liquid through a glass thermostat jacket that surrounds the glass tube.Further de-tails of the apparatus and experimental procedure can be Ž.found elsewhere Raeissi and Peters,2001.SAFT modelingFollowing previous work,we model the H and alkanes as 2homonuclear chainlike molecules,formed by tangentially Ž.jointed m Lennard-Jones LJ segments of equal diameter and the same dispersive energy,⑀.Each of the segments rep-resents a group of atoms,which is known as the united-atom approach.The number of segments m is allowed to take non-integer values toaccount for a realistic internuclear distance.The accuracy of this model in conjunction with the soft-SAFT Žapproach has been proven in several works Blas and Vega,.1998;Pamies and Vega,2001,2002.`Ž.The soft-SAFT equation of state EOS is a modification of the original SAFT equation proposed by Chapman et al.Figure 2.Vapor pressures of pure hydrogen in a log-logplot.Symbols are experimental data from the NIST chemistry Ž.Webbook http:r r r chemistry and the line corresponds to predictions of SAFT with optimized parame-ters for the subcritical region.Ž.Ž.1989and Huang and Radosz 1990,which is a first-order Ž.perturbation theory TPT1based on Wertheim ’s work.SAFT equations are usually written in terms of the residual Helmholtz free energy,where each term in the equation rep-resents different microscopic contributions to the total free energy of the fluid.Basic expressions concerning this work follow.For a more detailed description of the soft-SAFT Ž.EOS,the reader is referred to Pamies and Vega 2001and `references therein.For an extensive discussion on the devel-opment and applications of SAFT equations,see the recent Ž.review by Muller and Gubbins 2001.¨For nonassociating chain molecules,SAFT equations are usually written asA res s A ref q A chain1Ž.res Žres total where A is the residual Helmholtz energy A s A y ideal .A .The superscripts ref and chain refer to the contribu-tions from the monomer and the formation of the chain,re-spectively.The original SAFT is based on a hard-spheres reference fluid.In the soft-SAFT EOS,the reference term is a LJ monomer fluid,which accounts both for the repulsive and attractive interactions of the monomers forming the chain.In the chain and association terms,the original SAFT uses the radial distribution function of hard spheres,while the ra-dial distribution function of a LJ fluid is used in soft-SAFT.The chain contribution for a LJ fluid of tangent spherical segments,obtained through Wertheim ’s theory,in terms of the chain length,m ,and the pair correlation function,g ,LJ of LJ monomers,evaluated at the bond length,,is A chains N k T x 1y m ln g exp r k T w x Ž.Ž.Ž.Ž.Ým B i i LJ i L J i B i2Ž.where N is the number of chains,k is the Boltzmann con-m B stant,T is the temperature,x is the mole fraction of compo-i nent i ,and the is the potential energy.L J To calculate the free energy and derived thermodynamic properties of a mixture of LJ fluids,we use the accurate EOS Ž.of Johnson et al.1993,with van der Waals one-fluid mixing rules and the generalized Lorentz-Berthelot combining rules for the crossed interactions1s q 3Ž.Ž.i j i j ii j j 21r 2⑀s ⑀⑀4Ž.Ž.i j i j ii j j The factors and are the cross-interaction binary parame-ters.Table 2.Size Binary Parameter for the MixturesH qn -C 0.8650210H q n -C 0.8777216H q n -C 0.8893228H q n -C 0.8918236H qn -C 0.8933246Phase-equilibria calculationsPhase-equilibria calculations of binary mixtures with the soft-SAFT equation have been described in detail in previous Ž.work Blas and Vega,1998.Here we outline only the part needed for the present study.Molecular parameters for pure H have been calculated by 2fitting experimental pure hydrogen saturated liquid densities and vapor pressures.Because of the type of model used,the m parameter is allowed to be a fractional number in order to account in some way for the nonsphericity of the molecule.In the next section we will show that this approach is not unrealistic for obtaining excellent results.For n -alkanes,we employ the PV correlation recently published by Pamies and `Ž.Vega 2001.All values are given in Table 1.The PV correla-tion comes from the optimized parameters for the first eight members of the series,and it has been proven to provide very accurate results for vapor ᎐liquid properties of pure heavy n -Ž.alkanes and their mixtures Pamies and Vega,2001.