流化床模拟操作 - 360文档中心

典型化工厂3D虚拟现实生产实习仿真(操作手册)V2.0.2

东方汽化器(E102A\B)中汽化，东反应器(R101)，在催化剂的作用下，硝基苯被还原，生成苯胺和水并放出大量热。
反应式如下： C6H5-NO2+H2→C6H5-NH2+O2
1
通用流化床装置 3D 仿真操作实习手册
硝基苯加氢生成苯胺，硝基苯中 O 被 H 取代。加氢反应所放出的热量被废
开车前的开车前的准备工作：
东（1）检查本岗位所管辖的设备、管道、阀件的检修工作是否完成。方（2）对新装或改装的氢气管道必须进行气密性试验。仿（3）蒸汽管道通蒸汽试漏，并消除漏点。
（4）检查所管辖的设备管道间的阀件开关位置是否正确。（5）检查所有安全设施、消防器材是否完整无损。
东（6）检查所有仪表变送器是否接通电源，调节阀开启灵活。方（7）检查与本岗位生产有关的贮罐，以便平衡生产。东（8）打开 R101 的催化剂入口阀 VA108
5.3 人物栏介绍 ··········································································22 5.4 工具箱介绍 ················································································23
2
通用流化床装置 3D 仿真操作实习手册
（接上页- -设备列表）
序号
设备位号
设备名称
17
T301
苯胺脱水塔
18
T302
苯胺精馏塔
19 20 21 22 23 24
V101 V102 V201 V202 V203 V301
真废热汽包催化剂罐粗苯胺中间罐苯胺、水分离器废水储罐粗苯胺罐

循环流化床底部区域流动特性的数值模拟

摘
要：基于欧拉两相流模型计算循环流化床底部区域的流动特性。
泛的应用。
在低气速（．～２５ｍ／）低循环量下（．～３．ｋ／・）模拟时黏１０．ｓ、５２４５ｇ（ｓ，ｍ）
性采用层流模型取得了较好的效果。实验采用光导纤维探头测量仪测量流化床底部区域３个截面的局部颗粒浓度．拟计算了循环流化床模
１实验装置
冷态循环流化床（Ｆ实验研究系统如图１所ＣＢ）
示。实验台高１０ｍ，整个实验装置由３个流化床组
循环流化床内的流动是气固两相复杂流动，颗
粒流体流动结构的主要特征在于其非均匀的两相时空动态结构。循环流化床由底部的浓相区和上部的稀相区组成。循环流态化气固两相流动的重要特性是两相流动在床层轴向和径向整体规模上的不均匀
ｏｅｒｌｕ，ｎｙｎ７６１２ＣｏｌｇｆｅｃｌｇｎｅｎｆＰｔｏｅｍＤｏｇｉｇ２５０；．ｌｅｏＣｈｍｉａｅＥｎｉｅｒｇ，ｉ
ＳｉａｉｆＦｏＣｈａｔＳｉＳｉｍｕｌｔｏｎｏｌｗａｒｃｅｉｔｒＣｎ
底部３个截面的颗粒浓度的径向分布．同循环流化床装置的实验数并据进行了对比。结果表明，数值模拟计算与实验结果相吻合。

微型流化床反应器液相冷态进样停留时间分布模拟与实验

地
致液相平均停留时间的减小，且通过计算得出，当气相流量分别为４、６、８、１０Ｌ／ｈ时，液相流量增加
带来的液相停留时间的减小量分别为０．３１、０．２３、０．２３、０．２６ｓ，而当液相流量不变时，气相流量增加带来的停留时间的减小量分别为０．５２、
昆日
址霜
１
图４液相流量６Ｌ／ｈ时液相停留时间分布曲线
一
档
船
，‘
｛
｝
｛
ｌ
０９８７６５４３２
０
厘翟
臣 Ⅲ
图６不同条件下模拟所得液相平均停留时间由图６可以看出，气、液相流量的增大均会导
和改进具有重要意义。Ｆｌｕｅｎｔ软件可以较好地模拟反应器内流场情况，采用示踪剂法能够准确得
出口直径ｄ４ｍｍ液相原料进口直径ｄ，４ｍｍ载气入口直径ｄ４ｍｍ
出停留时间分布。俞志楠等对气流喷射床反
７９８
化
工
机
械
２０ｌ３年
液相流量为６Ｌ／ｈ时，不同气相流量条件下
笔者用下式处理Ｆｌｕｅｎｔ模拟结果，得到不同
的停留时间分布曲线如图４所示；气相流量为

