醋酸酐生产过程概念设计

化工过程模拟与优化课程设计报告
醋酸酐生产过程概念设计
1 ．过程设计分析
1.1 醋酸酐的相关信息
1.1.1性质与用途
醋酸酐（又称乙酸酐，简称醋酐）为无色易流动液体，有极强的醋酸气味。

有刺激作用。

相对密度（d415）1.080,熔点-73℃，非点139℃，折光指数（20℃）1.3904，水中溶解度（20℃）12%。

易燃烧，遇水分解成醋酸。

溶于乙醇、乙醚、苯和氯仿。

醋酸酐（又称乙酸酐，简称醋酐）是一种重要的有机化工原料，主要用于制造醋酸纤维、醋酸塑料、不燃性电影胶片及人造丝等化工产。

在医药工业中用于制造阿司匹林、合霉素、地巴唑等药物。

此外，在燃料，香料及化工生产中用作强乙酰化剂和脱水剂。

1.1.2生产与消费
我国从50年代末期开始生产醋酸酐。

上海试剂一厂采用乙酰氧化法首先建成了我国第一套醋酸酐生产装置。

随后，南通醋酸化工厂、山东新华制药厂、吉化公司电石厂等相继建设了十几套生产装置。

1972年合成醋酸酐产量突破万吨达到1.03万吨，1980年为1.43万吨，92年增长到4.04万吨，目前年产量超过7万吨，供需基本持平。

1.1.3技术要求
中华人民共和国国家标准GB10668-89
1.2醋酸酐生产过程的分析
1.2.1 醋酸酐的生产方法
醋酸酐的各种生产方法示意图：
其中最常用的主要工业生产方法有醋酸法、丙酮法、乙醛法等。

本设计拟采用丙酮法进行醋酸酐的生产设计。

丙酮在700~800℃，常压、没有催化剂的条件下进行裂解反应，反应停留时间0.01~1.0s。

裂解反应管的结焦比乙酸法严重，为了防止结焦，主要采用高铬钢管材，如用含镍钢材，应事先用一氧化碳和氧气混合物进行钝化处理，以防元素镍对结焦的促进作用。

本法丙酮的转化率约为24.4%,生成乙烯酮的选择性为72%,反应信息如下：
主反应：CH3CO CH3CH2=C=O+ CH4700℃，1atm;
副反应: CH2=C=O CO + 1/2 CH2=CH2700℃，1atm; 主反应：CH2=C=O + CH3COOH (CH3CO)2O 80℃，1atm 1.2.2 醋酸酐产品分离过程分析
由前面反应可知，在醋酸酐的合成过程中，由于丙酮转化不完全、副反应产物的存在和未反应完全醋酸的存在，必须对反应产物进行分级分离。

在本设计中，根据沸点之间的差异，首先用一个分离器将产物中甲烷、乙烯和一氧化碳分离出来，再将丙酮分离丙酮循环使用，最后醋酸与醋酸酐的沸点相近，用一个精馏塔进行分离使产品醋酸酐达到相应要求，并使精馏出来的醋酸循环使用。

2．醋酸酐生产过程的设计
2.1反应系统
反应主要包括：丙酮裂解、醋酸吸收乙烯酮生成醋酸酐工段；
将整个反应和分离循环等作为一个系统，考察它的输入与输出，可以得到以下的信息：
1进料物流：原料丙酮、醋酸；
2副产物：由于丙酮裂解过程产生CH 4、CO 、C 2H 4，可以去作燃料回收； 3由于反应很不完全，所以需要一股循环物流将未反应的丙酮送回裂解炉； 4过量反应物：醋酸吸收乙烯酮反应中，醋酸为过量反应物，故要循环使用； 5产品物流的项目：这些组成的沸点和去向在表2中给出：
2．2反应信息
2.2.1 反应、副反应及其条件：
主反应： CH 3CO CH 3 CH 2=C=O+ CH 4 700℃，1atm;
副反应: CH 2=C=O
CO + 1/2 CH 2=CH 2 700℃，1atm;
主反应：CH 2=C=O + CH 3COOH (CH 3CO)2O 80℃，1atm
2.2.2 选择性、转化率
选择性和转化率的关系可用s=1-4/3 x 表示
产率 y=s×x
2.2.3 反应的相态
1.CH4、CO、C2H4、CH2=C=O常温下均为气态；
2.丙酮的裂解反应为气相反应；
3.醋酸吸收乙烯酮反应中，乙酸、醋酸酐为液相，乙烯酮为气相；
4.两个反应均不需催化剂。

设计方案定为年产15,000吨，即设计产量为20.0 kmol/hr。

产品浓度控制在98%以上，从而反推原料量即丙酮、醋酸的流量。

反应条件定为：裂解反应700℃，1atm;醋酸与乙烯酮的反应为80℃，1atm;
由醋酸酐产量为P醋酸酐=20kmol/hr,根据反应计量式，把整个过程看作一个系统，进料为丙酮、醋酸，出料是废气、产品醋酸酐。

由选择性可知，丙酮的进料为20/0.72=27.8 k mol/hr,醋酸进料量为20.0k mol/hr,而丙酮与醋酸之间的摩尔差的丙酮量转化为废气。

设定数据为：丙酮进料量：27.8 k mol/hr;醋酸进料量：20.0 k mol/hr。

而由于在分离循环过程中累积导致最后可能会随产品损失部分反应进料，故最终醋酸酐的产量将比预计的低些。

2.3流程的循环结构
在醋酸酐生产过程中，裂解炉中丙酮是不完全反应,而在第二个反应器中醋酸吸收乙烯酮为了使乙烯酮完全反应，必须是醋酸酐过量。

为了提高反应物的利用率，因而在整个流程中会存在两股循环物流：丙酮循环回裂解炉，醋酸循环Reactor2。

醋酸酐生产过程的循环结构可简单表示如下：
醋酸酐生产的循环结构简图
2.4系统设计
2.4.1原料消耗
设计方案定为年产15,000吨，即设计产量为20.0kmol/h，产品纯度控制在98%(质量)以上。

