脱蜡油溶剂回收系统核算与优化Word格式.docx
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脱蜡油溶剂回收系统核算与优化Word格式.docx
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测定值
相对密度
0.8852
比色
3.5
粘度
40℃mm2.s-1
143.0
100℃mm2.s-1
14.41
闪点(开口)
℃
280
凝点
-4.9
残炭
%
0.13
酸值
mgKOH/g
0.029
溶剂含量
微量
苯胺点
115.4
馏程
HK
414
2%
469
10%
505
30%
534
50%
545
70%
560
90%
575
溶剂组成
项目
采样地点
溶剂含量%(重)
水
丁酮
甲苯
装置进料
0.8395
84.90
0.27
52.61
47.12
塔501顶
0.8236
99.4
0.47
60.54
38.87
塔501底
0.8450
80.21
0.15
47.34
52.52
塔502顶
0.8310
0.33
55.95
43.71
塔502底
0.8569
68.76
0.07
34.89
65.04
塔503顶
0.8435
0.12
38.71
61.18
塔503底
0.8823
7.4
塔504顶
塔504底
0.8825
4.0
塔505底
0.8845
0.017
塔类操作数据
设备
进料温度
塔顶温度
塔底温度
塔顶压力
塔501
109
108
0.08
塔502
130
129
0.16
塔503
205
203
204
0.26
塔504
196
198
0.01
塔505
174
188
-0.01
加热炉:
滤液进炉温度128℃,计出炉温度206℃
过热蒸汽:
750kg/h,进炉温度135℃,出炉温度343℃
燃料气温32℃,烟气温度247℃
换热器
设备名称
换热器型号
介质
程别
温度
面积
换512
FA700-160-16-4
热
T501顶剂二次
壳程
60
160
冷
滤液
管程
29
50
换513
FB900-240-16-4Ⅱ
T501顶剂一次
107
240
84
换514/1
FB-600-90-16-2
T503顶剂三次
119
93
90
92
换514/2
FB600-90-16-2
T503顶剂二次
149
104
换515/1.2
T502顶剂一次
114
240*2
换516
T505油一次
122
T501底滤液
换517
FLA1000-345-16-4
T503顶剂一次
202
146
345
机泵数据
流程号
泵名称
介质流量
m3/h
介质温度
压力KPa
电流A
进口
出口
额定电流
实际电流
电压
泵507
滤液泵
68.215
-13
20
1600
141
85
393
泵518
52.301
150
1200
56
38
泵519
炉进料泵
35.501
230
1700
131
34
泵521
脱蜡油泵
12.00
186
1000
26
18.8
数据来源说明:
1、该数据来自94年8月23日装置实际操作数据
2、脱蜡装置处理原料为大庆减四线糠醛精制馏分油,产品作为白土精制原料。
3、脱蜡装置处理量为:
517.9吨/天,其中蜡液脱蜡油收率为8873kg/小时
三、物料平衡、能量平衡、工艺计算
1、装置物料平衡流量单位kg/h
物流甲苯丁酮油水
入脱蜡液23510.026255.08875.0135.0
汽提水蒸汽430.0
方合计23510.026255.08875.0565.0
脱蜡油8874.3
出T201顶4206.79619.00.1120.3
T202-1顶6880.710046.50.114.0
T202-2顶11786.76495.40.20.7
T203顶412.183.10.1
T204顶223.811.00.2430.0
方合计23510.026255.08875.0565.0
–装置物料及单体设备物料平衡
略
2、装置能量平衡
–装置能量平衡及单体设备能量平衡
3、装置设备工艺核算
–主要校验换热器传热面积
四、计算结果分析
1、产品质量影响因素分析
-水蒸汽汽提
T204为汽提塔,汽提蒸汽用量增大,产品含溶剂越少,质量越高,水蒸汽汽提,产生含水溶剂,对结晶系统产生不良影响,溶剂回收困难。
-干式蒸馏
经灵敏度分析,干式闪蒸除溶剂效果较差,
在197℃,10KPa时,产品中含甲苯21kg/h
4KPa时,产品中含甲苯8.5kg/h
-氮气汽提
197度,50kg/h氮气时,产品含甲苯2.8kg/h
150kg/h0.05kg/h
270kg/h0.001kg/h
2、能耗影响因素分析
塔202-1压力对装置能耗灵敏度分析
T202-1炉负荷T2021顶T2022顶T202-1