FLUENT流化床模拟实例

Tutorial:Using the Eulerian Multiphase Model with Species TransportIntroductionFluidized beds are used in processes where gas/solid mass transfer is of importance.The de-composition of ozone(O3),using particles as a catalyst,creates a suitable low-temperature environment for mass transfer.This tutorial solves a gas/solidﬂow with a simple one-step ozone decomposition reaction in aﬂuidized bed.The reaction equation isO3→1.5O2(1) This tutorial demonstrates how to do the following:•Use the granular Eulerian multiphase model with species transport.•Deﬁne the rate of reaction with a user-deﬁned function(UDF).•Deﬁne the Syamlal-O’Brien drag correlation with a user-deﬁned function(UDF)usingappropriate parameters.•Set boundary conditions for internalﬂow.•Deﬁne theﬂuid and solid phases.•Calculate a solution using2D planar geometry in conjunction with the pressure-basedsolver.•Solve a time-accurate transient problem with data sampling for time statistics.PrerequisitesThis tutorial assumes that you are familiar with the FLUENT interface and that you have a good understanding of basic setup and solution procedures.Some steps will not be shown explicitly.In this tutorial you will use the Eulerian multiphase model with species transport.If you have not used this feature before,refer to the FLUENT6.3User’s Guide.Using the Eulerian Multiphase Model with Species TransportProblem DescriptionThe problem involves the transient startup of ozone decomposition in a ﬂuidized bed.The ﬂuid phase is a mixture of ozone and air,while the solid phase consists of sand particles with an 87.75micron diameter.A schematic of the ﬂuidized bed is shown in Figure 1.The domain is modeled as a 2D planar cylindricalcase.volume fraction 0.52 of solids pressure outlet uniform velocity inlet u = 0.08 m/s 0 Pa gauge Figure 1:Problem SpeciﬁcationUsing the Eulerian Multiphase Model with Species Transport Preparation1.Copy theﬁles2-D-FBed Ozone.msh.gz,rrate.c,and bp drag.c to your workingfolder.2.Start the2D double-precision(2ddp)version of FLUENT.Setup and SolutionStep1:Grid1.Read the gridﬁle(2-D-FBed_Ozone.msh).File−→Read−→Case...As FLUENT reads the gridﬁle,it will report its progress in the console.2.Check the grid.Grid−→CheckFLUENT will perform various checks on the mesh and will report the progress in the console.Make sure the minimum volume reported is a positive number.3.Display the grid using the default settings.Display−→Grid...Figure2:Grid Display4.Rotate the view so that the inlet of theﬂuidized bed is at the bottom.Display−→Views...Using the Eulerian Multiphase Model with Species Transport(a)Click the Camera...button to open the Camera Parameters panel.i.Drag the indicator of the dial with the left mouse button in the counter-clockwise direction until the upright view(-90◦)is displayed(Figure2).ii.Close the Camera Parameters panel.(b)Click the Save button in the Actions group box in the Views panel to save theupright view.When you do this,view-0will be added to the list of Views.(c)Close the Views panel.You can use the probe mouse button to check which zone number corresponds to eachboundary.If you click the probe mouse button on one of the boundaries in the graphicswindow,its zone number,name,and type will be printed in the FLUENT console.Thisfeature is especially useful when you have several zones of the same type and you wantto distinguish between them quickly.Using the Eulerian Multiphase Model with Species Transport Step2:Models1.Specify a transient,2D model.Deﬁne−→Models−→Solver...(a)Retain the default selection of Pressure Based from the Solver list and2D fromthe Space list.The pressure based solver must be used for multiphase calculations.(b)Select Unsteady from the Time list.(c)Click OK to close the Solver panel.2.Deﬁne the multiphase model.Deﬁne−→Models−→Multiphase...(a)Select Eulerian from the Model list.The panel will expand to show the inputs for the Eulerian model.Using the Eulerian Multiphase Model with Species Transport(b)Retain the default value of2for Number of Phases.(c)Click OK to close the Multiphase Model panel.3.Deﬁne the species model.Deﬁne−→Models−→Species−→Transport&Reaction...(a)Select Species Transport from the Model list.The Species Model panel will expand.(b)Enable Volumetric from the Reactions group box.(c)Disable Diﬀusion Energy Source from the Options group box.(d)Click OK to close the Species Model panel.Using the Eulerian Multiphase Model with Species Transport FLUENT will list the properties required for the models that you enabled,in theconsole.An Information dialog box will appear,reminding you to conﬁrm theproperty values that have been extracted from the database.(e)Click OK in the Information dialog box to continue.Step3:MaterialsDeﬁne−→Materials...1.Create a new material called air+ozone.(a)Click the Fluent Database...button to open the Fluent Database Materials panel.i.Selectﬂuid from the Material Type drop-down list.ii.Select ozone(o3)from the Fluent Fluid Materials selection list.iii.Click Copy to copy the information for ozone to your model and close the Fluent Database Materials panel.(b)Select mixture from the Material Type drop-down list.(c)Enter air+ozone for Name.(d)Click Change/Create.When you click Change/Create,a Question dialog box will appear,asking you ifmixture-template should be overwritten.Click No to retain mixture-template andadd the new material,air+ozone,to the list.The Materials panel will be updatedto show the new material name in the Fluent Mixture Materials list.Using the Eulerian Multiphase Model with Species Transport2.Click the Edit...button to the right of the Mixture Species drop-down list to open theSpecies panel.You will select the species that are involved in the decomposition of ozone.The orderof the species in the Selected Species list is important.Perform the following steps to achieve the proper order:(a)Select water-vapor(h2o)from the Selected Species selection list and click theRemove button to move it to the Available Materials selection list.(b)Similarly,remove n2from the Selected Species list.(c)Select ozone(o3)from the Available Materials selection list and click the Addbutton.(d)Similarly,add n2back in the Selected Species list.The Selected Species list should now contain o2,o3,and n2,respectively.(e)Click OK to close the Species panel.Using the Eulerian Multiphase Model with Species Transport 3.Click the Edit...button to the right of the Reaction drop-down list to open the Reac-tions panel.(a)Select o3from the Species drop-down list in the Reactants group box and enter1for both Stoich.Coeﬃcient and Rate Exponent.(b)Select o2from the Species drop-down list in the Products group box and enter1.5for Stoich.Coeﬃcient and0for Rate Exponent,respectively.There is no need to modify the Arrhenius Rate constants,as a UDF will be used to deﬁne them in Step4.(c)Click OK to close the Reactions panel.4.Retain the default settings in the Reaction Mechanisms panel.5.Select volume-weighted-mixing-law from the Density drop-down list.Thermal properties do not need to be speciﬁed since this is an isothermal case.6.Retain the default value of1.72e-05for Viscosity.7.Click Change/Create.Using the Eulerian Multiphase Model with Species Transport8.Create a new material called solids.In theﬂuidized bed the solid particles(treated as aﬂuid)are held in suspension by theair+ozone mix injected at the bottom of the bed.(a)Selectﬂuid from the Material Type drop-down list.(b)Select water-vapor(h2o)from the Fluent Fluid Materials drop-down list.(c)Enter solids for Name.(d)Enter silica for Chemical Formula.(e)Enter2650kg/m3for Density.(f)Click Change/Create and close the Materials panel.When you click Change/Create,a question dialog box will appear,asking you ifwater-vapor(h2o)should be overwritten.Click No to retain water-vapor(h2o)and add the new material,solids,to the list.The Materials panel will be updatedto show the new material name in the Fluent Fluid Materials list.You can remove materials that are not required to run this case by selecting mix-ture in the Material Type in the Materials panel.Under Fluent Mixture Materials,select mixture-template from the drop-down list and click the Delete button.Simi-larly,selectﬂuid in the Material Type and delete all Fluent Mixture Materials otherthan O2,O3,N2,air and silica.9.Specify the species for the gaseous phase(phase-1)and the sand bed phase(phase-2).Deﬁne−→Models−→Species−→Transport&Reaction...(a)Select phase-1from the Phase drop-down list and click the Set...button to openthe Phase Properties panel.i.Select air+ozone from the Material drop-down list.ii.Click OK to close the Phase Properties panel.(b)Select phase-2from the Phase drop-down list and click the Set...button to openthe Phase Properties panel.i.Select solids from the Material drop-down list.ii.Click OK to close the Phase Properties panel.(c)Click OK to close the Species Model panel.Step4:User-Deﬁned Functionspile the user-deﬁned functions.Deﬁne−→User-Deﬁned−→Functions−→Compiled...(a)Click the Add...button in the Source Files group box to open the Select Filepanel.(b)Select theﬁles,rrate.c and bp drag.c and click OK.The bp drag.c source code is a routine for customizing the default Syamlal-O’Briendrag law in FLUENT.In the solid phase,the default drag law uses coeﬃcientsof0.8(for voids≤0.85)and2.65(for voids>0.85),for minimumﬂuid ve-locities of0.25m/s.The current drag law has been modiﬁed to accommodate aminimumﬂuid velocity of0.08m/s.The source code,rrate.c,deﬁnes a customvolumetric reaction rate for the decomposition reaction of ozone.(c)Click Build to build the library.(d)Click Load to load the UDF.FLUENT will build a libudf folder and compile the UDF.A dialog box will appear warning you to make sure that UDF sourceﬁles are inthe folder that contain your case and dataﬁles.Click OK in the dialog box.(e)Close the Compiled UDFs panel.2.Specify the volume reaction rate function.Deﬁne−→User-Deﬁned−→Function Hooks...(a)Select rrate::libudf from the Volume Reaction Rate Function drop-down list.(b)Click OK to close the User-Deﬁned Function Hooks panel.Step5:Phases1.Deﬁne the granular secondary phase.Deﬁne−→Phases...(a)Select phase-2and click the Set...button.i.Enable Granular.ii.Deﬁne the properties of the solid phase as shown in the table:Parameters ValuesDiameter8.775e-05mGranular Viscosity syamlal-obrienGranular Bulk Viscosity lun-et-alFrictional Viscosity schaeﬀerAngle of Internal Friction30degreesGranular Temperature algebraicSolids Pressure syamlal-obrienRadial Distribution syamlal-obrienElasticity Modulus derivePacking Limit0.53Note:You will have to scroll down the Properties list to see the remaining options.iii.Click OK to close the Secondary Phase panel.2.Specify the drag law to be used for computing the interphase momentum transfer.(a)Click the Interaction...button to open the Phase Interaction panel.i.Select user-deﬁned from the Drag Coeﬃcient drop-down list to open the User-Deﬁned Functions panel.A.Select custom drag syam::libudf and click OK to close the User-DeﬁnedFunctions panel.ii.Click the Collisions tab and enter0.8for Constant Restitution Coeﬃcient.iii.Click OK to close the Phase Interaction panel.3.Close the Phases panel.Step6:Operating ConditionsSet the gravitational acceleration.Deﬁne−→Operating Conditions...1.Enable Gravity.The panel will expand to show additional inputs.2.Enter-9.81m/s2for Gravitational Acceleration in the X direction.3.Enter297K for Operating Temperature.4.Click OK to close the Operating Conditions panel.Step7:Boundary ConditionsDeﬁne−→Boundary Conditions...1.Set the conditions for the gaseous phase(phase-1).(a)Select Inlet from the Zone selection list.(b)Select phase-1from the Phase drop-down list and click the Set...button to openthe Velocity Inlet panel.i.Enter0.08m/s for Velocity Magnitude.ii.Click the Thermal tab and enter293K for Temperature.iii.Click the Species tab and enter0.2097and0.1for o2and o3respectively.iv.Click OK to close the Velocity Inlet panel.2.Deﬁne the boundary conditions for leftwall.(a)Select leftwall from the Zone selection list.(b)Select phase-2from the Phase drop-down list and click the Set...button to openthe Wall panel.i.Select Specularity Coeﬃcient from the Shear Condition list and enter0.5forSpecularity Coeﬃcient.ii.Click OK to close the Wall panel.3.Deﬁne the boundary conditions for the rightwall zone identical to that of the leftwall.4.Close the Boundary Conditions panel.Step8:AdaptionA small region will be adapted in order to create a register so that the solid volume fraction can be patched.1.Adapt the the regions to be patched.Adapt−→Region...(a)Enter0and0.115for X Min and X Max respectively.(b)Enter0and10for Y Min and Y Max respectively.(c)Click Mark.FLUENT will report the number of cells marked for adaption in the console.Clicking the Manage...button will open the Manage Adaption Registers panel.The name of the register created will be hexahedron-r0.(d)Close the Region Adaption panel.Step9:Solution1.Set the solution parameters.Solve−→Controls−→Solution...(a)Deselect Energy from the Equations selection list.(b)Enter0.7and0.3for Pressure and Momentum respectively.Note:You will have to scroll down Under-Relaxation Factors to see the remaining parameters.(c)Enter1.0for Granular Temperature.(d)Select Second Order Upwind from the Momentum,Energy,phase-1o2and phase-1o3drop-down lists.(e)Select QUICK from the Volume Fraction drop-down list.(f)Click OK to close the Solution Controls panel.2.Enable the plotting of residuals during the calculation.Solve−→Monitors−→Residual...3.Initialize the solution.Solve−→Initialize−→Initialize...(a)Change the initial phase-1X Velocity to0.01.(b)Change the initial phase-1o2to0.233(composition of oxygen in air).(c)Retain all other default initial values.(d)Click Init and close the Solutio Initialization panel.4.Patch the initial sand bed conﬁguration.Solve−→Initialize−→Patch...(a)Select phase-2from the Phase drop-down list.(b)Select Volume Fraction from the Variable selection list.(c)Select hexahedron-r0from the Registers To Patch selection list.(d)Enter0.52for Value.(e)Click Patch and close the Patch panel.After initializing the entire domain of yourﬂowﬁeld,you can enter diﬀerent initial-ization values for particular variables into diﬀerent cells.This is known as patching and is generally used if you have multipleﬂuid zones that you want to patch with diﬀerent values.5.Set the time stepping parameters.Solve−→Iterate...(a)Enter0.001for Time Step Size and10000for Number of Time Steps.(b)Select Fixed from the Time Stepping Method list.(c)Enable Data Sampling for Time Statistics.This will allow you to sample data at a frequency that is set by you.(d)Enter40for Max Iterations per Time Step.(e)Click Apply.6.Save the initial case and dataﬁles(ozone fluidbed.cas.gz andozone fluidbed.dat.gz).File−→Write−→Case&Data...7.Save the dataﬁles every1000time steps.File−→Write−→Autosave...(a)Enter1000for Autosave Data File Frequency.(b)Enter ozoneﬂuidbed%t.dat.gz for Filename.(c)Click OK to close the Autosave Case/Data panel.8.Click Iterate to run the calculation for10seconds in the Iterate panel.Step10:PostprocessingYou will now examine the progress of the sand and ozone/air mixture in theﬂuidized bed after a total of10seconds.Theﬂuidized bed should have reached a steadyﬂow solution at this time.1.Plot contours of mass fraction for oxygen and ozone species.Display−→Contours...(a)Select Species...and Mass fraction of o3from the Contours of drop-down list.(b)Enable Filled from the Options list.(c)Click Display.The O3mass fraction contours are shown in Figure3.(d)Similarly plot the mass fraction contours of O2.The mass fraction contours of O2is shown in Figures4.In Figure3you can see that O3is almost fully decomposed as it approaches the outlet of theﬂuidized bed.Figure3:O3Mass FractionFigure4:O2Mass Fraction2.View the phase motion by displaying plots of velocity vectors for the gas and solidphases.Display−→Vectors...(a)Select Velocity from the Vectors of drop-down list and phase-1from the Phasedrop-down lists.(b)Select Velocity...and Velocity Magnitude from the Color by drop-down list andphase-1from the Phase drop-down list.(c)Enter5for Scale and2for Skip to improve visualization of the velocity vectors.(d)Click Display.The phase-1velocity vectors are shown in Figure5.(e)Select phase-2from the Phase drop-down list to plot the phase-2velocity vectors.The phase-2velocity vectors are shown in Figure6.Figure5:Velocity Vectors for Phase-1Figure6:Velocity Vectors for Phase-23.Displayﬁlled contours of Phases...by Volume fraction for phase-1.Display−→Contours...(a)Select Phases...and Volume fraction from the Contours of drop-down list.(b)Select phase-1from the Phase drop-down list.(c)Click Display.The contours of volume fraction for phase-1are shown in Figure7.Figure7:Volume Fraction for Phase-1pare the mass fraction of O3and O2at the pressure outlet of theﬂuidized bed.Plot−→XY Plot...(a)Display an XY plot of mass fraction of O2.i.Select Species...and Mass fraction of o2from the Y Axis Function drop-downlist.ii.Retain the default selection of Direction Vector from the X Axis Function drop-down list.iii.Select outlet from the Surfaces selection list.iv.Enter0for X Plot Direction and1for Y Plot Direction.v.Click Plot.(b)Similarly,display an XY plot of mass fraction of O3by selecting Mass fraction ofo3from the Y Axis Function drop-down list.(c)Compare the O2and O3XY plots for mass fraction in Figure8and Figure9.Figure8:XY Plot of Mass Fraction of O3Figure9:XY Plot of Mass Fraction of O2SummaryThis tutorial demonstrated how to set up and solve a granular multiphase problem using the Eulerian multiphase model with species transport and reaction.The problem involved the2D modeling of particle suspension in aﬂuidized bed,and postprocessing showed the near-steady-state behavior of the sand in theﬂuidized bed,under the assumptions made. Such cases should be typically run for a total of40seconds of operation,however,as this is very computationally intensive,this case was only run for10seconds for demonstration in this tutorial.。