由醋酸酐产量为P醋酸酐=20.0kmol/hr,根据反应计量式，把整个过程看作一个系统，进料为丙酮、醋酸，出料是废气、产品醋酸酐，由选择性可知，丙酮的进料为20.0/0.72=28.7kmol/hr,醋酸进料量为20.0kmol/hr，而丙酮与醋酸之间的摩尔差的丙酮量转化为废气。

由于反应过程中原料的损失或反应的需求，需要一定程度的过量，所以设定数据为：丙酮进料量：28.7kmol/hr;
醋酸进料量：21.6kmol/hr;
2.4.2生产流程
如附图所示，新鲜丙酮与后面返回的未反应丙酮先进入M1混合，再进入裂解炉R1，经过预热，在700℃，1atm的反应管内进行裂解反应，裂解气经过废热锅炉EX-1产生120kg/cm2的超高压饱和蒸气，温度降到400℃，然后进入废热锅炉EX-2产生30kg/cm2高压蒸气，温度降到250℃，然后进入废热锅炉EX-3产生5kg/cm2低压蒸气，温度降到140℃，然后由冷却水降到70℃，同醋酸一同进入反应器R2进行反应。

R2的反应温度为80℃，压力为1atm。

反应器R2出来的气体，先经过COOL1的冷却，温度降为40℃，再进入SEP1中进行闪蒸，未冷凝的气体在SEP2中进一步闪蒸，仍未冷凝的气体去尾气吸收塔TOWER1，经塔顶进料的醋酸洗涤后，冷凝液循环返回反应炉R2进行反应，不凝性气体排空（或燃烧）。

SEP1与SEP2中冷凝下的液体，经泵PUMP2升压至5atm，一同进入管壳式换热器EX5进行减压蒸发，温度变为82℃，压力为1.2atm。

然后进入TOWER2。

TOWER2的操作压力为常压，丙酮从塔顶分出，循环至裂解炉R1，醋酸与醋酐从塔底分出，经泵PUMP3升压至3atm去TOWER3，TOWER3的操作压力为2.2atm。

醋酸从塔顶返回到R2，产品醋酐则从塔底经换热器EX6冷却到50℃后去产品罐。

2.4.3流程的循环结构
在醋酸酐生产过程中，裂解炉R1中丙酮的裂解反应是不完全反应；在反应器R2中，醋酸吸收乙烯酮，为了使乙烯酮完全反应，醋酸必须是过量的。

为了提高反应物的利用率，未参加反应的反应物要进行循环利用，因此，在整个流程中会存在两股循环物流：丙酮循环回裂解炉R1，醋酸循环回R2。

2.5分离序列
由前面的分析可知，最终反应产物中存在未反应的醋酸、丙酮，产物醋酸酐和副产物甲烷、乙烯和一氧化碳。

分离的目的就是将产物醋酸酐分离出来，同时将未反应的醋酸和丙酮
循环使用，此外副产物除去。

因此，存在分离序列的选择。

本设计采用启发－探索法进行排序。

主要用到的排定塔序的推理法为：最轻的组分最先分离；流量最大的组分最先分离；高收率的组分最后分离；分离困难的组分最后分离等。

根据各产品的组成的沸点排列，作为反应副产物的甲烷、乙烯和一氧化碳通常状况下为气体，先利用闪蒸或是相分离器将它们分离出来，送入燃料系统。

液相产物中的丙酮的沸点做笑，而且其量又大，先将丙酮分离出来；醋酸、醋酐的沸点相差不大，故将其放在最后分离。

整个分离系统由三个部分组成。

先用相分离器SEP1和SEP2将以甲烷、乙烯和一氧化碳为主的气相和以丙酮、醋酸、醋酐为主的液相分开，然后在TOWER1中将丙酮分离出来循环使用，塔底出来的醋酸和醋酸酐进入TOWER2进行分离，塔顶馏出物醋酸循环使用，塔底得到合格的醋酸酐产品。

2.5.1分离序列及条件确定
R2出来的反应物含有甲烷、乙烯、CO、丙酮、醋酸、醋酐，根据它们的沸点不同，先将轻组份甲烷、乙烯、CO分出。

如果采用常压冷凝，经模拟计算发现，即使冷到0℃以下不凝气中还含有大量丙酮。

例如，如果采用陈贇等的操作条件（30℃，1atm），不凝气中将含有50%wt的丙酮，即使再加一个吸收塔，也很难吸收干净，并且需要大量的低于常温（-10℃左右）的冷量。

我们采用5atm进行闪蒸, 这样有两个优点，一是高压下丙酮与不凝气容易分离，采用冷却水即可，无需低温冷源; 二是升压后温度提高了，闪蒸热可以用来加热进料，节省了大量的冷却水和加热蒸气。