压力KPacal/sec.流量kg/h流量kg/h顶温
1956.731+051.958+041.560+04117
2026.790+051.926+041.592+04119
2106.847+051.895+041.624+04120
2186.901+051.865+041.655+04121
2266.954+051.835+041.685+04123
2337.004+051.806+041.714+04124
2417.054+051.777+041.744+04125
2497.101+051.749+041.772+04126
2577.147+051.721+041.800+04127
2657.192+051.694+041.828+04129
五、结论
1、产品质量
干式闪蒸不能满足产品质量要求
水蒸汽汽提可保证产品质量,但产生含水溶剂。
氮气气提既可保证产品质量,又不产生含水溶剂。
2、装置能耗
T202-1压力对能耗影响较大,压力越高,能耗越高。
保证T201进料有足够换热温差,尽可能降低T202-1操作压力。
T202-2压力对装置能耗影响较小
炉出口温度:
195-210℃。
Abstract:
ComputingandOptimizingEnergyoftheSystemofDewaxingOilRecovery
Alllubestocks,exceptthosefromarelativelyfewhighlynaphtheniccrudeoils,mustbedewaxedortheywillnotflowproperlyatlowertemperatures.Dewaxingisoneofthemostimportantandmostdifficultprocessesinlubricatingoilmanufacturing.Solventdewaxingprocessesusesrefrigerationtocrystallizethewaxandsolventtodilutetheoilportionsufficientlytopermitrapidfiltrationtoseparatethewaxfromtheoil.Themostwidelyusedsolventdewaxingprocessesadoptmixturesofmethylethylketone(MEK)andtolueneasasolvent,whileMEKistheextractiveagent,tolueneasolvent.
Thewholesolventdewaxingprocessisverylargeandcomplicated,includingcrystallizingsystem,vacuumfilteringsystem,refrigerationsystem,andrecoverysystemandsecuregassystem,etc.Theoilrecoverysystemisthemostimportantintherecoverysystem,asshowninfigure5.Thesystemconsistsofthreestageflashtower(T201,T202,T202/1),furnace(F201),flashtower(T203),stripper(T204)andcoolingandheatexchangingsystem.
AgreatdealofEnergyisneededintherecoverysystem.Inordertorecoveringtheenergy,thesystemofthreestagesflashandheatexchangingisused.Itshouldbeassuredthatthesystemworkgood,orfuelisincreasedmore,therefor,wemustcomputeandoptimizetheprocessandenergyofthesystem.
计算过程
ASPENPLUSISATRADEMARKOFHOTLINE:
TBDEWAXXOIL
TABLEOFCONTENTS
COMPUTATIONALSEQUENCE
----------------------
SEQUENCEUSEDWAS:
$OLVER10T202-1E224-1,2T201E223-1,2E223P223P224F201T202-2T203
|T204E224-3,4E224-5,7E223-3E224
(RETURN$OLVER10)
OVERALLFLOWSHEETBALANCE
-------------------------
***MASSANDENERGYBALANCE***
INOUTRELATIVEDIFF.
