B違pi"3. 16 So sánh d英"nk羽w"vjw"vj壱r"ucw"mjk"e違k"vk院p"xà thi院v"m院"dcp"8亥w c栄c" tháp C-05
Thơng s嘘 A挨p"x鵜 Thi院v"m院"dcp"8亥w C違k"vk院p
T鰻pi"v鰻p"vj医v"gzgti{" c栄c"vjƒr"E-05 kW 204,6 2,9 N逢w"n逢嬰pi"mj嘘k" n逢嬰pi"fịng 15 Kg/s 33,811 31,481 N逢w"n逢嬰pi"mj嘘k" n逢嬰pi"fịng 17 Kg/s 21,184 23,514 J o"n逢嬰pi"E3"vtqpi" dịng 15 Ph亥p"oqn 0,827 0,844
JXVX<"Rj́pi"Aình Li吋u Trang 73
Thơng s嘘 A挨p"x鵜 Thi院v"m院"dcp"8亥w C違k"vk院p
J o"n逢嬰pi"E4"vtqpi"
dịng 15 Ph亥p"oqn 0,152 0,131
J o"n逢嬰pi"E5"vtqpi"
dịng 15 Ph亥p"oqn 0,015 0,019
Xét v隠"o員v"jk羽w"sw違"p<pi"n逢嬰pi."ucw"mjk"jk羽w"ej雨pj"e違k"vk院p"8k隠w ki羽p"pj壱r"nk羽w."
m泳e"8瓜"v鰻p"vj医v"gzgti{"e栄c"vjƒr"Fgogvhanier C-27"8ã gi違o"mjq違pi";:.8%. Ngồi ra, hi羽w"sw違"rj¤p"vƒej"Ogvjcpg"vtqpi"fịng s違p"rj育o"8雨pj"37"e pi"8逢嬰e"e違k"vjk羽p"v瑛"
82,7% lên 84,4% và do v壱{."rj亥p"oqn"v逢挨pi"泳pi"e栄c"E4-"vtqpi"fịng s違p"rj育o" 8雨pj"e pi"ik違o"zw嘘pi"*v鰻pi"rj亥p"oqn"E4"xà C3 gi違o"3.9'+0
Vw{"pjk‒p."8k"8»k"o泳e"e違k"vjk羽p"jk羽w"sw違"p<pi"n逢嬰pi"8ƒpi"m吋."xk羽e"jk羽w"ej雨pj"vj»pi"
s嘘"pjk羽v"8瓜"e栄c"fịng nh壱r"nk羽w"8雨pj"34g"xà 14 d磯p"8院p"{êu c亥w"8k隠w"ej雨pj"n衣k"j羽"
th嘘pi"vtcq"8鰻k"pjk羽v"vtqpi"e映o"vjƒr"Fgogvhanizer C-05. C映"vj吋."xk羽e"v<pi"pjk羽v"8瓜"
dịng nh壱r"nk羽w"34g"v瑛"-600C lên -400C s胤"f磯p"8院p"{êu c亥w"ikc"pjk羽v"b鰻"uwpi"ejq"
dịng nh壱r"nk羽w"pày sau khi qua van ti院v"n逢w"VLV-101 (FV-1001) và vi羽e"ik違o"pjk羽v" 8瓜"fịng 14 t瑛"-18,50C 8院p -350C s胤"f磯p"8院p"yêu c亥w"làm l衣pj"fịng nh壱r"nk羽w"pày sau khi giãn n叡"swc"Vwtdq"Gzrcpfgt"EE-230"Pj逢"x壱{."pjìn chung cĩ th吋"ejw{吋p"
ph亥p"pjk羽v"n逢嬰pi"f逢"vj瑛c"vtqpi"fịng 14 sang dịng 12e 8吋"e„"vj吋" v壱p"f映pi"p<pi" n逢嬰pi0"Ik違k"rjƒr"pày yêu c亥w"eƒe"pijkên c泳w"ejk"vk院v"j挨p"8吋"e„"vj吋"8ƒpj"ikƒ"v鰻ng th吋"vqàn h羽"vj嘘pi"vtcq"8鰻k"pjk羽v"vtqpi"c映o"vjƒr"Fgogvjcpk¦gt."o "8員e"dk羽v"nà các thi院v"d鵜"eịn cĩ kh違"p<pi"e違k"vjk羽p"jk羽w"sw違"jq衣v"8瓜pi"pj逢"8ã trình bày trong M映e" 3.2 t瑛"8„"gĩp ph亥p"ti院v"mk羽o"ejk"rj "e違k"vk院p. Bên c衣pj"8„."x噂k"ik違k"rjƒr"e違k"vk院p."