虽然增加了一台压缩机，并消耗了电能，但经过权衡还是值得的。

液相产物中的丙酮的沸点较小，而且其量又大，先将丙酮分离出来；乙酸、醋酸酐的沸点相差不大，故将其放在最后分离。

整个分离系统由三个部分组成：先用闪蒸罐SEP1、SEP2和洗涤塔TOWER1将以甲烷、乙烯和一氧化碳为主的气相和以丙酮、醋酸、醋酸酐为主的液相分开，然后在第一精馏塔TOWER2中将丙酮分离出来循环使用，塔底出来的醋酸和醋酸酐进入第二精馏塔TOWER3进行分离，塔顶馏出物醋酸循环使用，塔底得到合格的醋酸酐产品，其分离序列如图：
分离序列图
2.5.2闪蒸罐和吸收塔分离条件的确定
根据反应产物分布和其沸点分布，使反应副产物甲烷、乙烯和一氧化碳近乎完全分离。

利用Apsen-plus流程模拟软件模拟的各闪蒸罐的操作条件如下表所示：
表3 闪蒸器SEP1的分离条件
表4 闪蒸器SEP2的分离条件
表5 吸收塔TOWER1的分离条件
2.6生产过程的热量集成与热负荷
2.6.1热集成
由反应器R2出来的物料，经压缩机压缩后温度升高，在进入闪蒸罐SEP1前又需要冷
却，经SEP1、SEP2分离下来的冷凝液在进入分离塔TOWER2前需要加热，为充分利用热量，在这两股物流之间加一台管壳式换热器EX5来利用两者的热量，使得两股物流达到各自所要求的温度。

节省了一定的加热蒸汽和冷凝水。

丙酮、醋酸、醋酐的分离采用两个热耦合塔TOWER2，TOWER3，T2采用常压操作，T3采用加压操作（2.2atm绝），T3的冷凝器可以作为C2的再沸器，这样可以节省大量蒸汽和冷却水。

2.6.2热负荷
由ASPEN计算结果，可得各设备的热负荷，如表8所示
3．与往届同学相比所作的改进
1、产量的扩大：由上届的1500吨/年，扩大为15000吨/年
2、热量的有效利用：从反应器R1出来的气体温度为7000C，经过多级冷却，
产生不同压力的蒸汽；此外。