CONVENTIONALCOMPONENTS(KMOL/HR)
TOLUE-01255.154255.154-0.511997E-07
METHY-01364.109364.109-0.119326E-06
WATER31.372431.3724-0.257796E-07
PC411C0.252534E-010.252534E-010.315986E-12
PC420C0.785524E-010.785524E-010.205113E-12
PC441C0.1562870.1562870.618025E-13
PC473C0.3577210.3577210.806935E-14
PC496C0.5407110.5407110.246392E-14
PC525C0.5386450.5386450.618343E-15
PC555C1.138161.138160.195091E-15
PC580C3.682153.682150.482424E-15
PC608C3.058943.058940.299791E-12
PC633C2.463472.463470.118888E-11
PC650C0.1832070.1832070.220884E-12
TOTALBALANCE
MOLE(KMOL/HR)662.858662.859-0.864742E-07
MASS(KG/HR)59205.059205.0-0.734928E-07
ENTHALPY(CAL/SEC)-0.801030E+07-0.729015E+07-0.899021E-01
ASSAYDATAANALYSIS
-------------------ASSAYID:
DEWAXOIL
SPECIFICGRAVITY60F/60F0.8852
APIGRAVITY28.3508
DENSITYGM/CC0.8829
MOLECULARWEIGHTMISSING
DISTILLATIONCURVES
-------------------
PERCENTDISTILLEDVERSUSTEMPERATURE,C
ASTM
PERCENTD86TBP
DISTILLEDLVPCTLVPCT
-------------------------
0414.0408.4
5482.5493.1
10505.0532.2
30534.0575.7
50545.0593.9
70560.0615.8
90575.0635.8
95582.2643.7
100589.4651.6
PRESKPA101.3101.3
PSEUDOCOMPONENTBREAKDOWN
ASSAYID:
DEWAXOIL
MOLEWEIGHTVOLUME
COMPONENTPERCENTPERCENTPERCENT
---------------------------------------------
PC411C0.20660.11910.1286
PC420C0.64260.38280.4116
PC441C1.27860.81880.8717
PC473C2.92662.08722.1896
PC496C4.42363.39923.5296
PC525C4.40673.69953.7950
PC555C9.31158.54738.6602
PC580C30.124529.715529.8063
PC608C25.025926.583126.3857
PC633C20.154222.871722.4866
PC650C1.49881.77531.7345
PSEUDOCOMPONENTPHYSICALPROPERTIES
-----------------------------------
PSEUDOCOMPONENTPROPERTYSUMMARY
COMPONENTNBPAPISGMWTCPC
CCKPA
PC411C410.559041.13410.8196418.7472553.6148969.8831
PC420C419.725940.36940.8233432.5310561.4516950.2038
PC441C440.631838.67480.8315465.0142579.2118907.7088
PC473C472.832536.19010.8438517.8418606.2736848.1094
PC496C496.032334.48690.8524557.9318625.5600809.0595
PC525C524.624632.47980.8629609.5547649.0976764.8631
PC555C554.798030.46300.8736666.4959673.6715722.3846
PC580C580.211828.83900.8825716.2300694.1669689.5401
PC608C607.525027.16400.8918771.2664715.9968656.9016
PC633C633.065825.65920.9003823.9883736.2320628.6233
PC650C650.261624.67750.9060860.0438749.7620610.6966
BLOCK:
E223MODEL:
HEATX
-----------------------------
MOLE(KMOL/HR)824.748824.7480.000000E+00
MASS(KG/HR)72721.572721.50.000000E+00
ENTHALPY(CAL/SEC)-0.988004E+07-0.988004E+070.000000E+00
***INPUTDATA***
FLOWDIRECTIONANDSPECIFICATION:
COUNTERCURRENTHEATEXCHANGER
SPECIFIEDCOLDOUTLETTEMP
SPECIFIEDVALUEC50.0000
LMTDCORRECTIONFACTOR1.00000
PRESSURESPECIFICATION:
HOTSIDEPRESSUREDROPKPA0.0000
COLDSIDEOUTLETPRESSUREKPA220.0000
DUTYANDAREA:
CALCULATEDHEATDUTYCAL/SEC159688.2823
CALCULATED(REQUIRED)AREASQM13.8898
HEATTRANSFERCOEFFICIENT:
AVERAGECOEFFICIENT(DIRTY)CAL/SEC-SQCM-K0.0229
LOG-MEANTEMPERATUREDIFFERENCE:
LMTDCORRECTIONFACTOR1.0000
LMTD(CORRECTED)C50.2958
E223-1,2MODEL:
MASS(KG/HR)72721.572721.50.200105E-15
ENTHALPY(CAL/SEC)-0.944680E+07-0.944680E+070.000000E+00
SPECIFIEDVALUEC84.0000
COLDSIDEOUTLETPRESSUREKPA215.0000
CALCULATEDHEATDUTYCAL/SEC273544.6548
CALCULATED(REQUIRED)AREASQM37.7271
AVE
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- 蜡油 溶剂回收 系统 核算 优化