流化床干燥综合3D虚拟仿真试验项目操作说明

流化床干燥综合3D虚拟仿真实验项目操作说明流化床干燥综合3D虚拟仿真实验项目是利用动态数学模型实时模拟真实实验流化床干燥的现象和过程，通过3D 仿真实验装置交互式操作，产生和真实实验相一致的实验现象和结果。

根据学生的需求与知识结构，构建了两个层次（基础理论型、仿真操作型）四个教学单元的实验内容，使实践教学内容由验证理论向综合应用、研究设计延伸，使不同层次、不同类型的学生都能在本仿真项目中，根据自己的需要来进行自主学习。

能够体现化工实验步骤和数据梳理等基本实验过程，满足工艺操作要求，满足流程操作训练要求，能够安全、长周期运行。

既能让每位学生都能亲自动手做实验，观察实验现象，记录实验数据，达到验证公式和原理的目的，且能够进一步通过对设备参数的改变，来加深对知识点和原理的理解。

一、干燥工艺及相关设备的认识本单元主要包括干燥工艺的主要原理、流程、设备及过程特点等，并拓展介绍相关的流体输送设备、传热流程及设备。

通过手动设备拆装，观察流化床干燥器内部构件，达到了解其整体结构的目的。

二、流化床干燥单元操作的开车、停车本单元的主要目的是让学生掌握流化床干燥单元的开、停车方法过程中所需要控制的相关参数等。

在这一单元，采用指导模式和自主操作两种学习方式。

指导模式的学习，是学生在软件提示下，进行设备的开停车步骤操作。

学生也可以选择自主操作模式，自主操作设备的开车、正常运行和停车步骤。

基本操作1、快捷键操作：W（前）S（后）A（左）D（右）、鼠标右键（视角旋转）。

图 1-1注：在非中文输入状态下，点击 W 可逐步放大页面，点击 A 界面右移，可使左边装置进入视角，点击 D 界面左移，可使右边装置进入视角，点击 S，退出拉近，界面恢复。

