Calculo De Separadores Trifasicos
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Publicado: 15 de septiembre de 2011
Successfully Specify Three-Phase Separators
Here is a stepwise procedure Jor
designing
I
Uquid/liquid/vapor
separators.
is "ften necessary to "'parale Iwo immi",ibltliquids. ,he light and l>eavy phases. and a yapot. A typ;cal example in petroleum refining is the separruion of waler. and a hydrocarbon liquid and vapor. Linle ha$ bun publisll,,,counter· parts. except thai the liqu.id oection dif· fen. fur the: vertical type. I baffle com· monly ~eeps the liquid "'paration
W I"" O _ .
,..., .... Willi...
Y s""'.1er. •'pecified.• uch ... a slug >Inme). 5. Obtain UD from Table 7 and initially o.kulate the diameter accoJding to:
2:
L,,VH+V, - AT A v - AUL
('"
Round to the ft. The minimum for L,_ d,,+ 12 in. 10. Set the interface at the height H"n.. obtaining the height. of the heavy and light liquid •. HHI. and II!./.. 11. For the liquid "'Uling O/IfIal and high liquidlevels;
H~I..L= D -H.
(55)
(52)
A.,''''' = AUJ." V,/L.,
A~ufAT"
(53)
60 min for refinery ... ",ice. or IO----l S min for cl> L"IN< lile des.ign i. ,",ce[JI' able fOfvaporlliquid :lC1"'r.llion . 11. Calculate ,he lighl liquid t.yer Ihlckness based 00 IlIe I>
,-
holdup/surge (typically, 5---1~ min); assume /Ill is about 6 in. below the woir heightand UL is about 6 in. above the boito", of the vessel . U.ing T" ble 1 with IIn dO and lidO. cal· culate ),HU, and Aw;. Cakuhue L.-
(TH T.}Qm. +
L,' (A~u. -A,L!. )
Ihctor by 6-in.incremtd I>q>a,,"e Iho .~x(U'" in Table 10. n.e opera,ill3 pttSSun: and 'cmpc"'tun: are 2'i psig and 100, respecti,.. ly. and it i. ne "" this page. U... 'n " '; in,; ~se 1 _ ,., in.2!. A,,, 1l(11.0 ft) ( 19.5 ft) .. 673 .87 ft, AN - (0. 841) (11.0 ft)' _ 101.88 ft' 23. See Eq, E 19. box on thi, page. 2J . In Ihi. e .. mple. cakulalions 'Oi"'" performed for only On
Here is a stepwise procedure Jor
designing
I
Uquid/liquid/vapor
separators.
is "ften necessary to "'parale Iwo immi",ibltliquids. ,he light and l>eavy phases. and a yapot. A typ;cal example in petroleum refining is the separruion of waler. and a hydrocarbon liquid and vapor. Linle ha$ bun publisll,,,counter· parts. except thai the liqu.id oection dif· fen. fur the: vertical type. I baffle com· monly ~eeps the liquid "'paration
W I"" O _ .
,..., .... Willi...
Y s""'.1er. •'pecified.• uch ... a slug >Inme). 5. Obtain UD from Table 7 and initially o.kulate the diameter accoJding to:
2:
L,,VH+V, - AT A v - AUL
('"
Round to the ft. The minimum for L,_ d,,+ 12 in. 10. Set the interface at the height H"n.. obtaining the height. of the heavy and light liquid •. HHI. and II!./.. 11. For the liquid "'Uling O/IfIal and high liquidlevels;
H~I..L= D -H.
(55)
(52)
A.,''''' = AUJ." V,/L.,
A~ufAT"
(53)
60 min for refinery ... ",ice. or IO----l S min for cl> L"IN< lile des.ign i. ,",ce[JI' able fOfvaporlliquid :lC1"'r.llion . 11. Calculate ,he lighl liquid t.yer Ihlckness based 00 IlIe I>
,-
holdup/surge (typically, 5---1~ min); assume /Ill is about 6 in. below the woir heightand UL is about 6 in. above the boito", of the vessel . U.ing T" ble 1 with IIn dO and lidO. cal· culate ),HU, and Aw;. Cakuhue L.-
(TH T.}Qm. +
L,' (A~u. -A,L!. )
Ihctor by 6-in.incremtd I>q>a,,"e Iho .~x(U'" in Table 10. n.e opera,ill3 pttSSun: and 'cmpc"'tun: are 2'i psig and 100, respecti,.. ly. and it i. ne "" this page. U... 'n " '; in,; ~se 1 _ ,., in.2!. A,,, 1l(11.0 ft) ( 19.5 ft) .. 673 .87 ft, AN - (0. 841) (11.0 ft)' _ 101.88 ft' 23. See Eq, E 19. box on thi, page. 2J . In Ihi. e .. mple. cakulalions 'Oi"'" performed for only On
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