m員v"fù tính ch医v"eƒe"fịng s違p"rj育o"mj»pi"swƒ"mjƒe"dk羽v"uq"x噂k"vjk院v"m院"dcp"8亥w."vw{"
nhiên, vi羽e"tà sốt l衣k"違pj"j逢荏pi"e栄c"eƒe"vj»pi"u嘘"e違k"vk院p"nên tồn h羽"vj嘘pi"nà th壱v"
JXVX<"Rj́pi"Aình Li吋u Trang 74
EJ姶愛PI"6 - K蔭T LU一N VÀ KI蔭N NGH卯
E<p"e泳"vjgq"f英"nk羽w"vjk院v"m院"eƒe"vjk院v"d鵜"e»pg ngh羽"ej pj"e栄c"pjà máy c pi"pj逢"eƒe"
yêu c亥w"tàng bu瓜e"x隠"v pj"ej医v"piw{ên li羽w"xà s違p"rj育o."rj亥p"o隠o"J{u{u"8ã 8逢嬰e"
s穎"f映pi"8吋"o»"rj臼pi"v pj"vqƒp"v pj"ej医v"e栄c"eƒe"fịng v壱v"ej医v"xà thi院v"d鵜0"X噂k"vj院"
m衣pj"vtqpi"xk羽e"o»"rj臼pi"eƒe"sw{"vtình d亥w"mj "p„k"ejwpi x "8員e"dk羽v"n "8嘘k"x噂k"
các quy trình ch院"dk院p"mj nĩi riêng, k院v"sw違"v鰻pi"j嬰r"vj»pi"u嘘"jq衣v"8瓜pi"e栄c"eƒe"
thi院v"d鵜"ej pj"vtqpi"j羽"vj嘘pi"e pi"pj逢"u嘘"nk羽w"eƒe"fịng s違p"rj育o"vjw"pj壱p"v瑛"m院v"
qu違"o»"rj臼pi"thơng qua Hysys 8隠w"e„"u詠"ejênh l羽ej"mj»pi"8ƒpi"m吋"x噂k"u嘘"nk羽w"
thi院v"m院"e栄c"pjà máy. Do v壱{."f英"nk羽w"o»"rj臼pi"nk‒p"swcp"8院p"8嘘k"pijkên c泳w"nà c映o"vjƒr"E-05 cĩ th吋"8逢嬰e"vt ej"zw医v"v瑛"m院v"sw違"o»"rj臼pi"j羽"vj嘘pi"e»pi"pij羽"e栄c"
nhà máy nh茨o"rj映e"x映"ejq"xk羽e"rj¤p"v ej"u¤w"jk羽w"sw違"u穎"f映pi"p<pi"n逢嬰pi.
K院v"sw違"v pj"vqƒp cho th医{"jk羽w"uw医v"gzgti{"荏"h亥w"j院v"eƒe"vjk院v"d鵜"8隠w"v逢挨pi"8嘘k"ecq.
A嘘k"x噂k"d瓜"ikc"ejkc"fịng TEE-101, hi羽w"uw医v"8衣v"322'"fq"d違p"ej医v"e栄c"jq衣v"8瓜pi"
c栄c"vjk院v"d鵜"mj»pi"違pj"j逢荏pi"8隠p"eƒe"vj»pi"u嘘"gpvtqr{"xà enthanlpy c栄c"eƒe"fịng v壱v"ej医v0"A嘘k"x噂k"vjk院v"d鵜"iia nhi羽v"d鰻"uwpi"G-102, vi羽e"rj¤p"v ej"ejk"vk院v"mj違"p<pi"
cung c医r"pjk羽v"n逢嬰pi"d鰻"uwpi"8吋"ikc"pjk羽v"fịng nh壱r"nk羽w"8雨pj"vjƒr"E-05 c亥p"8逢嬰e"
xem xét k院v"j嬰r"mjk"8ƒpj"ikƒ"ejq"vqàn tháp tách.