2、进入主场景后，可进入相应实验室，如流体力学实验室，完成实验的全部操作，进入实验室后可回到主场景中。

按住鼠标滚轮上下移动鼠标可进行视角的调整。

3、拉近镜头：鼠标左键双击设备进行操作，还可使用快捷键 W。

聚乙烯流化床反应器床内温度分布的模拟

聚乙烯流化床反应器床内温度分布的模拟聚乙烯是一种广泛应用的塑料，其生产过程中需要使用一些特殊的反应器，其中流化床反应器是一种常用的设备。

在流化床反应器中，聚乙烯颗粒被加热至高温，然后通过催化剂进行反应，最终形成聚乙烯产品。

在这个过程中，反应器床内的温度分布对反应的效率和产品质量都有着重要的影响。

因此，模拟反应器床内温度分布是一个非常重要的课题。

本文将介绍聚乙烯流化床反应器床内温度分布的模拟方法和结果。

首先，我们将介绍流化床反应器的基本原理和反应机理。

然后，我们将详细介绍模拟方法，包括数值模拟的基本原理和计算流体力学（CFD）模拟方法。

最后，我们将呈现模拟结果，并对结果进行分析和讨论。

一、流化床反应器的基本原理和反应机理流化床反应器是一种将反应物料放在气体流动中进行反应的设备。

在流化床反应器中，催化剂通常被放置在一个床层中，并被气体携带到反应物料中进行反应。

在聚乙烯生产中，反应物料通常是乙烯气体，而催化剂则是一种Ziegler-Natta催化剂。

聚乙烯的反应机理比较复杂，但可以简单地概括为以下几个步骤：1. 乙烯气体被吸附在催化剂表面。

2. 催化剂与乙烯气体反应，形成聚合物链。

3. 聚合物链不断生长，直到达到一定长度。

4. 聚合物链脱离催化剂表面，成为自由的聚合物。

5. 自由的聚合物不断生长，直到形成聚乙烯颗粒。

在这个过程中，床层内的温度对反应的速率和产物的质量都有着非常重要的影响。

二、模拟方法1. 数值模拟的基本原理数值模拟是一种通过计算机模拟物理现象的方法。

在模拟过程中，将物理现象分割成许多小的区域，并在每个区域中进行计算。

这种方法可以帮助我们更好地理解物理现象，并预测未来的变化。

2. 计算流体力学（CFD）模拟方法计算流体力学（CFD）是一种通过计算机模拟流体力学现象的方法。

在CFD模拟中，将流体分割成小的区域，并在每个区域中进行计算。

这种方法可以帮助我们更好地理解流体力学现象，并预测未来的变化。

灰熔聚流化床气化炉内气固两相流的数值模拟

熔融状态下相互碰撞，黏结成含碳量较低的灰球排出炉外．１］内的气固混合特性是认识ＩＣ炉内［炉Ｃ
传热的传质机理的关键，提高ＩＣ效率及碳转化对Ｃ
率有着重要意义．研究基于欧拉双流体模型，本利用
ＣＤ软件ＦＮＴ对某化肥厂现运行ＩＣ内的气ＦＩＵＥＣ固混合特性进行数值模拟¨６，析流化气速与喷动３】分＿气速对气固混合的影响，ＩＣ的优化设计和运行提为Ｃ
供参考．］ｆ
图１几何模型
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１２
５ｍ／，于２ｓ合理的Ｖｆ，存在一最佳ｓ小５ｍ／．ｇ必下Ｖ，炉内气体分布结构满足ＩＣ要求，使Ｃ且气固混
合效果最好．一结论不会随静止床层高度的变化这
０引言
中国科学院山西煤炭化学研究所开发的具有特殊气体分布结构的ＩＣ，Ｃ解决了传统流化床煤气化炉排渣含碳量高的问题，其关键技术是在炉内中心
射流区形成局部高温，煤充分燃烧，使煤灰在软而未
示）内的气固两相流动行为，出了所模拟ＩＣ的合理流化气速与喷动气速的速度范围及匹配关得Ｃ系：化气速不能太小，则布风板区域会出现死区；化气速也不能太大，则将失去ＩＣ的设流否流否Ｃ

循环流化床烟气脱硫塔内气液两相流场数值模拟

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环流化床脱硫技术进行进一步研究有重要的意义。影响循环流化床脱硫率的最大因素之一就是气液固三相是否能够有效均匀的混合反应［。本文是以某热电有限公司所使用的循环流化床脱硫塔为研究５］对象，采用ＦＵＮＬＥＴ软件来模拟脱硫塔内部流场的变化情况，主要是关注于气液两相流，不考虑固体脱硫剂的喷人情况，只考虑被处理烟气与雾化水混合的流场情况，即不带化学反应的气液两相流动 …。
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喷嘴布置
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三维喷动流化床流动特性数值模拟

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流化床操作流程

流化床操作规程一、设备安装1. 设备部件WBF-2G型多功能实验机主要由：机箱箱体、流化装置、空气过滤装置、加热装置、抖袋清粉装置、过滤室装置、气控装置、电控装置等工艺过程的公用系统组成，按工艺要求分别配备顶喷装置、底喷装置、侧喷装置各一套。

顶喷喷枪和底喷喷枪是可拆卸和组合的一套喷枪组合。

如选用底喷工艺或顶喷工艺，只需要换相应配套装置和喷枪就能满足该工艺要求：与主机相配套的机构有：蠕动泵、同时配备380V∕50HZ（三相四线）交流电源和0.4〜0.6MPa压缩空气等组成一个完整的工艺流程控制系统。

该设备与配套装备只需要放在水平地面上，主机出风口管道接至实验室户外，机箱接地导线可靠安全，接地电阻R≤100? ，接通电源和压缩空气就可运行；2. 过滤室装置的安装2.1 将过滤室装置的元盘安装座按照工作台面上的对应位置，先将控制管线对应穿插在其孔内，然后竖立起过滤室装置，用安装螺丝对应连接孔连接好；2.2 根据电气原理图，将控制线、出风温度传感器、控制用的气管等连接到位；并检查其可靠性。

3. 顶喷装置、底喷装置的安装根据工艺操作选择顶喷或者底喷装置3.1 顶喷装置先将顶喷过度段装置与顶喷物料筒连接好，然后将整个顶喷物料筒装置的支撑轴连接在过滤室支座的连接套筒内；嵌入密封条；安装好喷枪；3.2 底喷装置先将喷枪安装在底喷过度段装置上，然后与底喷物料筒连接好，将整个底喷物料筒装置的支撑轴连接在过滤室支座的连接套筒内；嵌入密封条；4. 滤袋架及滤袋的安装4.1 该安装顺序必须在设备的空机动作调试正确后，才能进行；4.2 接通电源和起源，按照操作步骤进行操作至放滤袋架，将准备好的滤袋按照滤袋架的形状要求系好，分别将滤袋架卡接在抖袋汽缸接口上；二、设备调试1. 顶喷装置、底喷装置的升降调试选择一种工艺操作模式，接通电源和起源，按照操作步骤进行，反复点击容器升降按键，调试升、降顺序和装置升降的活动性；2. 喷枪雾化效果的调试将压缩空气接入喷枪，启动系统至喷雾运行状态，调节供液频率和雾化压力可改变雾化效果；颗粒成型原理：雾滴大小与液体流量成正比，与雾化压力成反比雾化角度（微调）可通过雾化压力和调试喷枪头的空气帽来完成。