把蒸馏塔T3的冷凝器作为塔T2的再沸器，这样一来，达到了节能的目的。

3、工艺的改进：从反应器R2出来的产物，经过两次冷却、闪蒸，使丙酮能更好地被分离出来，从而循环再利用。

TABLE OF CONTENTS RUN CONTROL SECTION (1)
RUN CONTROL INFORMATION (1)
INPUT SECTION (2)
INPUT FILE(S) (2)
FLOWSHEET SECTION (6)
FLOWSHEET CONNECTIVITY BY STREAMS (6)
FLOWSHEET CONNECTIVITY BY BLOCKS (6)
CONVERGENCE STATUS SUMMARY (6)
CONVERGENCE BLOCK: $OLVER01 (7)
COMPUTATIONAL SEQUENCE (7)
OVERALL FLOWSHEET BALANCE (7)
U-O-S BLOCK SECTION (9)
BLOCK: MIXER-1 MODEL: MIXER (9)
BLOCK: REACT-1 MODEL: RSTOIC (9)
BLOCK: MIXER-2 MODEL: MIXER (11)
BLOCK: REACT-2 MODEL: RSTOIC (11)
BLOCK: EX-5 MODEL: HEATER (13)
BLOCK: TOWER-2 MODEL: RADFRAC (14)
BLOCK: TOWER-3 MODEL: RADFRAC (20)
BLOCK: TOWER-1 MODEL: RADFRAC (26)
BLOCK: SEP-2 MODEL: FLASH2 (31)
BLOCK: EX-6 MODEL: HEATER (32)
BLOCK: PUMP3 MODEL: PUMP (33)
BLOCK: COOL2 MODEL: HEATER (34)
BLOCK: COOL1 MODEL: HEATER (34)
BLOCK: PUMP2 MODEL: PUMP (35)
BLOCK: EX-2 MODEL: HEATER (36)
BLOCK: EX-3 MODEL: HEATER (37)
BLOCK: EX-1 MODEL: HEATER (38)
BLOCK: EX-4 MODEL: HEATER (39)
BLOCK: SEP-1 MODEL: FLASH2 (40)
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE II
TABLE OF CONTENTS
STREAM SECTION (42)
1 10 10-1 11 12 (42)
12-1 13 13-1 14 15 (43)
16 17 2 3 4 (44)
5 5-1 5-2 5-3 6 (45)
6-1 8 8-1 9 9-1 (46)
9-2 (47)
PROBLEM STATUS SECTION (48)
BLOCK STATUS (48)
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 1
RUN CONTROL SECTION
RUN CONTROL INFORMATION
-----------------------
THIS COPY OF ASPEN PLUS LICENSED TO GUANGDONG ENGINEERING EQUIP.
TYPE OF RUN: NEW
INPUT FILE NAME: _2641zzz.inm
OUTPUT PROBLEM DATA FILE NAME: _2641zzz VERSION NO. 1
LOCATED IN: PDF SIZE USED FOR INPUT TRANSLATION:
NUMBER OF FILE RECORDS (PSIZE) = 0
NUMBER OF IN-CORE RECORDS = 256
PSIZE NEEDED FOR SIMULATION = 256
CALLING PROGRAM NAME: apmain
LOCATED IN: D:\ASPENT~1\AP100\xeq SIMULATION REQUESTED FOR ENTIRE FLOWSHEET
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 2
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 3
FLOWSHEET SECTION
FLOWSHEET CONNECTIVITY BY STREAMS
---------------------------------
STREAM SOURCE DEST STREAM SOURCE DEST
1 ---- MIXER-1 14 ---- TOWER-1
2 MIXER-1 REACT-1
3 REACT-1 EX-1
4 MIXER-2 REACT-2 6 REACT-2 COOL1
15 EX-5 TOWER-2 11 TOWER-2 MIXER-1
10 TOWER-2 PUMP3 13-1 TOWER-3 MIXER-2
12 TOWER-3 EX-6 9 TOWER-1 ----
17 TOWER-1 MIXER-2 9-2 SEP-2 TOWER-1
8-1 SEP-2 PUMP2 12-1 EX-6 ----
10-1 PUMP3 TOWER-3 13 COOL2 SEP-2
6-1 COOL1 SEP-1 16 PUMP2 EX-5
5-2 EX-2 EX-3 5-3 EX-3 EX-4
5-1 EX-1 EX-2 5 EX-4 MIXER-2
9-1 SEP-1 COOL2 8 SEP-1 PUMP2
FLOWSHEET CONNECTIVITY BY BLOCKS
--------------------------------
BLOCK INLETS OUTLETS
MIXER-1 1 11 2
REACT-1 2 3
MIXER-2 17 5 13-1 4
REACT-2 4 6
EX-5 16 15
TOWER-2 15 11 10
TOWER-3 10-1 13-1 12
TOWER-1 9-2 14 9 17
SEP-2 13 9-2 8-1
EX-6 12 12-1
PUMP3 10 10-1
COOL2 9-1 13
COOL1 6 6-1
PUMP2 8 8-1 16
EX-2 5-1 5-2
EX-3 5-2 5-3
EX-1 3 5-1
EX-4 5-3 5
SEP-1 6-1 9-1 8
CONVERGENCE STATUS SUMMARY
--------------------------
TEAR STREAM SUMMARY
===================
STREAM MAXIMUM MAXIMUM VARIABLE CONV
ID ERROR TOLERANCE ERR/TOL ID STAT BLOCK
------ ------- --------- -------- -------- ---- -----
4 0.72897E-09 0.12068E-08 0.60404 ACETI-02MOLEFLOW # $OLVER01
# = CONVERGED
= NOT CONVERGED
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 7
FLOWSHEET SECTION CONVERGENCE BLOCK: $OLVER01
----------------------------
Tear Stream : 4
Tolerance used: 0.100D-03
Trace molefrac: 0.100D-05
MAXIT= 30
METHOD: DIRECT-SUBST STATUS: CONVERGED
TOTAL NUMBER OF ITERATIONS: 35
NUMBER OF ITERATIONS ON LAST OUTER LOOP: 4
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 8
FLOWSHEET SECTION OVERALL FLOWSHEET BALANCE
-------------------------
*** MASS AND ENERGY BALANCE ***
IN OUT GENERATION RELATIVE DIFF. CONVENTIONAL COMPONENTS
(KMOL/HR )
ACETO-01 28.7250 0.486507E-04 -28.7186 0.220128E-03 ACETI-01 21.5700 0.893752 -20.6763 -0.128587E-05 ACETI-02 0.000000E+00 20.6763 20.6763 0.126923E-06 KETEN-01 0.000000E+00 0.000000E+00 0.113672E-02 0.000000E+00 CARBO-01 0.000000E+00 8.04077 8.04122 0.553348E-04 METHA-01 0.000000E+00 28.7170 28.7186 0.561803E-04 ETHYL-01 0.000000E+00 4.02037 4.02061 0.598602E-04 TOTAL BALANCE
MOLE(KMOL/HR ) 50.2950 62.3482 12.0630 0.156119E-03 MASS(KG/HR ) 2963.68 2963.22 0.154785E-03 ENTHALPY(KCAL/HR ) -0.416391E+07 -0.381148E+07 -0.846389E-01 ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 9
