精馏塔中英文对照外文翻译文献Word格式.docx
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精馏塔中英文对照外文翻译文献Word格式.docx
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气相混合物上升到塔顶上方的冷凝器中,这些气相混合物被降温到泡点,其中的液态部分进入到塔顶产品冷却器中,停留一定的时间然后进入苯的储罐,而其中的气态部分重新回到精馏塔中,这个过程就叫做回流。
液相混合物就从塔底一部分进入到
塔底产品冷却器中。
一部分进入再沸器,在再沸器中被加热到泡点温度重新回到精馏
塔。
塔里的混合物不断重复前面所说的过程,而进料口不断有新鲜原料的加入。
最终,完成苯与氯苯的分离。
填料塔属于微分接触型的气液传质设备。
塔内以填料作为气液接触和传质的基本构件。
液体在填料表面呈膜状自上而下流动,气体呈连续相自下而上与液体作逆流流
动,并进行气液两相间的传质和传热。
两相的组分浓度或温度沿塔高呈连续变化。
板式塔是一种逐级接触的气液传质设备。
塔内以塔板作为基本构件,气体自塔底
向上以鼓泡活喷射的形式穿过塔板上的液层,使气-液相密切接触而进行传质与传热,两相的组分浓度呈阶梯式变化。
综合考虑板式塔由于比填料塔性能稳定、效率高、安装检修方便及造价低等优点,本设计选用板式塔。
塔板是板式塔的主要构件,分为错流式塔板和逆流式塔板两类,工业应用以错流式塔板为主,常用的错流式塔板主要有泡罩塔、筛板塔、浮阀塔等。
筛板塔在相对气液相负荷、效率、可靠性以及价格方面都较其他两种塔优,
因此本设计选用筛板塔,其特点如下:
结构简单、制造维修方便;
生产能力大,比浮阀塔还高;
塔板压力降较低,适宜于真空蒸馏;
塔板效率较高,但比浮阀塔稍低;
合理设计的筛板塔可是具有较高的操作弹性,仅稍低与泡罩塔;
小孔径筛板易堵塞,故不宜处理脏的、粘性大的和带有固体粒子的料液。
本设计的题目是苯-氯苯分离精馏塔设计,即需设计一个精馏塔用来分离易挥发的苯和不易挥发的氯苯,采用连续操作方式,具体工艺参数如下:
处理量:
12000吨/年
料液组成(含氯苯):
34%
产品组成(氯苯纯度):
99%
塔顶产品组成(含氯苯):
≤1.5%
操作压力:
塔顶压强4KPa(表压)
进料热状况和回流比自选
塔底加热蒸气压力:
0.5MPa(表压)
单板压降:
≤0.7KPa
地震裂度:
7度
土质情况:
第二类场地土
当地气压=100kPa
设备年工作时间:
300天(每天24小时连续运行)
水电供给:
水源充足,供电正常
对于16MnR钢板负偏差1c=0,因而名义厚度6nmm。
但对于低合金钢制容器,规定不包括腐蚀裕量的最小厚度应不小于3mm,若加上5mm的腐蚀裕量,名义厚度至少取8mm。
由于封头的椭球部分经线曲率变化平滑连续,故应力分布比较均匀,且椭圆形封头深度较半球形封头小得多,易于冲压成型,是目前中、低压容器中应用较多的封头。
因此本设计选用椭圆形封头。
塔的手孔是操作人员对塔进行检验及维修用的。
本塔设计中手孔选择DN250的4带颈对焊法兰手孔。
由于工艺操作需要有各种接管,在本塔的设计中接管的尺寸分别是DN32,DN50,DN65,DN80,DN125,所有接管均不用补强。
参考文献:
[1]Bcoli,Luyben
Shunta,蒸馏塔控制设计
[2]Thirston·
c·
W“蒸馏塔控制的计算机辅助设计”,碳氢化合物处理
[3]Tolliver.AndMcCune“蒸馏塔控制设计基于稳态仿真”,ISA事务卷
[4]Roat
s
D。
Morec.F。
J.J。
一个稳态蒸馏塔控制系统灵敏度分析技术”
[5]SkogestadS.动力学和控制”,蒸馏塔——一个关键的调查”,预印本IFAC研讨会,DYCORD
大学公园,医学博士,美国
[6]Luyben
w·
L“稳态蒸馏塔的节能方面控制设计”,I&
E.C,Fundam,14卷,4号,1975年。
[7]ChineI-LAndFruehaufP.S。
“考虑IMC优化来改善控制器性能”,C.E.P.卷。
86年,1990年10月10号。
[8]Shuntaj.p.AndLuyben
w.L。
“动态效果的温度控制在蒸馏塔盘置”,AICHEJ,17卷,1971年1月1号
ABSTRACT
Steady
state
models
continue
to
be
powerful
and
efficient
tools
for
designing
control
systems
for
distillation
columns.
This
paper
presents
a
design
procedure
an
example
applicatin
of
this
technique
actual
column.
KEYWORDS
Computer
Aided
Engineering,
Simulated
Distillation,
Chemical
Processing,
Distillation
Control,
State
Modeling
INTRODUCTION:
Steadystateprocessmodelshavelongbeenusedtoassistthecontrolengineerindesigningcontrolstrategiesfordistillationcolumns.However,withthelargenumberofindustrialcolumnsstilloperatinginmanualorwithineffectualcontrols,thereremainsaneedforsounddistillationcolumncontroldesigntechniques.WebelievethatTolliverandMcCune(1978)havemadethegreatestcontributiontothedevelopmentofthistypeofdesignprocedure.TwootherverygoodpapersonthissubjectarebyThurston(1981)andRoat,etal(1988).WhileourprocedureisanextensionofthatproposedbyTolliverandMcCune,wehaveimprovedtheprocedureinthefollowingways
·
Weadvocatethatmassflowsbeusedinmodelsversusthepreviousstandardofmolarflows.Wehavedeterminedindependentlythatuseofmolarflowscanleadtoincorrectresults.ArecentreviewarticleondistillationcolumncontrolbySkogestad(1992)confirmsthesefindings.