K院v"sw違"rj¤p"v ej"v pj"ej医v"pjk羽v"8瓜pi"e栄c"vjƒr"E-05 v噂k"u詠"j厩"vt嬰"c栄c"e»pi"e映"
Column Targetting trong ph亥p"o隠o"Curgp"Rnwu"ejq"vj医{"t鰻pi"vj医v"vjqƒv"gzgti{"ijk"
nh壱p"荏"m泳e"426 kW khi v壱p"jành theo các thơng s嘘"vjk院v"m院 hi羽p"v衣k."vtqpi"8„"8 c"
th泳"pj医v"(nh壱r"nk羽w"8雨pj+"e„"o泳e"v鰻p"vj医v l噂p"pj医v0"O泳e"8瓜"8„pi"i„r"e栄c"8 c"pj壱r"
li羽w"8雨pj ghi nh壱p"vtên 80% t鰻pi"v鰻p"vj医v"gzgti{0
Các bi吋w"8欝"EIEE"mj»pi"ejq"vj医{"u詠"dk院p"f衣pi"8ƒpi"m吋"ik英c"8k隠w"mk羽p"vj壱v"x "8k隠w"
ki羽p"n#"v逢荏pi0"Fq"x壱{"xk羽e"8k隠w"ej雨pj"v益"u嘘"j欝k"n逢w"x "d嘘"vt "eƒe"d瓜"ikc"pjk羽v"pi逢pi"
JXVX<"Rj́pi"Aình Li吋u Trang 75 c栄c"vjƒr"E-05, thơng s嘘"pjk羽v"8瓜"c栄c"eƒe"dịng nh壱r"nk羽w"u胤"8逢嬰e"逢w"vk‒p"mj違q"uƒv"8吋"
tránh kh違"p<pi"rj違k"vjc{"8鰻k"m院v"e医w"jk羽p"e„"e栄c"vjk院v"d鵜0
永pi"x噂k m泳e"pjk羽v"8瓜"-18,50C c栄c"fịng 14, k院v"sw違"rj¤p"v ej"ejq"vj医y m泳e"8瓜"v鰻p"
th医v"gzgti{"e栄c"vjƒr"8衣v"e詠e"vk吋w"荏"khi nhi羽v"8瓜"fịng 12e x医r"z雨"-200C. V逢挨pi"v詠." 泳ng v噂k"m泳e"pjk羽v"8瓜"-600C c栄c"fịng 12e, cĩ th吋"pj壱p"vj医{"o泳e"8瓜"v鰻p"vj医v"gzgti{"
c栄c"vjƒr"ik違o"8ƒpi"m吋"mjk"pjk羽v"8瓜"fịng nh壱r"nk羽w"36"ik違o0"Ikƒ"vt鵜"v鰻p"vj医v"e詠e"ti吋w"
ghi nh壱p"mjk"pjk羽v"8瓜"fịng nh壱r"nk羽w"pày x医r"z雨"-600C. Tuy nhiên, trong khi v医p"8隠"
hi羽w"uw医v"8逢嬰e"ik違k"sw{院v"vtk羽v"8吋"vjì các ràng bu瓜e"x隠"ej医v"n逢嬰pi"xà s嘘"n逢嬰pi"u違p"
ph育o"e„"u詠"vjc{"8鰻k"8ƒpi"m吋"uq"x噂k"f英"nk羽w"jq衣v"8瓜pi"e栄c"pjà máy.