`Figures 1and 2show the coexisting vapor ᎐liquid densities and vapor pressures of pure hydrogen.The circles are experi-Žmental data.NIST Chemistry Webbook.http:rr r chemistry .The solid line corresponds to predictions from the equation,using the molecular parameters shown in Table 1.As can be observed in Figure 1,the parameters have been optimized for the subcritical region.Although EOSs with a classical formulation can accurately describe the phase be-havior of pure fluids and mixtures far from the critical point,they are unable to predict the near-critical region.This prob-lem can also be explained as a difficulty in describing the Žcritical compressibility factor and critical exponents Chen .and Mi,2001.To overcome this limitation,a crossover treat-ment has been used recently in several works.See,forexam-Figure 3.Size binary parameter as a function of the car -bon number of the alkane in H H n -alkane 2mixtures.Ž.ple,the work of Kiselev and Ely1999.An alternative ap-proach is to rescale the molecular parameters to the critical Ž.point Pamies and Vega,2001.`SAFT predictions in Figures1and2do not cover the tem-perature region below16K,because of the range of validity of the reference EOS for the Lennard-Jones fluid:the tem-perature range covered by the molecular simulation data that this equation correlates is approximately0.7F T U F6.0. Therefore,although some extrapolation is possible,as shown in these plots,consistent results are not guaranteed.For thisŽU. reason,experimental data under23.7K T s0.7was not used in the optimization of the parameters for the hydrogen molecule.Because of the asymmetry of the binary mixtures we are dealing with,the two cross-interaction binary parametersandshould also be fitted to experimental data.One of the main advantages of using such a molecular-based EOS is that parameters should not depend on the thermodynamic condi-tions.Hence,the procedure we take is to use a single set of data,for example,along an isopleth,to adjust the size pa-rameter while maintaining the energy parameter at a con-stant optimized value along the homologous series.Then we use the optimized values to predict equilibrium properties at any other thermodynamic condition.The fitted values of the cross-interaction size parameter are given in Table2.The energy parameter was fixed at 5.000ؒ10y2.This number makes the hydrogen᎐alkane segment cross-interaction energy ⑀much lower than the interaction energy of the alkane᎐12alkane and hydrogen᎐hydrogen segments,which is consistent with the low solubilities measured.Figure3shows the trend of the size parameter with respect to the carbon number of the normal alkane.This trend is the same as that of the sizeŽparameter,,of the n-alkane homologous series Pamies and`.Vega,2001,and asymptotically tends to a constant value as ()()UTable3.Measured Solubility Data for the H1H n-Decane2Mixture2T P T P T PŽ.Ž.Ž.Ž.Ž.