U-O-S BLOCK SECTION BLOCK: MIXER-1 MODEL: MIXER
-----------------------------
INLET STREAMS: 1 11
OUTLET STREAM: 2
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE
*** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 137.419 137.419 0.000000E+00
MASS(KG/HR ) 7956.57 7956.57 0.000000E+00
ENTHALPY(KCAL/HR ) -0.720845E+07 -0.720845E+07 0.000000E+00
*** INPUT DATA ***
TWO PHASE FLASH
MAXIMUM NO. ITERATIONS 30
CONVERGENCE TOLERANCE 0.00010000
OUTLET PRESSURE ATM 1.00000 BLOCK: REACT-1 MODEL: RSTOIC
------------------------------
INLET STREAM: 2
OUTLET STREAM: 3
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE *** MASS AND ENERGY BALANCE ***
IN OUT GENERATION RELATIVE DIFF. TOTAL BALANCE
MOLE(KMOL/HR ) 137.419 170.158 32.7392 -0.835157E-16 MASS(KG/HR ) 7956.57 7956.57 0.228615E-15 ENTHALPY(KCAL/HR ) -0.720845E+07 -0.375878E+07 -0.478559
U-O-S BLOCK SECTION
BLOCK: REACT-1 MODEL: RSTOIC (CONTINUED)
*** RESULTS ***
OUTLET TEMPERATURE C 700.00
OUTLET PRESSURE ATM 1.0000
HEAT DUTY KCAL/HR 0.34497E+07
VAPOR FRACTION 1.0000
REACTION EXTENTS:
REACTION REACTION
NUMBER EXTENT
KMOL/HR
1 28.719
28.0412
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 11
U-O-S BLOCK SECTION BLOCK: REACT-1 MODEL: RSTOIC (CONTINUED)
BLOCK: MIXER-2 MODEL: MIXER
-----------------------------
INLET STREAMS: 17 5 13-1
OUTLET STREAM: 4
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE
*** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 198.614 198.604 0.490082E-04
MASS(KG/HR ) 9647.46 9647.00 0.475497E-04
ENTHALPY(KCAL/HR ) -0.925919E+07 -0.925882E+07 -0.399618E-04
*** INPUT DATA ***
TWO PHASE FLASH
MAXIMUM NO. ITERATIONS 30
CONVERGENCE TOLERANCE 0.00010000
OUTLET PRESSURE ATM 1.00000
BLOCK: REACT-2 MODEL: RSTOIC
------------------------------
INLET STREAM: 4
OUTLET STREAM: 6
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE *** MASS AND ENERGY BALANCE ***
IN OUT GENERATION RELATIVE DIFF. ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 12
U-O-S BLOCK SECTION BLOCK: REACT-2 MODEL: RSTOIC (CONTINUED)
TOTAL BALANCE
MOLE(KMOL/HR ) 198.604 177.928 -20.6763 0.125219E-15 MASS(KG/HR ) 9647.00 9647.00 0.377110E-15 ENTHALPY(KCAL/HR ) -0.925882E+07 -0.949952E+07 0.253383E-01
*** RESULTS ***
OUTLET TEMPERATURE C 80.000
OUTLET PRESSURE ATM 0.98000
HEAT DUTY KCAL/HR -0.24070E+06
VAPOR FRACTION 0.94658
REACTION EXTENTS:
REACTION REACTION
NUMBER EXTENT
KMOL/HR
1 20.676
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 13
U-O-S BLOCK SECTION BLOCK: REACT-2 MODEL: RSTOIC (CONTINUED)
BLOCK: EX-5 MODEL: HEATER
------------------------------
INLET STREAM: 16
OUTLET STREAM: 15
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE
*** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 131.614 131.614 0.000000E+00
MASS(KG/HR ) 8535.34 8535.34 0.000000E+00
ENTHALPY(KCAL/HR ) -0.964082E+07 -0.877714E+07 -0.895857E-01
*** RESULTS ***
OUTLET TEMPERATURE C 82.000
OUTLET PRESSURE ATM 1.2000
HEAT DUTY KCAL/HR 0.86368E+06
OUTLET VAPOR FRACTION 0.73941
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 14 U-O-S BLOCK SECTION BLOCK: EX-5 MODEL: HEATER (CONTINUED)
BLOCK: TOWER-2 MODEL: RADFRAC
-------------------------------
INLETS - 15 STAGE 6
OUTLETS - 11 STAGE 1
10 STAGE 14
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE
*** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 131.614 131.614 0.000000E+00
MASS(KG/HR ) 8535.34 8535.34 0.000000E+00
ENTHALPY(KCAL/HR ) -0.877714E+07 -0.871220E+07 -0.739975E-02 ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 15
U-O-S BLOCK SECTION BLOCK: TOWER-2 MODEL: RADFRAC (CONTINUED)
**** COL-SPECS ****
MOLAR VAPOR DIST / TOTAL DIST 1.00000
MOLAR REFLUX RATIO 1.00000
MOLAR DISTILLATE RATE KMOL/HR 35.0000
**** PROFILES ****
P-SPEC STAGE 1 PRES, ATM 1.05000
2 1.07000
*******************
**** RESULTS ****
*******************
*** COMPONENT SPLIT FRACTIONS ***
OUTLET STREAMS
--------------
11 10
COMPONENT:
ACETO-01 .99900 .10000E-02
ACETI-01 .31588E-03 .99968
ACETI-02 .16615E-05 1.0000
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 16
U-O-S BLOCK SECTION BLOCK: TOWER-2 MODEL: RADFRAC (CONTINUED)
*** COMPONENT SPLIT FRACTIONS ***
OUTLET STREAMS
--------------