流化床中的CFD-DEM耦合模拟

Ii 指的是颗粒惯性矩 i 指的是颗粒角速度
Fd ,i 为流体作用于当前运动颗粒的曳力
Fp,i 为颗粒所受到流体作用力的压力梯度力
Fc,ij 为颗粒i与颗粒j之间的接触作用力；颗粒和壁面接触时，将壁面视为一个具有无限大直径的静
止颗粒，以此来计算两者之间的作用力和力矩。
三、CFD-DEM数学模型
颗粒相运动方程 Fd ,i
四、计算模型及边界条件
四、计算模型及边界条件
床体底部采用均匀速度入口，而其出口则釆用压力出口边界条件。对管壁和左右壁面，则采用无滑移壁面边界条件来进行计算。对温度边界条件的设定，入流气体温度设定为293K，埋管壁面温度固定为373K，其余边界条件则设定为Neumann边界条件。
在计算过程中，对固相和气相运动的时间步分别设定为1X10^-7s和1X10^-5s。对在不同流化风速下进行的每个计算算例，均进行了15s的计算。但对床体内时均特性的统计，则在 10s后计算数据上进行。
流体作用于当前运动颗粒的曳力
gs 为曳力系数
Vp 为颗粒体积为当前网格内流体速度矢量
vp 为颗粒的速度矢量 p 为当前计算网格内的固相浓度
f 为空隙率 p 1 f
三、CFD-DEM数学模型
颗粒相运动方程 f
颗粒切割法，即按照一定的数值算法将单个颗粒分为许多个颗粒元，根据每个颗粒元的位置探测其所在的计算网格，得到该颗粒在该网格内的体积份额，以此来计算整个流场网格内的空隙率。假定在计算过程中将单个颗粒分割为个部分，分别根据每个部分的质心得到其所在计算网格。对计算网格，其内的空隙率计算为：
二、CFD-DEM耦合思路
气相运动的计算釆用欧拉方法在计算网格单元尺度上进行求解（CFD方法）；固相运动则采用离散单元法（DEM方法）在颗粒尺度进行跟踪，即拉格朗日法。

循环流化床操作规程

循环流化床操作规程
《循环流化床操作规程》
一、概述
循环流化床是一种高效的固体颗粒流态化技术，广泛应用于化工、冶金、环保等领域。

为了保证循环流化床的安全运行和有效操作，制定了循环流化床操作规程，以规范操作人员的行为，确保设备正常运行。

二、操作人员要求
1. 操作人员应具备相关专业知识和技能，并接受相关培训。

2. 操作人员应遵守相关操作规程和安全规定，严格执行操作程序。

3. 操作人员应熟悉循环流化床的结构和工作原理，了解设备主要部件的性能和用途。

三、操作步骤
1. 开车前检查：操作人员应在开车前对设备进行检查，确保设备处于正常运行状态。

2. 启动设备：按照操作规程操作控制系统，逐步启动设备。

3. 填料操作：根据生产计划和工艺要求，按照操作规程进行填料操作。

4. 操作监控：在设备运行过程中，操作人员应随时监控设备运行情况，及时发现并处理异常情况。

5. 清洗维护：设备运行结束后，操作人员应按照操作规程对设备进行清洗和维护，确保设备的正常运行。

四、安全措施
1. 操作人员应严格按照安全操作规程进行操作，避免发生意外事故。

2. 操作人员应穿戴好相关个人防护用品，确保自身安全。

3. 操作人员应定期参加相关安全培训，提高安全意识和技能。

五、记录和报告
操作人员应按照操作规程填写相关操作记录，并在发现设备异常或故障时及时上报。

总之，循环流化床操作规程对于确保设备运行安全、稳定和高效具有重要意义，操作人员应严格遵守规程，确保设备的正常运行。

FLUENT操作过程及全参数选择

振动流化床仿真操作过程及参数选择1创建流化床模型。

根据靳海波论文提供的试验机参数，创建流化床模型。

流化床直148mm，高1m，开孔率9%，孔径2mm。

在筛板上铺两层帆布保证气流均布。

因为实验机为一个圆形的流化床，所以可简化为仅二维模型。

而实际实验中流化高度远小于1m，甚至500mm，所以为提高计算时间，可将模型高度缩为500mm。

由于筛板上铺设两层帆布以达到气流均分的目的，所以认为沿整个筛板的进口风速为均匀的。

最终简化模型如下图所示：上图为流化后的流化床模型，可以看出流化床下端的网格相对上端较密，因为流化行为主要发生的流化床下端，为了加快计算时间，所以采用这种下密上疏的划分方式。

其中进口设置为velocity inlet；出口设置为outflow；左右两边分为设置为wall。

在GAMBIT中设置完毕后，输出二维模型vfb.msh。

outflow边界条件不需要给定任何入口的物理条件，但是应用也会有限制，大致为以下四点：1.只能用于不可压缩流动2.出口处流动充分发展3.不能与任何压力边界条件搭配使用（压力入口、压力出口）4.不能用于计算流量分配问题（比如有多个出口的问题）2打开FLUENT 6.3.26，导入模型vfb.msh点击GRID—CHECK，检查网格信息及模型中设置的信息，核对是否正确，尤其查看是否出现负体积和负面积，如出现马上修改。

核对完毕后，点击GRID-SCALE弹出SCALE GRID窗口，设置单位为mm，并点击change length unit 按钮。

具体设置如下：3设置求解器保持其他设置为默认，更改TIME为unsteady，因为实际流化的过程是随时间变化的。

（1）pressure based 求解方法在求解不可压流体时，如果我们联立求解从动量方程和连续性方程离散得到的代数方程组，可以直接得到各速度分量及相应的压力值，但是要占用大量的计算内存，这一方法已可以在Fluent6.3中实现，所需内存为分离算法的1.5-2倍。

旋转流化床粉体混合机混合效果数值模拟和实验验证

CHEMICAL INDUSTRY AND ENGINEERING PROGRESS 2018年第37卷第9期·3294·化工进展旋转流化床粉体混合机混合效果数值模拟和实验验证陈程1，刘雪东1,2，罗召威1，崔树旗1，谈志超1（1常州大学机械工程学院，江苏常州 213164；2江苏省绿色过程装备重点实验室，江苏常州 213164）摘要：为了对旋转流化床粉体混合机进行优化设计，采用CFD-DEM 联合仿真的方法，对旋转流化床粉体混合机内球形颗粒的混合过程进行数值模拟，通过Lacey 指数具体评价颗粒的混合效果，研究了进气管倾斜角度、进气管布置方式、进气方式对球形颗粒混合效果的影响，并进行球形颗粒混合实验验证。

结果表明，进气管最合适的倾斜角度应保证气流作用区域面积恰好为底部颗粒物料区域面积的一半。

进气管水平布置时能够保证很好的混合质量及较快的混合速率。

脉冲及连续方式进气均能实现均匀混合，脉冲进气方式比连续进气方式耗气量更低。

颗粒混合实验有很好的混合效果，与数值模拟的结果具有较高的一致性，从而获得了一种混合效果优越的结构形式，进气管倾斜角度α=35°，水平布置。

关键词：旋转流化床；数值模拟；CFD-DEM 联合仿真；混合；优化设计中图分类号：TQ027.1 文献标志码：A 文章编号：1000–6613（2018）09–3294–09 DOI ：10.16085/j.issn.1000-6613.2018-0039Numerical simulation and experimental verification of mixing effect inrotating fluidized bed powder mixerCHEN Cheng 1，LIU Xuedong 1,2，LUO Zhaowei 1，CUI Shuqi 1，TAN Zhichao 1（1School of Mechanical Engineering ，Changzhou University ，Changzhou 213164，Jiangsu ，China ；2Jiangsu KeyLaboratory of Green Process Equipment ，Changzhou University ，Changzhou 213164，Jiangsu ，China ）Abstract ：In order to get structure optimal design of a rotating fluidized bed powder mixer, the mixing progress of spherical powder granules in a rotating fluidized bed powder mixer was simulated by a combined approach of computational fluid dynamics (CFD) and discrete element method (DEM). Lacey mix index was used to quantitatively analyze the mixing degree of granules in the mixer. The effects of different parameters including the tilt angle of the intake pipe, the arrangement of the intake pipe and intake method were studied respectively. To verify the mixing performance of the rotating fluidized bed powder mixer, a granule mixing experiment was carried out. Simulation results showed that the most appropriate angle of intake pipe should ensure the area of airflow is just half of the area of granular materials in the bottom of the mixer. Besides, if the intake pipe is horizontal arranged, effective mixing quality and mixing rate could be achieved. Moreover, whether the intake is continuous or pulsed, spherical granules could achieve uniform mixing. Compared with the continuous intake ，the air comsumption of pulsed intake was less. Finally, the powder mixing experimental results showed a positive mixing quality, which were in good agreement with the numerical data. It could be drawn that it is a structure with superior mixing effect if the intake pipe is tilted at an angle of 35 degrees and horizontal arranged.Key words ：rotating fluidized bed ；numerical simulation ；computational fluid dynamics - discrete element method coupling ；mixing ；optimal design研发。