Ž.K MPa K MPa K MPax s0.016x s0.051x s0.078111283.17 2.568283.268.545283.2113.485 283.22 2.573298.197.775298.1312.265 298.14 2.343313.067.135313.0811.215 298.15 2.348328.06 6.565328.0210.315 313.05 2.163343.01 6.075342.989.535 313.12 2.158357.63 5.645357.568.875 328.04 1.993357.99 5.645357.948.845 342.98 1.843372.57 5.255373.068.215 357.79 1.723387.62 4.905387.977.665 357.88 1.718402.57 4.585402.857.165 372.84 1.608417.52 4.305417.74 6.705 387.76 1.508432.46 4.045432.62 6.295 402.66 1.418447.34 3.815447.66 5.905 417.83 1.343432.71 1.283447.61 1.238x s0.031x s0.056x s0.088111283.22 5.025283.239.463298.1614.216 298.13 4.585298.098.613313.1012.996 312.96 4.215313.017.893328.0411.946 327.92 3.895328.027.273343.0811.026 342.91 3.595343.08 6.713357.6610.226 357.74 3.345357.94 6.243358.0910.216 357.87 3.345373.03 5.793372.579.506 372.79 3.115387.77 5.413387.618.866 387.76 2.915403.56 5.033402.558.276 403.03 2.725418.24 4.733417.547.736 417.94 2.565433.85 4.443432.437.246 432.65 2.435447.92 4.203447.41 6.806 447.53 2.325x s0.038x s0.06711283.22 6.335283.2111.635298.10 5.775298.1110.575313.07 5.295313.079.685327.81 4.885328.078.905342.73 4.525343.078.235357.69 4.205358.007.635357.99 4.195359.187.575372.79 3.905373.807.055387.80 3.645388.73 6.585402.71 3.425405.35 6.105417.69 3.215419.52 5.735432.60 3.035435.18 5.375448.46 2.865449.63 5.065Note:x is the mole fraction.the length of the chain increases,representing the effective value for the H y CH interaction.Additionally,the alkane22chain length timeslinearly varies with the carbon number,which easily allows us to obtain,with confidence,theval-ues for other H q n-alkane mixtures.2Results and DiscussionWe present measurements of the solubility of H in n-de-2cane,n-hexadecane,n-octacosane,n-hexatriacontane,and n-hexatetracontane,and predictions from the soft-SAFT EOS for this system.Experimental data are summarized in Tables 3᎐7.We also check the performance of the modified Peng-Ž.Robinson PR EOS,as found in the Hysys Plant2.4.1pro-cess-engineering simulator.Several reasons led us to choose this equation for comparison.On the one hand,PR is one of the most used equations in the process industry,and it has been proven to provide very good predictions for alkane bi-Ž. nary systems Pamies and Vega,2001,and references therein.`On the other hand,we found it very appropriate to use a version embedded in a commercial package,since this is the path engineers usually take in order to use phase-equilibrium data for the design and optimization of chemical processes.()()Table4.Measured Solubility Data for the H1H n-Hexadecane2Mixture2T P T P T PŽ.Ž.Ž.Ž.Ž.Ž.K MPa K MPa K MPax s0.018x s0.078x s0.109111298.13 2.266298.2110.951312.9714.307 313.11 2.071313.219.991327.8113.127 328.09 1.921328.179.166342.7512.127 343.07 1.781343.048.461357.6411.267 357.97 1.656357.917.856357.8611.217 358.07 1.656358.037.851372.7810.467 372.79 1.551372.857.331387.719.767 387.80 1.451387.91 6.866402.629.147 403.05 1.361403.17 6.446417.668.577 418.19 1.286418.21 6.066432.548.077 432.82 1.216432.92 5.711447.347.607 448.02 1.151448.17 5.341x s0.035x s0.086x s0.113111298.16 4.600313.0510.970313.0415.134 313.07 4.205327.9310.190327.9613.884 328.09 3.870342.949.320342.9612.824 343.05 3.590354.768.780357.6011.914 357.63 3.345357.738.650357.9811.904 357.99 3.345372.968.060372.6711.084 373.03 3.115387.907.540388.0010.344 387.81 2.920402.837.060402.839.694 402.84 2.745417.78 6.650417.719.104 417.81 2.580432.65 6.260432.758.564 432.75 2.435447.54 5.910447.598.074 447.71 2.300x s0.056x s0.09111313.07 6.893312.8411.640328.11 6.343327.8710.700343.03 5.873342.669.930357.66 5.473357.759.190358.00 5.463357.819.190372.64 5.103372.978.550387.68 4.773387.907.980402.76 4.483402.787.490417.72 4.213417.657.040432.65 3.973432.66 6.630447.52 3.753447.52 6.250x s0.073x s0.09411313.079.203313.0512.153328.018.463328.0011.143343.057.823343.0210.303357.947.273357.809.563357.957.263357.959.573372.93 6.763373.188.883372.93 6.763388.018.303387.96 6.333403.017.783402.93 5.943417.907.333417.85 5.583432.69 6.923432.76 5.263447.56 6.523447.58 4.963Note:x is the mole fraction.()()Table5.Measured Solubility Data for the H1H n-Octacosane2Mixture2T P T P T PŽ.Ž.Ž.Ž.Ž.