11 10
COMPONENT:
CARBO-01 1.0000 .10671E-29
METHA-01 1.0000 .44890E-25
ETHYL-01 1.0000 .34058E-20
*** SUMMARY OF KEY RESULTS ***
TOP STAGE TEMPERATURE C 58.2078
BOTTOM STAGE TEMPERATURE C 139.922
TOP STAGE LIQUID FLOW KMOL/HR 108.694
BOTTOM STAGE LIQUID FLOW KMOL/HR 22.9202
TOP STAGE VAPOR FLOW KMOL/HR 108.694
BOTTOM STAGE VAPOR FLOW KMOL/HR 87.7633
MOLAR REFLUX RATIO 1.00000
MOLAR BOILUP RATIO 3.82908
CONDENSER DUTY (W/O SUBCOOL) KCAL/HR -782,005.
REBOILER DUTY KCAL/HR 846,957.
**** MANIPULATED VARIABLES ****
BOUNDS CALCULATED LOWER UPPER VALUE
MOLAR DISTILLATE RATE KMOL/HR 20.000 170.00 108.69
**** DESIGN SPECIFICATIONS ****
NO SPEC-TYPE QUALIFIERS UNIT SPECIFIED CALCULATED
VALUE VALUE
1 MOLE-RECOV STREAMS: 11 0.99900 0.99900 COMPS: ACETO-01
BASE-STREAMS: 15
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 17
U-O-S BLOCK SECTION BLOCK: TOWER-2 MODEL: RADFRAC (CONTINUED)
STAGE FLOW RATE FEED RATE PRODUCT RATE
KMOL/HR KMOL/HR KMOL/HR
LIQUID VAPOR LIQUID VAPOR MIXED LIQUID VAPOR
1 108.7 108.7 108.6935
2 108.9 217.4
3 108.7 217.6
4 107.1 217.3
5 98.84 215.8 98.3100
6 131.4 109.2 33.3037
7 131.5 108.5
8 131.4 108.5
12 107.3 88.49
13 110.7 84.37
14 22.92 87.76 22.9201 **** MASS FLOW PROFILES ****
STAGE FLOW RATE FEED RATE PRODUCT RATE
KG/HR KG/HR KG/HR
LIQUID VAPOR LIQUID VAPOR MIXED LIQUID VAPOR
1 6313. 6288. 6288.2234
2 6323. 0.1260E+05
3 6314. 0.1261E+05
4 6255. 0.1260E+05
5 6030. 0.1254E+05 5922.6948
6 8600. 6396. 2612.6468
7 8604. 6353.
8 8603. 6356. ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 18
U-O-S BLOCK SECTION BLOCK: TOWER-2 MODEL: RADFRAC (CONTINUED)
**** MASS FLOW PROFILES ****
STAGE FLOW RATE FEED RATE PRODUCT RATE
KG/HR KG/HR KG/HR
LIQUID VAPOR LIQUID VAPOR MIXED LIQUID VAPOR
12 9454. 6204.
13 0.1049E+05 7206.
14 2247. 8239. 2247.1182
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 19
U-O-S BLOCK SECTION BLOCK: TOWER-2 MODEL: RADFRAC (CONTINUED)
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 20
U-O-S BLOCK SECTION BLOCK: TOWER-2 MODEL: RADFRAC (CONTINUED)
BLOCK: TOWER-3 MODEL: RADFRAC
-------------------------------
INLETS - 10-1 STAGE 22
OUTLETS - 13-1 STAGE 1
12STAGE 28
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 21
U-O-S BLOCK SECTION BLOCK: TOWER-3 MODEL: RADFRAC (CONTINUED)
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE
*** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 22.9202 22.9202 0.000000E+00
MASS(KG/HR ) 2247.12 2247.12 0.708292E-13
ENTHALPY(KCAL/HR ) -0.320145E+07 -0.317237E+07 -0.908344E-02
**** COL-SPECS ****
MOLAR VAPOR DIST / TOTAL DIST 0.0
MOLAR REFLUX RATIO 2.00000
MOLAR DISTILLATE RATE KMOL/HR 1.50000
**** PROFILES ****
P-SPEC STAGE 1 PRES, ATM 2.20000
2 2.22000
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 22 OUTLET STREAMS
--------------
13-1 12
COMPONENT:
ACETO-01 .99966 .34459E-03
ACETI-01 .64482 .35518
ACETI-02 .20000E-02 .99800
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 23
U-O-S BLOCK SECTION BLOCK: TOWER-3 MODEL: RADFRAC (CONTINUED)
*** SUMMARY OF KEY RESULTS ***
TOP STAGE TEMPERATURE C 135.564
BOTTOM STAGE TEMPERATURE C 169.414
TOP STAGE LIQUID FLOW KMOL/HR 16.3751
BOTTOM STAGE LIQUID FLOW KMOL/HR 21.4202
TOP STAGE VAPOR FLOW KMOL/HR 0.0
BOTTOM STAGE VAPOR FLOW KMOL/HR 21.5410
MOLAR REFLUX RATIO 10.9168
MOLAR BOILUP RATIO 1.00564
CONDENSER DUTY (W/O SUBCOOL) KCAL/HR -163,862.
REBOILER DUTY KCAL/HR 192,942.
**** MANIPULATED VARIABLES ****
BOUNDS CALCULATED LOWER UPPER VALUE
MOLAR REFLUX RATIO 0.80000 15.000 10.917
**** DESIGN SPECIFICATIONS ****
NO SPEC-TYPE QUALIFIERS UNIT SPECIFIED CALCULATED
VALUE VALUE
1 MOLE-RECOV STREAMS: 1
2 0.99800 0.99800 COMPS: ACETI-02
BASE-STREAMS: 10-1
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 24
U-O-S BLOCK SECTION BLOCK: TOWER-3 MODEL: RADFRAC (CONTINUED)
**** PROFILES ****
ENTHALPY
STAGE TEMPERATURE PRESSURE CAL/MOL HEAT DUTY
C ATM LIQUI
D VAPOR KCAL/HR
1 135.56 2.2000 -0.10770E+06 -86667. -.16386+06
2 144.0
3 2.2200 -0.11114E+06 -98532.
21 166.60 2.2931 -0.13869E+06 -0.12713E+06
22 166.68 2.2969 -0.13869E+06 -0.12715E+06
23 167.10 2.3008 -0.13892E+06 -0.12779E+06
26 168.31 2.3123 -0.13975E+06 -0.12931E+06
27 168.83 2.3162 -0.14013E+06 -0.12997E+06
28 169.41 2.3200 -0.14056E+06 -0.13074E+06 .19294+06