D英"nk羽w phân tích cho th医{"mj違"p<pi"8k隠w"ej雨pj"m院v"j嬰r"pjk羽v"8瓜"e栄c"e違"4"fịng nh壱r"
li羽w"34g"x "36"8吋"e„"vj吋"8衣v"8逢嬰e"o泳e"v鰻p"vj医v"gzgti{"v嘘k"vjk吋w"pj逢pi"x磯p"fw{"vtì các thơng s嘘"ej医v"n逢嬰pi"xà s嘘"n逢嬰pi"u違p"rj育o"荏"o泳e"dk院p"8鰻k"mj»pi"swƒ"n噂p"uq"x噂k"
m泳e"jq衣v"8瓜pi"vjk院v"m院 c栄c"pjà máy. Sau khi ti院p"j pj"eƒe"d逢噂e"rj¤p"v ej"8ƒpj"ikƒ, nhi羽v"8瓜"eƒe"fịng nh壱r"nk羽w"34g"x "36"8逢嬰e"8隠"zw医v"n亥p"n逢嬰v"荏"eƒe"o泳e"-400C và - 350C. 雲"8k隠w"mk羽p"x壱p"jành này, m泳e"8瓜"v鰻p"vj医v"gzgti{"e栄c"vjƒr C-05 gi違o"8ƒpi"
k吋"zw嘘pi cịn kho違pi"5"mYv逢挨pi"8逢挨pi"x噂k m泳c gi違o";:.8% so v噂k"8k隠w"mk羽p"vjk院v"
k院. Ngồi ra, hi羽w"sw違"rj¤p"vƒej"Ogvjcpg"vtqpi"fịng s違p"rj育o"8雨pj"37"e pi"8逢嬰e"
c違k"vjk羽p"v瑛":4.9'"nên 84,4% và do v壱{."rj亥p"oqn"v逢挨pi"泳pi"e栄c"E4-"vtqpi"fịng s違p"rj育o"8雨pj"e pi"ik違o"zw嘘pi"*v鰻pi"rj亥p"oqn"E4"xà C3 gi違o"3.9').
Tuy nhiên, vi羽e"v<pi"pjk羽v"8瓜"fịng nh壱r"nk羽w"34g"v瑛"-600C lên -400C s胤"f磯p"8院p"{êu c亥w"ikc"pjk羽v"d鰻"uwpi"ejq"fịng nh壱r"nk羽w"pày sau khi qua van ti院v"n逢w"XNX-101 (FV-1001) và vi羽e"ik違o"pjk羽v"8瓜"fịng 14 t瑛"-18,50E"8院p"-350C s胤"f磯p"8院p"yêu c亥w"
làm l衣pj" fịng nh壱r" nk羽w" pày sau khi giãn n叡" swc" Vwtdq" Gzrcpfgt" EE-01. Do
JXVX<"Rj́pi"Aình Li吋u Trang 76
jq p"8鰻k"eƒe"fịng nh壱r"nk羽w"e„"vj吋"zgo"zfiv"8吋"e„"vj吋"8違o"d違q"v pj"mj違"vjk"x隠"o員v"
k悦"vjw壱v"n磯p"mkpj"v院"mji th詠e"jk羽p"eƒe"ik違k"rjƒr"e違k"vk院p0
Pj逢"x壱{."m院v"j嬰r"x噂k"m院v"sw違"rj¤p"v ej"jk羽w"uw医v"gzgtiy cho các thi院v"d鵜"vjành ph亥p,
8吋"c違k"vjk羽p"jk羽w"sw違"jq衣v"8瓜pi"e栄c"vjƒr"Fgogvjcpk¦gt"泳pi"x噂k"u詠"jk羽w"ej雨pj"pjk羽v" 8瓜"eƒe"fịng nh壱r"nk羽w."e亥p"zgo"n衣k"j羽"vj嘘pi"vtcq"8鰻k"nhi羽v"vtqpi"e映o"vjƒr"vƒej"E-05 nĩi chung và tồn b瓜"sw{"vtình cơng ngh羽"e栄c"pjà máy nĩi riêng. Gi違k"rjƒr"rj¤p" v ej"8k吋o"Rkpej"ejq"j羽"vj嘘pi"vtcq"8鰻k"pjk羽v"e栄c"pjà máy cĩ th吋"8逢嬰e"zgo"zfiv"vj詠e"
hi羽p"ejq"eƒe"pijkên c泳w"vk院r"vjgq"pj茨o"v嘘k"逢w"j„c"vjk院v"m院0 A欝pi"th運k."xk羽e"rj¤p"
tích chi ti院v"jk羽w"sw違"u穎"f映pi"p<pi"n逢嬰pi"e栄c"eƒe"e映o"vjk院v"d鵜"mjƒe"vtqpi"j羽"vj嘘pi"
cơng ngh羽" e栄c" pjà máy c pi" e„" vj吋" ewpi" e医r" vj‒o" eƒe" j逢噂pi" e違k" vk院p" d鰻" uwpi"
JXVX<"Rj́pi"Aình Li吋u Trang 77
TÀI LI烏U THAM KH謂O Ti院pi"Xk羽v
1. Chính Ph栄" Xk羽v" Pco, 2011. Ngh鵜" 8鵜pj" u嘘" 95142331PA-CP - Sw{" 8おpj"xぬ"
phＴv"xk"rjＴo"jành chính vｚ"uぬ"fつpi"p<pi"n⇔ぢpi"vkｘv"mkうo"xà hiうw"swＶ.