Ž.K MPa K MPa K MPax s0.030x s0.091x s0.143111342.68 2.245342.677.468342.6012.581 357.58 2.085357.63 6.928357.5211.681 372.49 1.955372.73 6.458372.4510.891 387.48 1.835387.62 6.058387.5010.191 402.45 1.735402.48 5.708402.459.581 417.39 1.635417.55 5.388417.439.041 432.27 1.545432.47 5.098432.398.551 447.13 1.465447.31 4.838447.328.131x s0.054x s0.106x s0.178111342.68 4.165342.568.613372.4914.001 357.70 3.865357.537.973387.4813.101 372.79 3.605372.457.453402.4312.311 387.80 3.385387.48 6.983417.4011.611 402.52 3.185402.40 6.563432.3210.991 417.46 3.005417.37 6.193447.2310.411 432.39 2.845432.32 5.863447.34 2.705447.26 5.553x s0.0711342.59 5.841357.49 5.421372.47 5.061372.49 5.071387.47 4.751402.42 4.461417.35 4.221432.28 3.981432.33 3.981447.21 3.771Note:x is the mole fraction.In Figure4the symbols represent our primary experimen-Ž.tal data isopleths,which are summarized in Table3.Thesymbols in Figure5represent the solubility of H in liquid2n-decane for a number of isotherms,which have been calcu-lated from the primary experimental data,as summarized in Table3and depicted in Figure4.In both Figures4and5, the solid lines are the soft-SAFT predictions using the pa-rameters of Tables1and2.Excellent agreement is obtained,Ž.with an absolute averaged deviation AAD of about0.8%. Only about12.5%of the measurements have been used to fit the cross-interaction parameters,but it is impossible to dis-tinguish which of the isopleths in Figure4was chosen.Dot-dashed lines in this figure correspond to predictions using the PR EOS,which are shown for three selected isopleths. This EOS performs equally well as the soft-SAFT EOS,ex-cept at low temperatures,where it declines toward lower pressures.Ž. Figures6and7show experimental data Tables4and5 and theoretical results for the H q n-C and H q n-C216228 mixtures,respectively.In these figures,the accuracy of the SAFT predictions is similar to that obtained for the lighter Ž.alkane n-decane.On the other hand,the performance of ()()Table6.Measured Solubility Data for the H1H n-Hexatriacontane2Mixture2T P T P T PŽ.Ž.Ž.Ž.Ž.Ž.K MPa K MPa K MPax s0.033x s0.097x s0.169111357.62 1.985357.53 6.188357.5411.921 372.53 1.845372.54 5.778372.5211.101 387.54 1.735387.61 5.418387.5410.391 402.52 1.625402.60 5.098402.499.771 417.50 1.535417.48 4.818417.479.201 432.46 1.455432.41 4.558432.418.731 447.43 1.375447.35 4.328447.358.281x s0.066x s0.118x s0.210111357.56 4.069357.607.881372.5314.341 372.53 3.799372.537.341387.5713.421 387.64 3.559387.58 6.881402.5012.621 402.55 3.349402.53 6.471417.4811.901 417.48 3.159417.49 6.101432.3711.261 432.43 2.999432.41 5.791447.2310.681 447.39 2.849447.36 5.511Note:x is the mole fraction.()()Table7.Measured Solubility Data for the H1H n-Hexatetracontane2Mixture2T P T P T PŽ.Ž.Ž.Ž.Ž.Ž.K MPa K MPa K MPax s0.065x s0.129x s0.204111372.61 3.063372.59 6.741372.5211.811 387.64 2.853387.55 6.311387.5711.041 402.62 2.683402.51 5.941402.5410.391 417.61 2.533417.51 5.601417.449.801 432.50 2.403432.37 5.311432.379.271 447.48 2.293447.32 5.041447.278.811x s0.095x s0.173x s0.257111372.71 4.623372.589.461372.5715.970 387.64 4.333387.668.841387.6114.910 402.60 4.083402.638.301402.6913.990 417.56 3.853417.657.831417.7313.180 432.54 3.653432.527.421432.5812.470 447.46 3.463447.517.051447.5011.840 U Note:x is the mole fraction.the PR EOS rapidly deteriorates,and this is more noticeable at the largest mole fraction values of H in the liquid phase.2In Figures8and9we check the performance of both the soft-SAFT and PR EOS compared to experimental data from Ž.Lin et al.1980,which were measured up to much higher pressures and temperatures than were those we present in this study.The results are a very severe test for the perfor-mance of both EOSs in these systems.Data up to25MPa and665K are used for comparison.No fitting to these data was performed.Cross-interaction parameters for this mixture were optimized using the experimental data of a single iso-pleth selected from those shown in Figure6,which are atFigure4.Isopleths of the H H n-decane vapor–liquid2equilibrium.Symbols are used for experimental data taken from Table3,and solid and dot-dashed lines correspond to soft-SAFT andPR predictions,respectively.rather lower pressures and temperatures.Predictions fromŽthe SAFT equation are excellent for the liquid phase Figure .