流化床反应仿真操作单元指导书

流化床反应仿真操作单元指导书(总8页)本页仅作为文档封面，使用时可以删除This document is for reference only-rar21year.March《反应过程与技术》仿真操作指导书周波辽宁石化职业技术学院石油化工系流化床反应仿真操作单元一.工艺流程说明：该流化床反应器取材于HIMONT工艺本体聚合装置，用于生产高抗冲击共聚物。

具有剩余活性的干均聚物（聚丙烯），在压差作用下自闪蒸罐D-301流到该气相共聚反应器R-401。

在气体分析仪的控制下，氢气被加到乙烯进料管道中，以改进聚合物的本征粘度，满足加工需要。

聚合物从顶部进入流化床反应器，落在流化床的床层上。

流化气体（反应单体）通过一个特殊设计的栅板进入反应器。

由反应器底部出口管路上的控制阀来维持聚合物的料位。

聚合物料位决定了停留时间，从而决定了聚合反应的程度，为了避免过度聚合的鳞片状产物堆积在反应器壁上，反应器内配置一转速较慢的刮刀，以使反应器壁保持干净。

栅板下部夹带的聚合物细末，用一台小型旋风分离器S401除去，并送到下游的袋式过滤器中。

所有末反应的单体循环返回到流化压缩机的吸入口。

来自乙烯汽提塔顶部的回收气相与气相反应器出口的循环单体汇合，而补充的氢气，乙烯和丙烯加入到压缩机排出口。

循环气体用工业色谱仪进行分析，调节氢气和丙烯的补充量。

然后调节补充的丙烯进料量以保证反应器的进料气体满足工艺要求的组成。

用脱盐水作为冷却介质，用一台立式列管式换热器将聚合反应热撤出。

该热交换器位于循环气体压缩机之前。

共聚物的反应压力约为(表)，70℃，注意，该系统压力位于闪蒸罐压力和袋式过滤器压力之间，从而在整个聚合物管路中形成一定压力梯度，以避免容器间物料的返混并使聚合物向前流动。

反应机理:乙烯，丙烯以及反应混合气在一定的温度70度，一定的压力下，通过具有剩余活性的干均聚物（聚丙烯）的引发，在流化床反应器里进行反应，同时加入氢气以改善共聚物的本征粘度，生成高抗冲击共聚物。