STAGE FLOW RATE FEED RATE PRODUCT RATE
KMOL/HR KMOL/HR KMOL/HR
LIQUID VAPOR LIQUID VAPOR MIXED LIQUID VAPOR
1 16.38 0.0000E+00 1.5000
2 16.50 17.88
21 16.73 18.23
22 42.76 18.23 22.9201
23 42.81 21.34
26 42.92 21.46
27 42.96 21.50
28 21.42 21.54 21.4201 **** MASS FLOW PROFILES ****
STAGE FLOW RATE FEED RATE PRODUCT RATE
KG/HR KG/HR KG/HR
LIQUID VAPOR LIQUID VAPOR MIXED LIQUID VAPOR
1 1000. 0.0000E+00 91.6074
2 1022. 1092.
21 1642. 1732.
22 4196. 1733. 2247.1182
23 4212. 2041.
26 4271. 2093.
27 4298. 2115.
28 2156. 2142. 2155.5107 ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 25
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 26
U-O-S BLOCK SECTION BLOCK: TOWER-1 MODEL: RADFRAC
-------------------------------
INLETS - 9-2 STAGE 12
14 STAGE 1
OUTLETS - 9 STAGE 1
17 STAGE 12
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE *** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 67.8844 67.8844 0.209339E-15
MASS(KG/HR ) 2407.00 2407.00 -0.188927E-15
ENTHALPY(KCAL/HR ) -0.340920E+07 -0.342097E+07 0.343968E-02
**** COL-SPECS ****
MOLAR VAPOR DIST / TOTAL DIST 1.00000
CONDENSER DUTY (W/O SUBCOOL) KCAL/HR 0.0 REBOILER DUTY KCAL/HR 0.0
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 27
U-O-S BLOCK SECTION BLOCK: TOWER-1 MODEL: RADFRAC (CONTINUED)
**** PROFILES ****
P-SPEC STAGE 1 PRES, ATM 4.94000
2 4.94800
*******************
**** RESULTS ****
*******************
*** COMPONENT SPLIT FRACTIONS ***
OUTLET STREAMS
--------------
9 17
COMPONENT:
ACETO-01 .21479E-05 1.0000
ACETI-01 .69483E-02 .99305
ACETI-02 .10001E-21 1.0000
CARBO-01 .99864 .13607E-02
METHA-01 .99498 .50199E-02
ETHYL-01 .98160 .18405E-01
*** SUMMARY OF KEY RESULTS ***
TOP STAGE TEMPERATURE C 26.4755
BOTTOM STAGE TEMPERATURE C 63.7668
TOP STAGE LIQUID FLOW KMOL/HR 21.7834
BOTTOM STAGE LIQUID FLOW KMOL/HR 26.9563
TOP STAGE VAPOR FLOW KMOL/HR 40.9280
BOTTOM STAGE VAPOR FLOW KMOL/HR 44.7483
CONDENSER DUTY (W/O SUBCOOL) KCAL/HR 0.0 REBOILER DUTY KCAL/HR 0.0
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 28
U-O-S BLOCK SECTION BLOCK: TOWER-1 MODEL: RADFRAC (CONTINUED)
**** PROFILES ****
ENTHALPY
STAGE TEMPERATURE PRESSURE CAL/MOL HEAT DUTY
C ATM LIQUI
D VAPOR KCAL/HR
1 26.475 4.9400 -0.11330E+06 -16831.
2 28.018 4.9480 -0.11325E+06 -16799.
7 44.204 4.9730 -0.11222E+06 -17243.
8 46.579 4.9780 -0.11109E+06 -17456. -.11767+05
9 60.699 4.9830 -0.10948E+06 -18599.
11 68.574 4.9930 -0.10601E+06 -20092.
12 63.767 4.9980 -0.10135E+06 -20177.
STAGE FLOW RATE FEED RATE PRODUCT RATE
KMOL/HR KMOL/HR KMOL/HR
LIQUID VAPOR LIQUID VAPOR MIXED LIQUID VAPOR
1 21.78 40.93 21.5700 40.9280
2 21.81 41.14
7 22.32 41.46
8 83.23 41.68 60.0000 60.0000
9 24.12 42.59
11 25.39 44.14
12 26.96 44.75 46.3143 26.9563
**** MASS FLOW PROFILES ****
STAGE FLOW RATE FEED RATE PRODUCT RATE
KG/HR KG/HR KG/HR
LIQUID VAPOR LIQUID VAPOR MIXED LIQUID VAPOR
1 1300. 807.7 1295.3337 807.7133
2 1302. 812.8
7 1332. 832.3
8 4966. 844.7 3579.5922 3579.5922
9 1438. 898.3
11 1511. 989.0
12 1599. 1024. 1111.6621 1599.2825 ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 29
U-O-S BLOCK SECTION BLOCK: TOWER-1 MODEL: RADFRAC (CONTINUED)
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 30
U-O-S BLOCK SECTION BLOCK: TOWER-1 MODEL: RADFRAC (CONTINUED)
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 31
U-O-S BLOCK SECTION BLOCK: TOWER-1 MODEL: RADFRAC (CONTINUED)
STREAM MOLE-FLOW TEMPERATURE DUTY
KMOL/HR C KCAL/HR
P-2 60.0000 40.0000 -1.1767+04
BLOCK: SEP-2 MODEL: FLASH2
------------------------------
INLET STREAM: 13
OUTLET VAPOR STREAM: 9-2
OUTLET LIQUID STREAM: 8-1
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE
*** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 73.0028 73.0028 -0.194662E-15
MASS(KG/HR ) 2656.93 2656.93 0.102659E-11
ENTHALPY(KCAL/HR ) -0.239511E+07 -0.251457E+07 0.475085E-01
*** RESULTS ***
OUTLET TEMPERATURE C 40.000
OUTLET PRESSURE ATM 5.0000
HEAT DUTY KCAL/HR -0.11946E+06
VAPOR FRACTION 0.63442
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 32
U-O-S BLOCK SECTION BLOCK: SEP-2 MODEL: FLASH2 (CONTINUED)
BLOCK: EX-6 MODEL: HEATER
------------------------------
INLET STREAM: 12
OUTLET STREAM: 12-1
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE
*** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 21.4202 21.4202 0.000000E+00
MASS(KG/HR ) 2155.51 2155.51 0.000000E+00
ENTHALPY(KCAL/HR ) -0.301082E+07 -0.312262E+07 0.358042E-01
*** RESULTS ***
OUTLET TEMPERATURE C 50.000
OUTLET PRESSURE ATM 1.2000
HEAT DUTY KCAL/HR -0.11180E+06
OUTLET VAPOR FRACTION 0.00000E+00
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 33
U-O-S BLOCK SECTION BLOCK: EX-6 MODEL: HEATER (CONTINUED)
BLOCK: PUMP3 MODEL: PUMP
----------------------------
INLET STREAM: 10
OUTLET STREAM: 10-1
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE *** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 22.9202 22.9202 0.000000E+00
MASS(KG/HR ) 2247.12 2247.12 0.000000E+00
ENTHALPY(KCAL/HR ) -0.320188E+07 -0.320145E+07 -0.135796E-03
FLASH SPECIFICATIONS:
LIQUID PHASE CALCULATION
NO FLASH PERFORMED
MAXIMUM NUMBER OF ITERATIONS 30
TOLERANCE 0.00010000
*** RESULTS ***
VOLUMETRIC FLOW RATE (L/MIN ) 47.8538
PRESSURE CHANGE (ATM ) 1.85000
NPSH AVAILABLE (METER ) 0.0
FLUID POWER (KW ) 0.14950
BRAKE POWER (KW ) 0.50567
ELECTRICITY (KW ) 0.50567
PUMP EFFICIENCY USED 0.29566 NET WORK (KW ) -0.50567
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 34
U-O-S BLOCK SECTION BLOCK: COOL2 MODEL: HEATER
------------------------------
INLET STREAM: 9-1
OUTLET STREAM: 13
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE *** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 73.0028 73.0028 0.000000E+00
MASS(KG/HR ) 2656.93 2656.93 0.000000E+00
ENTHALPY(KCAL/HR ) -0.231777E+07 -0.239511E+07 0.322903E-01
*** RESULTS ***
OUTLET TEMPERATURE C 30.000
OUTLET PRESSURE ATM 1.0000
HEAT DUTY KCAL/HR -77339.
OUTLET VAPOR FRACTION 0.87740
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 35
U-O-S BLOCK SECTION BLOCK: COOL1 MODEL: HEATER
------------------------------
INLET STREAM: 6
OUTLET STREAM: 6-1
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE *** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 177.928 177.928 0.000000E+00
MASS(KG/HR ) 9647.00 9647.00 0.000000E+00
ENTHALPY(KCAL/HR ) -0.949952E+07 -0.103889E+08 0.856112E-01
*** RESULTS ***
OUTLET TEMPERATURE C 40.000
OUTLET PRESSURE ATM 1.0000
HEAT DUTY KCAL/HR -0.88941E+06
OUTLET VAPOR FRACTION 0.41029
ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 36
U-O-S BLOCK SECTION BLOCK: PUMP2 MODEL: PUMP
----------------------------
INLET STREAMS: 8 8-1
OUTLET STREAM: 16
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE *** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 131.614 131.614 0.000000E+00
MASS(KG/HR ) 8535.34 8535.34 -0.213113E-15
ENTHALPY(KCAL/HR ) -0.964230E+07 -0.964082E+07 -0.152898E-03
FLASH SPECIFICATIONS:
LIQUID PHASE CALCULATION
NO FLASH PERFORMED
MAXIMUM NUMBER OF ITERATIONS 30
TOLERANCE 0.00010000
*** RESULTS ***
VOLUMETRIC FLOW RATE (L/MIN ) 177.676
PRESSURE CHANGE (ATM ) 4.00000
NPSH AVAILABLE (METER ) -10.8842
FLUID POWER (KW ) 1.20020
BRAKE POWER (KW ) 1.71457
ELECTRICITY (KW ) 1.71457
PUMP EFFICIENCY USED 0.70000
NET WORK (KW ) -1.71457
NEGATIVE NPSH MAY BE DUE TO VAPOR IN THE FEED OR UNACCOUNTED SUCTION HEAD. BLOCK: EX-2 MODEL: HEATER
------------------------------
INLET STREAM: 5-1
OUTLET STREAM: 5-2
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 37
U-O-S BLOCK SECTION BLOCK: EX-2 MODEL: HEATER (CONTINUED)
*** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 170.158 170.158 0.000000E+00
MASS(KG/HR ) 7956.57 7956.57 0.000000E+00
ENTHALPY(KCAL/HR ) -0.518896E+07 -0.578470E+07 0.102986
*** RESULTS ***
OUTLET TEMPERATURE C 250.00
OUTLET PRESSURE ATM 1.0000
HEAT DUTY KCAL/HR -0.59574E+06
OUTLET VAPOR FRACTION 1.0000
BLOCK: EX-3 MODEL: HEATER
------------------------------
INLET STREAM: 5-2
OUTLET STREAM: 5-3
PROPERTY OPTION SET: PENG-ROB STANDARD PR EQUATION OF STATE ASPEN PLUS VER: WIN32 REL: 10.0-1 05/14/2010 PAGE 38
U-O-S BLOCK SECTION BLOCK: EX-3 MODEL: HEATER (CONTINUED)
*** MASS AND ENERGY BALANCE ***
IN OUT RELATIVE DIFF.
TOTAL BALANCE
MOLE(KMOL/HR ) 170.158 170.158 0.000000E+00
MASS(KG/HR ) 7956.57 7956.57 0.000000E+00
ENTHALPY(KCAL/HR ) -0.578470E+07 -0.615877E+07 0.607378E-01
*** RESULTS ***
OUTLET TEMPERATURE C 140.00
OUTLET PRESSURE ATM 1.0000
HEAT DUTY KCAL/HR -0.37407E+06
OUTLET VAPOR FRACTION 1.0000 BLOCK: EX-1 MODEL: HEATER
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