Ž8.Poorer results were expected for the vapor phase Figure .9,since no information of this phase was used in the opti-mization of cross-interaction parameters.However,the excel-lent accuracy of SAFT predictions for the H solubility in the2liquid phase,on which this study is focused,is remarkable. PR solubility predictions are much less accurate,although va-por-phase compositions are captured better by PR than by SAFT.We are aware of the somewhat unfair comparison be-tween both EOSs,because,when we used our experimental data,we did not fit any parameter of the PR equation.AsFigure5.Solubility of hydrogen in n-decane,for se-lected isotherms.Symbols are interpolated experimental data from Table3,and lines correspond to soft-SAFT predictions.Tempera-tures are given in K.Figure 6.Isopleths of the H H n -hexadecane vapor –2liquid equilibrium.Symbols are used for experimental data taken from Table 4,and solid and dot-dashed lines correspond to soft-SAFT and PR predictions,respectively.Figure 7.Isopleths of the H H n -octacosane vapor –2liquid equilibrium.Symbols are used for experimental data taken from Table 5,and solid and dot-dashed lines correspond to soft-SAFT and Ž.PR predictions at x s 0.030,0.091,and 0.178,respec-1tively.mentioned before,our aim is to show the performance of the Hysys modified version of the PR EOS,with all parameters Žfrom the Hysys database.It has already been proven Park et .al.,1995that the fitting of the PR binary interaction param-eter to each experimental isotherm will provide much better results.But the predictive capability of the EOS is not shown in this way.The performance of the PR equation depends strongly on the ␣function and the binary interaction param-eter used.Although the effect of the binary parameter can be minimized through an optimized temperature-dependent ␣Ž.function Twu et al.,1995,we believe that to fit parameters depending on temperature is an unavoidable requirement for obtaining accurate predictions using cubic EOSs.On the con-trary,the soft-SAFT EOS does not have temperature-depen-dent parameters,and we only use data of a single experimen-tal isopleth for the optimization of the binary interaction pa-rameter of the mixture.In this way,we use SAFT in a fully predictive way at other thermodynamic conditions.ŽFigures 10and 11present experimental data Tables 6and .7,respectively ,and model predictions for the binary systems H q n -C and H q n -C ,respectively.Due to the prox-236246imity to the triple point of the n -hexatetracontane,no ther-modynamically consistent solutions for the SAFT EOS could be obtained below approximately 400K.These stringent thermodynamic conditions lie far beyond the thermodynamic Žrange of validity of the LJ reference EOS see the section .entitled Phase-Equilibria Calculations .The same reasoning can be used for the H q n -C mixture below approxi-236Ž.mately 360K Figure 10.Nevertheless,accuracies remain as low as for those mixtures with the lower chain-length alka-Figure 8.Solubility of H in n -hexadecane,for selected2isotherms.Ž.Symbols are experimental data taken from Lin et al.1980,and solid and dot-dashed lines correspond to soft-SAFT and PR predictions,respectively.Temperatures are given in K.Figure 9.Equilibrium mole fraction of hydrogen in thevapor phase of the H H n -hexadecane mix -2ture,for selected isotherms.