FLUENT流化床模拟实例

Tutorial:Using the Eulerian Multiphase Model with Species TransportIntroductionFluidized beds are used in processes where gas/solid mass transfer is of importance.The de-composition of ozone(O3),using particles as a catalyst,creates a suitable low-temperature environment for mass transfer.This tutorial solves a gas/solidﬂow with a simple one-step ozone decomposition reaction in aﬂuidized bed.The reaction equation isO3→1.5O2(1) This tutorial demonstrates how to do the following:•Use the granular Eulerian multiphase model with species transport.•Deﬁne the rate of reaction with a user-deﬁned function(UDF).•Deﬁne the Syamlal-O’Brien drag correlation with a user-deﬁned function(UDF)usingappropriate parameters.•Set boundary conditions for internalﬂow.•Deﬁne theﬂuid and solid phases.•Calculate a solution using2D planar geometry in conjunction with the pressure-basedsolver.•Solve a time-accurate transient problem with data sampling for time statistics.PrerequisitesThis tutorial assumes that you are familiar with the FLUENT interface and that you have a good understanding of basic setup and solution procedures.Some steps will not be shown explicitly.In this tutorial you will use the Eulerian multiphase model with species transport.If you have not used this feature before,refer to the FLUENT6.3User’s Guide.Using the Eulerian Multiphase Model with Species TransportProblem DescriptionThe problem involves the transient startup of ozone decomposition in a ﬂuidized bed.The ﬂuid phase is a mixture of ozone and air,while the solid phase consists of sand particles with an 87.75micron diameter.A schematic of the ﬂuidized bed is shown in Figure 1.The domain is modeled as a 2D planar cylindricalcase.volume fraction 0.52 of solids pressure outlet uniform velocity inlet u = 0.08 m/s 0 Pa gauge Figure 1:Problem SpeciﬁcationUsing the Eulerian Multiphase Model with Species Transport Preparation1.Copy theﬁles2-D-FBed Ozone.msh.gz,rrate.c,and bp drag.c to your workingfolder.2.Start the2D double-precision(2ddp)version of FLUENT.Setup and SolutionStep1:Grid1.Read the gridﬁle(2-D-FBed_Ozone.msh).File−→Read−→Case...As FLUENT reads the gridﬁle,it will report its progress in the console.2.Check the grid.Grid−→CheckFLUENT will perform various checks on the mesh and will report the progress in the console.Make sure the minimum volume reported is a positive number.3.Display the grid using the default settings.Display−→Grid...Figure2:Grid Display4.Rotate the view so that the inlet of theﬂuidized bed is at the bottom.Display−→Views...Using the Eulerian Multiphase Model with Species Transport(a)Click the Camera...button to open the Camera Parameters panel.i.Drag the indicator of the dial with the left mouse button in the counter-clockwise direction until the upright view(-90◦)is displayed(Figure2).ii.Close the Camera Parameters panel.(b)Click the Save button in the Actions group box in the Views panel to save theupright view.When you do this,view-0will be added to the list of Views.(c)Close the Views panel.You can use the probe mouse button to check which zone number corresponds to eachboundary.If you click the probe mouse button on one of the boundaries in the graphicswindow,its zone number,name,and type will be printed in the FLUENT console.Thisfeature is especially useful when you have several zones of the same type and you wantto distinguish between them quickly.Using the Eulerian Multiphase Model with Species Transport Step2:Models1.Specify a transient,2D model.Deﬁne−→Models−→Solver...(a)Retain the default selection of Pressure Based from the Solver list and2D fromthe Space list.The pressure based solver must be used for multiphase calculations.(b)Select Unsteady from the Time list.(c)Click OK to close the Solver panel.2.Deﬁne the multiphase model.Deﬁne−→Models−→Multiphase...(a)Select Eulerian from the Model list.The panel will expand to show the inputs for the Eulerian model.Using the Eulerian Multiphase Model with Species Transport(b)Retain the default value of2for Number of Phases.(c)Click OK to close the Multiphase Model panel.3.Deﬁne the species model.Deﬁne−→Models−→Species−→Transport&Reaction...(a)Select Species Transport from the Model list.The Species Model panel will expand.(b)Enable Volumetric from the Reactions group box.(c)Disable Diﬀusion Energy Source from the Options group box.(d)Click OK to close the Species Model panel.Using the Eulerian Multiphase Model with Species Transport FLUENT will list the properties required for the models that you enabled,in theconsole.An Information dialog box will appear,reminding you to conﬁrm theproperty values that have been extracted from the database.(e)Click OK in the Information dialog box to continue.Step3:MaterialsDeﬁne−→Materials...1.Create a new material called air+ozone.(a)Click the Fluent Database...button to open the Fluent Database Materials panel.i.Selectﬂuid from the Material Type drop-down list.ii.Select ozone(o3)from the Fluent Fluid Materials selection list.iii.Click Copy to copy the information for ozone to your model and close the Fluent Database Materials panel.(b)Select mixture from the Material Type drop-down list.(c)Enter air+ozone for Name.(d)Click Change/Create.When you click Change/Create,a Question dialog box will appear,asking you ifmixture-template should be overwritten.Click No to retain mixture-template andadd the new material,air+ozone,to the list.The Materials panel will be updatedto show the new material name in the Fluent Mixture Materials list.Using the Eulerian Multiphase Model with Species Transport2.Click the Edit...button to the right of the Mixture Species drop-down list to open theSpecies panel.You will select the species that are involved in the decomposition of ozone.The orderof the species in the Selected Species list is important.Perform the following steps to achieve the proper order:(a)Select water-vapor(h2o)from the Selected Species selection list and click theRemove button to move it to the Available Materials selection list.(b)Similarly,remove n2from the Selected Species list.(c)Select ozone(o3)from the Available Materials selection list and click the Addbutton.(d)Similarly,add n2back in the Selected Species list.The Selected Species list should now contain o2,o3,and n2,respectively.(e)Click OK to close the Species panel.Using the Eulerian Multiphase Model with Species Transport 3.Click the Edit...button to the right of the Reaction drop-down list to open the Reac-tions panel.(a)Select o3from the Species drop-down list in the Reactants group box and enter1for both Stoich.Coeﬃcient and Rate Exponent.(b)Select o2from the Species drop-down list in the Products group box and enter1.5for Stoich.Coeﬃcient and0for Rate Exponent,respectively.There is no need to modify the Arrhenius Rate constants,as a UDF will be used to deﬁne them in Step4.(c)Click OK to close the Reactions panel.4.Retain the default settings in the Reaction Mechanisms panel.5.Select volume-weighted-mixing-law from the Density drop-down list.Thermal properties do not need to be speciﬁed since this is an isothermal case.6.Retain the default value of1.72e-05for Viscosity.7.Click Change/Create.Using the Eulerian Multiphase Model with Species Transport8.Create a new material called solids.In theﬂuidized bed the solid particles(treated as aﬂuid)are held in suspension by theair+ozone mix injected at the bottom of the bed.(a)Selectﬂuid from the Material Type drop-down list.(b)Select water-vapor(h2o)from the Fluent Fluid Materials drop-down list.(c)Enter solids for Name.(d)Enter silica for Chemical Formula.(e)Enter2650kg/m3for Density.(f)Click Change/Create and close the Materials panel.When you click Change/Create,a question dialog box will appear,asking you ifwater-vapor(h2o)should be overwritten.Click No to retain water-vapor(h2o)and add the new material,solids,to the list.The Materials panel will be updatedto show the new material name in the Fluent Fluid Materials list.You can remove materials that are not required to run this case by selecting mix-ture in the Material Type in the Materials panel.Under Fluent Mixture Materials,select mixture-template from the drop-down list and click the Delete button.Simi-larly,selectﬂuid in the Material Type and delete all Fluent Mixture Materials otherthan O2,O3,N2,air and silica.9.Specify the species for the gaseous phase(phase-1)and the sand bed phase(phase-2).Deﬁne−→Models−→Species−→Transport&Reaction...(a)Select phase-1from the Phase drop-down list and click the Set...button to openthe Phase Properties panel.i.Select air+ozone from the Material drop-down list.ii.Click OK to close the Phase Properties panel.(b)Select phase-2from the Phase drop-down list and click the Set...button to openthe Phase Properties panel.i.Select solids from the Material drop-down list.ii.Click OK to close the Phase Properties panel.(c)Click OK to close the Species Model panel.Step4:User-Deﬁned Functionspile the user-deﬁned functions.Deﬁne−→User-Deﬁned−→Functions−→Compiled...(a)Click the Add...button in the Source Files group box to open the Select Filepanel.(b)Select theﬁles,rrate.c and bp drag.c and click OK.The bp drag.c source code is a routine for customizing the default Syamlal-O’Briendrag law in FLUENT.In the solid phase,the default drag law uses coeﬃcientsof0.8(for voids≤0.85)and2.65(for voids>0.85),for minimumﬂuid ve-locities of0.25m/s.The current drag law has been modiﬁed to accommodate aminimumﬂuid velocity of0.08m/s.The source code,rrate.c,deﬁnes a customvolumetric reaction rate for the decomposition reaction of ozone.(c)Click Build to build the library.(d)Click Load to load the UDF.FLUENT will build a libudf folder and compile the UDF.A dialog box will appear warning you to make sure that UDF sourceﬁles are inthe folder that contain your case and dataﬁles.Click OK in the dialog box.(e)Close the Compiled UDFs panel.2.Specify the volume reaction rate function.Deﬁne−→User-Deﬁned−→Function Hooks...(a)Select rrate::libudf from the Volume Reaction Rate Function drop-down list.(b)Click OK to close the User-Deﬁned Function Hooks panel.Step5:Phases1.Deﬁne the granular secondary phase.Deﬁne−→Phases...(a)Select phase-2and click the Set...button.i.Enable Granular.ii.Deﬁne the properties of the solid phase as shown in the table:Parameters ValuesDiameter8.775e-05mGranular Viscosity syamlal-obrienGranular Bulk Viscosity lun-et-alFrictional Viscosity schaeﬀerAngle of Internal Friction30degreesGranular Temperature algebraicSolids Pressure syamlal-obrienRadial Distribution syamlal-obrienElasticity Modulus derivePacking Limit0.53Note:You will have to scroll down the Properties list to see the remaining options.iii.Click OK to close the Secondary Phase panel.2.Specify the drag law to be used for computing the interphase momentum transfer.(a)Click the Interaction...button to open the Phase Interaction panel.i.Select user-deﬁned from the Drag Coeﬃcient drop-down list to open the User-Deﬁned Functions panel.A.Select custom drag syam::libudf and click OK to close the User-DeﬁnedFunctions panel.ii.Click the Collisions tab and enter0.8for Constant Restitution Coeﬃcient.iii.Click OK to close the Phase Interaction panel.3.Close the Phases panel.Step6:Operating ConditionsSet the gravitational acceleration.Deﬁne−→Operating Conditions...1.Enable Gravity.The panel will expand to show additional inputs.2.Enter-9.81m/s2for Gravitational Acceleration in the X direction.3.Enter297K for Operating Temperature.4.Click OK to close the Operating Conditions panel.Step7:Boundary ConditionsDeﬁne−→Boundary Conditions...1.Set the conditions for the gaseous phase(phase-1).(a)Select Inlet from the Zone selection list.(b)Select phase-1from the Phase drop-down list and click the Set...button to openthe Velocity Inlet panel.i.Enter0.08m/s for Velocity Magnitude.ii.Click the Thermal tab and enter293K for Temperature.iii.Click the Species tab and enter0.2097and0.1for o2and o3respectively.iv.Click OK to close the Velocity Inlet panel.2.Deﬁne the boundary conditions for leftwall.(a)Select leftwall from the Zone selection list.(b)Select phase-2from the Phase drop-down list and click the Set...button to openthe Wall panel.i.Select Specularity Coeﬃcient from the Shear Condition list and enter0.5forSpecularity Coeﬃcient.ii.Click OK to close the Wall panel.3.Deﬁne the boundary conditions for the rightwall zone identical to that of the leftwall.4.Close the Boundary Conditions panel.Step8:AdaptionA small region will be adapted in order to create a register so that the solid volume fraction can be patched.1.Adapt the the regions to be patched.Adapt−→Region...(a)Enter0and0.115for X Min and X Max respectively.(b)Enter0and10for Y Min and Y Max respectively.(c)Click Mark.FLUENT will report the number of cells marked for adaption in the console.Clicking the Manage...button will open the Manage Adaption Registers panel.The name of the register created will be hexahedron-r0.(d)Close the Region Adaption panel.Step9:Solution1.Set the solution parameters.Solve−→Controls−→Solution...(a)Deselect Energy from the Equations selection list.(b)Enter0.7and0.3for Pressure and Momentum respectively.Note:You will have to scroll down Under-Relaxation Factors to see the remaining parameters.(c)Enter1.0for Granular Temperature.(d)Select Second Order Upwind from the Momentum,Energy,phase-1o2and phase-1o3drop-down lists.(e)Select QUICK from the Volume Fraction drop-down list.(f)Click OK to close the Solution Controls panel.2.Enable the plotting of residuals during the calculation.Solve−→Monitors−→Residual...3.Initialize the solution.Solve−→Initialize−→Initialize...(a)Change the initial phase-1X Velocity to0.01.(b)Change the initial phase-1o2to0.233(composition of oxygen in air).(c)Retain all other default initial values.(d)Click Init and close the Solutio Initialization panel.4.Patch the initial sand bed conﬁguration.Solve−→Initialize−→Patch...(a)Select phase-2from the Phase drop-down list.(b)Select Volume Fraction from the Variable selection list.(c)Select hexahedron-r0from the Registers To Patch selection list.(d)Enter0.52for Value.(e)Click Patch and close the Patch panel.After initializing the entire domain of yourﬂowﬁeld,you can enter diﬀerent initial-ization values for particular variables into diﬀerent cells.This is known as patching and is generally used if you have multipleﬂuid zones that you want to patch with diﬀerent values.5.Set the time stepping parameters.Solve−→Iterate...(a)Enter0.001for Time Step Size and10000for Number of Time Steps.(b)Select Fixed from the Time Stepping Method list.(c)Enable Data Sampling for Time Statistics.This will allow you to sample data at a frequency that is set by you.(d)Enter40for Max Iterations per Time Step.(e)Click Apply.6.Save the initial case and dataﬁles(ozone fluidbed.cas.gz andozone fluidbed.dat.gz).File−→Write−→Case&Data...7.Save the dataﬁles every1000time steps.File−→Write−→Autosave...(a)Enter1000for Autosave Data File Frequency.(b)Enter ozoneﬂuidbed%t.dat.gz for Filename.(c)Click OK to close the Autosave Case/Data panel.8.Click Iterate to run the calculation for10seconds in the Iterate panel.Step10:PostprocessingYou will now examine the progress of the sand and ozone/air mixture in theﬂuidized bed after a total of10seconds.Theﬂuidized bed should have reached a steadyﬂow solution at this time.1.Plot contours of mass fraction for oxygen and ozone species.Display−→Contours...(a)Select Species...and Mass fraction of o3from the Contours of drop-down list.(b)Enable Filled from the Options list.(c)Click Display.The O3mass fraction contours are shown in Figure3.(d)Similarly plot the mass fraction contours of O2.The mass fraction contours of O2is shown in Figures4.In Figure3you can see that O3is almost fully decomposed as it approaches the outlet of theﬂuidized bed.Figure3:O3Mass FractionFigure4:O2Mass Fraction2.View the phase motion by displaying plots of velocity vectors for the gas and solidphases.Display−→Vectors...(a)Select Velocity from the Vectors of drop-down list and phase-1from the Phasedrop-down lists.(b)Select Velocity...and Velocity Magnitude from the Color by drop-down list andphase-1from the Phase drop-down list.(c)Enter5for Scale and2for Skip to improve visualization of the velocity vectors.(d)Click Display.The phase-1velocity vectors are shown in Figure5.(e)Select phase-2from the Phase drop-down list to plot the phase-2velocity vectors.The phase-2velocity vectors are shown in Figure6.Figure5:Velocity Vectors for Phase-1Figure6:Velocity Vectors for Phase-23.Displayﬁlled contours of Phases...by Volume fraction for phase-1.Display−→Contours...(a)Select Phases...and Volume fraction from the Contours of drop-down list.(b)Select phase-1from the Phase drop-down list.(c)Click Display.The contours of volume fraction for phase-1are shown in Figure7.Figure7:Volume Fraction for Phase-1pare the mass fraction of O3and O2at the pressure outlet of theﬂuidized bed.Plot−→XY Plot...(a)Display an XY plot of mass fraction of O2.i.Select Species...and Mass fraction of o2from the Y Axis Function drop-downlist.ii.Retain the default selection of Direction Vector from the X Axis Function drop-down list.iii.Select outlet from the Surfaces selection list.iv.Enter0for X Plot Direction and1for Y Plot Direction.v.Click Plot.(b)Similarly,display an XY plot of mass fraction of O3by selecting Mass fraction ofo3from the Y Axis Function drop-down list.(c)Compare the O2and O3XY plots for mass fraction in Figure8and Figure9.Figure8:XY Plot of Mass Fraction of O3Figure9:XY Plot of Mass Fraction of O2SummaryThis tutorial demonstrated how to set up and solve a granular multiphase problem using the Eulerian multiphase model with species transport and reaction.The problem involved the2D modeling of particle suspension in aﬂuidized bed,and postprocessing showed the near-steady-state behavior of the sand in theﬂuidized bed,under the assumptions made. Such cases should be typically run for a total of40seconds of operation,however,as this is very computationally intensive,this case was only run for10seconds for demonstration in this tutorial.。