Wealsoadvocatethattheactualcontrolstructurebeenforcedwhenusingthesteadystatesimulationtoidentifyatemperaturesensorlocationforcompositioncontrol.Thisisaccomplishedbyacarefulchoiceofindependentvariableswhendefiningthemodelsolutionconditions.TolliverandMcCuneadvocatevaryingonlymolardistillateflowregardlessoftheproposedcontrolstructure.Thistoocanleadtoincorrectresults.
Weshowthatthistechniquecanbeusedformulticomponentcolumnstoquantifytheincrementalbenefitofcompositioncontrolusingon-lineanalyzersversustemperaturecontrol.
Thispaperdealsexclusivelywiththedesignofsinglepointcompositioncontrols.Thevastmajorityofcolumnshaveonesidedcompositionspecifications;
thoseinwhichasinglepointcompositioncontrolschemecankeepbothtopandbottomproductcompositionsatorbelowlimitsforawiderangeofdisturbances.Thisdoesnothavetobeacceptedonfaithbecausethedesignprocedureexplicitlyteststhishypothesis.Thepredominanceofonesidedspecificationsleavesthemainincentivefordualpointcontrolschemestobeenergysavings.Inmostcases,theenergysavingsissmallanddoesnotjustifytheaddeddifficultyofimplementingandmaintainingdualpointcontrol.
Luyben(1975)presentsthepotentialenergysavingsformanydifferenttypesofseparations.Additionally,dualpointschemesoftenhavesignificantlylongerrecoveriesfromupsetsduetointeractionsbetweenthecontrolloops.
Webelieveitisappropriatetocontraststeadystateanddynamicmodelsascontroldesigntools.Whilebothtoolshaveaplace,wehavefoundthatusingsteadystatemodelscoupledwithexperienceandageneralknowledgeofdistillationcolumndynamicsisadequateformanyproblemsandcanbemoreefficientthanusingdynamicmodels.ForagooddevelopmentontherationalebehindusingsteadystatemodelsrefertothechaptersonQuasi-StaticAnalysisinRademaker,etal(1975).Oneobviouslimitationofsteadystatemodelingisthatittellsusnothingaboutthedynamicresponse,makingitdifficulttocomparethedynamicdisturbancerejectioncapabilityofalternativecontrolschemes.
Whenweencounteradifficultandimportantproblemweinvesttheextraengineeringtimetodevelopadynamicmodel.Theidealdesigntoolwouldbeonethathasbothsteadystateanddynamiccapabilities.Thistoolwouldprovidetheefficiencyofsteady-stateanalysis,butwouldalsohavetheaddedbenefitofcomparingthedisturbancerejectioncapabilitiesofdifferentschemeswiththedynamicmodel.Thecombinedtoolwouldallowthedesignertoperformbothtaskswithoutrequiringaninvestmentintimetodeveloptwodifferentmodels.AnewproductsoontobereleasedbyHyprotech,Ltd.willcombinesteadystateanddynamicmodelinginonesuchpackage.
Ourdesignprocedurecanbebestthoughtofasgeneralapproachratherthanasingledetailedprocedurethatcoversallcases.Theproceduremustbeadaptedtoeachproblembecausetherearemanydifferenttypesofdistillationandalmosteveryindustrialproblemusuallyhassomeuniquerequirement.
Wehaveappliedthisgeneralproceduretomanydifferenttypesofspecializedcolumnsincludinghomogeneousandheterogeneousazeotropes,extractivedistillation,strippersandabsorbersandmulticomponentcolumns.Wehavealsousedthisprocedureformanydifferentcolumnconfigurationsincludingcolumnswitheitherliquidorvaporsidedraws,columnswithpartialcondensersandwithbothpackedandtraycolumns.
Because
we
often
encounter
columns
with
multiple
components
in
the
feed,
little
more
should
said
about
these
cases.
In
multicomponent
columns,
unlike
binary
fixing
temperature
pressure
does
not
fix
composition.
spite
limitation,
can
still
used
meet
many
composition
specifications.
Often
results
largeryield
losses
or
higher
energy
consumptions
than
if
on-line
analyzer
was
available
control.
is
where
steady
very
helpful
us
because
use
them
quantify
incremental
benefit
analyzers
versus
one
case,
document
yield
improvement
gained
from
addition
analyzer.
The
savings
over
two
hundred
thousand
dollars
year.
DESIGN
PROCEDURE
:
WehaveextendedthedesignprocedurereportedbyTolliverandMcCune(1978).Thedesignprocedureiscomposedofthefollowingsteps:
Step
1
Develop
basis
2
Select
candidate
scheme.
3
"
Open
loop"
test
using
model
find
sensor
location.
4
Closed
scheme
feed
rate
Disturbances
Design
Basis
-
Like
any
effort,
ideal
first
step
completely
define
providing
all
information
needed
select
best
alternative.
contract
between
client
designer.
accuracy
mainly
client'
responsibility.
are
summarized
Table
1.
piece
product
specifications
top
bottom
column.
We
need
know
sided.
A
sided
specification
means
that
exceed
specification.
keep
within
certain
range.
For
example,
would
require
stay
90-110
ppm.
much
common.
have
encountered
only
column
has
It
also
important
reasons
Occasionally,
some
picked
arbitrarily
simply
sizing
ba
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