Ž.Symbols are experimental data taken from Lin et al.1980and solid and dot-dashed lines correspond to soft-SAFT and PR predictions,respectively.Temperatures are given inK.Figure 10.Isopleths of the H H n -hexatriacontane va -2por –liquid equilibrium.Symbols are used for experimental data taken from Table 6,and solid lines correspond to soft-SAFTpredictions.Figure 11.Isopleths of the H H n -hexatetracontane2vapor –liquid equilibrium.Symbols are used for experimental data taken from Table 7,and solid lines correspond to soft-SAFT predictions.nes,except for the highest solubilities of H ,where devia-2tions can increase up to an AAD of 2.5%.Consequently,the length of the alkane chain does not significantly influence the accuracy of the predictions,at least for the range of chain-length studied here.The overall AAD of soft-SAFT predic-Ž.tions with respect to solubility measurements Tables 3᎐7is less than 1.5%.PR predictions are not included in Figures 10and 11,since the two heaviest alkanes are not available in the Hysys Plant library.To summarize,the molecular model,in conjunction with the soft-SAFT theory,provides very reliable results for the solubility of H in n -alkane systems in a wide range of pres-2sures and temperatures.Furthermore,the accuracy of the predictions is independent of the thermodynamic conditions and the length of the alkane chain.It is also important to note that,to some extent,the success of the soft-SAFT the-ory relies on the physical meaning of the molecular parame-Žters such as segment size,dispersive energy,and chain .length .Although their values are effective,their physical meaning is conserved,as we have already seen in Figure 3.Ž.As was recently discussed Pamies and Vega,2001,parame-`ters should be optimized by considering the experimental in-formation range needed to later reproduce the thermody-namic features of interest.For H q n -alkane mixtures,the 2experimental data from a single isopleth suffices to provide excellent predictions,provided that molecular parameters have been optimized following a meaningful trend.ConclusionsExperimental data on the solubility of hydrogen in heavy n -alkanes and SAFT modeling of these very asymmetric sys-tems have been presented.For the five selected mixtures Žstudied H q n-C,H q n-C,H q n-C,H q n-2102162282.C,and H q n-C,the data covered a temperature range 36246from about280K up to450K,and pressures up to16MPawere applied.The theoretical description is performed using the soft-SAFT equation of state,which describes the fluid systems through a chainlike homonuclear model of Lennard-Jones segments,bonded tangentially to form the chain.Opti-mized values for the vapor᎐liquid equilibria of the pure com-pounds are used to predict the behavior of the mixtures.In addition,the binary size interaction parameter of the gener-alized Lorentz-Berthelot combining rules was fitted to the ex-perimental data of a single isopleth and used to quantita-tively describe the same system in the whole range of experi-mental conditions,in a fully predictive manner.The overall absolute averaged deviation of SAFT predictions with the ex-perimental data is less than1.5%.SAFT predictions are ex-cellent over the entire thermodynamic range where data were measured.The accuracy is independent of the thermody-namic variables,and does not get significantly worse as the chain length of the n-alkane increases.Consequently,it isproven that for H q n-alkane mixtures,the soft-SAFT2molecular model is able to provide very accurate and reliable results whenever optimized parameters remain meaningful, that is,follow physically meaningful trends.AcknowledgmentsThe experimental work of this study was financed by Shell Global Solutions International B.V.,Shell Research and Technology Centre, Amsterdam,The Netherlands.Financial support for this