流化床操作流程

流化床操作规程一、设备安装1.设备部件WBF-2G型多功能实验机主要由：机箱箱体、流化装置、空气过滤装置、加热装置、抖袋清粉装置、过滤室装置、气控装置、电控装置等工艺过程的公用系统组成，按工艺要求分别配备顶喷装置、底喷装置、侧喷装置各一套。

顶喷喷枪和底喷喷枪是可拆卸和组合的一套喷枪组合。

如选用底喷工艺或顶喷工艺，只需要换相应配套装置和喷枪就能满足该工艺要求：与主机相配套的机构有：蠕动泵、同时配备380V/50HZ（三相四线）交流电源和0.4～0.6MPa压缩空气等组成一个完整的工艺流程控制系统。

该设备与配套装备只需要放在水平地面上，主机出风口管道接至实验室户外，机箱接地导线可靠安全，接地电阻R≤ 100Ω，接通电源和压缩空气就可运行；2.过滤室装置的安装2.1将过滤室装置的元盘安装座按照工作台面上的对应位置，先将控制管线对应穿插在其孔内，然后竖立起过滤室装置，用安装螺丝对应连接孔连接好；2.2根据电气原理图，将控制线、出风温度传感器、控制用的气管等连接到位；并检查其可靠性。

3.顶喷装置、底喷装置的安装根据工艺操作选择顶喷或者底喷装置3.1顶喷装置先将顶喷过度段装置与顶喷物料筒连接好，然后将整个顶喷物料筒装置的支撑轴连接在过滤室支座的连接套筒内；嵌入密封条；安装好喷枪；3.2底喷装置先将喷枪安装在底喷过度段装置上，然后与底喷物料筒连接好，将整个底喷物料筒装置的支撑轴连接在过滤室支座的连接套筒内；嵌入密封条；4. 滤袋架及滤袋的安装4.1该安装顺序必须在设备的空机动作调试正确后，才能进行；4.2接通电源和起源，按照操作步骤进行操作至放滤袋架，将准备好的滤袋按照滤袋架的形状要求系好，分别将滤袋架卡接在抖袋汽缸接口上；二、设备调试1.顶喷装置、底喷装置的升降调试选择一种工艺操作模式，接通电源和起源，按照操作步骤进行，反复点击容器升降按键，调试升、降顺序和装置升降的活动性；2.喷枪雾化效果的调试将压缩空气接入喷枪，启动系统至喷雾运行状态，调节供液频率和雾化压力可改变雾化效果；颗粒成型原理：雾滴大小与液体流量成正比，与雾化压力成反比雾化角度（微调）可通过雾化压力和调试喷枪头的空气帽来完成。