work has also been provided by the Spanish Government,under projectsŽ. PPQ2000-2888-E and PPQ-2001-0671.One of the authors J.C.P. acknowledges a predoctoral grant from the Departament d’Universi-tats,Recerca i Societat de la Informacio de la Generalitat de Gener-´alitat de Catalunya.Literature CitedBlas,F.J.,and L.F.Vega,‘‘Prediction of Binary and Ternary Dia-Ž. grams Using the Statistical Associating Fluid Theory SAFTŽ. Equation of State,’’Ind.Eng.Chem.Res.,37,6601998.Chapman,W.G.,K.E.Gubbins,G.Jackson,and M.Radosz,‘‘Saft-Equation-of-State Solution Model for Associating Fluids,’’FluidŽ.Phase Equilib.,52,311989.Chen,J.,and J.G.Mi,‘‘Equation of State Extended from SAFT with Improved Results for Non-Polar Fluids Across the CriticalŽ.Point,’’Fluid Phase Equilib.,186,1652001.Coorens,H.G.A.,C.J.Peters,and J.de Swaan Arons,‘‘Phase Equilibria in Binary Mixtures of Propane and Tripalmitin,’’FluidŽ.Phase Equilib.,40,1351988.Huang,S.H.,and M.Radosz,‘‘Equation of State for Small,Large, Polydisperse,and Associating Molecules,’’Ind.Eng.Chem.Res.,Ž.29,22841990.Johnson,J.K.,J.A.Zollweg,and K.E.Gubbins,‘‘The Lennard-JonesŽ. Equation of State Revisited,’’Mol.Phys.,78,5911993. Kiselev,S.B.,and J.F.Ely,‘‘Crossover SAFT Equation of State: Application for Normal Alkanes,’’Ind.Eng.Chem.Res.,38,4993Ž.1999.Lin,H.,H.M.Sebastian,and K.Chao,‘‘Gas-Liquid Equilibrium in Hydrogen q n-Hexadecane and Methane q n-Hexadecane at El-evated Temperatures and Pressures,’’J.Chem.Eng.Data,25,252Ž.1980.Muller,E.A.,and K.E.Gubbins,‘‘Molecular-Based Equations of ¨State for Associating Fluids:A Review of SAFT and Related Ap-Ž. proaches,’’Ind.Eng.Chem.Res.,40,21932001.Pamies,J.C.,and L.F.Vega,‘‘Vapor-Liquid Equilibria and Critical `Behavior of Heavy n-Alkanes Using Transferable Parameters from the Soft-SAFT Equation of State,’’Ind.Eng.Chem.Res.,40,2532Ž.2001.Pamies,J.C.,and L.F.Vega,‘‘Critical Properties of Homopolymer `Fluids Studied by a Lennard-Jones Statistical Associating FluidŽ.Theory,’’Mol.Phys.,100,25192002.Park,J.,R.L.Robinson,Jr.,and K.A.M.Gasem,‘‘Solubilities of Hydrogen in Heavy Normal Paraffins at Temperatures from323.2 to423.2K and Pressures to17.4MPa,’’J.Chem.Eng.Data,40,241Ž.1995.Peters,C.J.,‘‘Phase Behavior of Binary Mixtures of Ethane q n-Eicosane and Statistical Mechanical Treatment of Fluid Phases,’’Ž.Ph.D.Thesis.Delft University of Technology1986.Raeissi,S.,and C.J.Peters,‘‘Bubble-Point Pressures of the Binary System Carbon Dioxide q Linalool,’’J.Supercrit.Fluids,20,221Ž.2001.Twu,C.H.,J.E.Coon,A.H.Harvey,and J.R.Cunningham,‘‘An Approach for the Application of a Cubic Equation of State to Hy-Ž. drogen-Hydrocarbon Systems,’’Ind.Eng.Chem.Res.,35,9051996. Manuscript recei®ed Jan.8,2003,and re®ision recei®ed Apr.28,2003.。
3 碳氢化合物,高分子
hydrocarbon碳氢化合物：Hydrocarbons are composed of hydrogen and carbon. The intramolecular bonds are covalent.macromolecules高分子：a huge molecule made up of thousands of atoms. Macromolecules高分子（polymer)Polymer was coined to mean many mers.A compound consisting of long-chain molecules, each molecule made up of repeating units connected together.Mer(单体单元，结构单元)：Structural entities, originates from the Greek word meros, which means part;Monomer（单体）：A stable molecule from which a polymer is synthesized, such as ethylene. Polymerization(聚合反应）：The synthesis of the large molecular weight polymers is termed polymerizationThermoplastics（热塑性聚合物）Thermoplastics soften when heated (and eventually liquefy) and harden when cooled—processes that are totally reversible and may be repeated. （加热变软冷却变硬可回收的）Thermosetting （热固性聚合物）Thermosetting polymers become permanently hard when heat is applied and do not soften upon subsequent heating.塑料形成方式：The most common method for forming plastic polymers. Include compression（压塑）, transfer(传递模塑), blow（吹塑模塑法）, injection (注塑模塑), and extrusion molding (挤压模塑)。