2. Chính Ph栄"Xk羽v"Pco, 2011.Ngh鵜"8鵜pj"u嘘"43142331PA-CP - Sw{"8おpj"chi tiｘv"
và biうp"rjƒr"vjk"jành luｆv"uぬ"dつpi"p<pi"n⇔ぢpi"vkｘv"mkうo"xà hiうw"swＶ.
3. Nhà máy ch院"dk院p"mj "Fkpj"E嘘. Các thơng sぐ"e»pi"pijう"x "eƒe"u￢"8げ"e»pi"
nghう."dＶp"xｖ"vjkｘv"dお.
4. Qu嘘e"J瓜k"Xk羽v"Pco, 2010. Luｆv"uぬ"fつpi"p<pi"n⇔ぢpi"vkｘv"mkうo"xà hiうw"swＶ.
Ti院pi"Cpj
5. Agrawal, R., Herron, D.M. 1998. Efficient use of an intermediate reboiler or condenser in a binary distillation. AIChE J 44, 1303-1315.
6. Arẳjo, A.B., Brito, R.P., Vasconcelos, L.S. 2003. Exergetic analysis of distillation processes-A case study. Energy 32, 1185-1193.
7. Arif Hepbasli, 2006. A key review on exergetic analysis and assessment of renewable energy resources for a sustainable future.
8. Aspen Engineering Suite, 2004. www.aspentech.com.
9. Bandyopadhyay, S., Malik, R.K., Shenoy, U.V. 1998. Temperature-enthalpy curve for energy targeting of distillation columns. Comput Chem Eng 22, 1733-1744.
10. Bo Chen, Zuwei Liao, Jingdai Wang, Huanjun Yu, Yongrong Yang, 2011.
JXVX<"Rj́pi"Aình Li吋u Trang 78 11. Changalvaie, Abbas Ali, Feghhi, Shariyar, 2011. Exergy analysis for
evaluation of energy consumption in an olefin plant.
12. Chang, H., Li, Jr-W. 2005. A new exergy method for process analysis and optimization. Chem Eng Sci 60, 2771-2784.
13. De Koeijer, G.M., Rivero, R. 2003. Entropy production and exergy loss in experimental distillation columns. Chem Eng Sci 58, 1587-97.
14. Demirel, Y., Sandler, S.I. 2004. Nonequilibrium thermodynamics in engineering and science. J Phys Chem 108, 31-43.
15. Ibrahim Dincer, Marc A. Rosen, 2007. Exergy: Energy, environment and sustainable development.
16. J. D. Seader, Ernest J. Henley, 2005. Separation Process Principles, 2nd Edition.
17. Marc A. Rosen, 2002. Clarifying thermodynamic efficiencies and losses via exergy.
18. Mohd. Kamaruddin Abd Hamid, 2007. HYSYS: An Introduction to Chemical Engineering Simulation.
Pi {"vjƒpi"p<o"ukpj< 21/08/1985 P挨k"ukpj< B院p"Vtg
A鵜c"ej雨"nkên l衣e< 159/1 H欝"X<p"Jw‒."Rj逢運pi";."Sw壱p"Rj¿"Pjw壱p."Vjành ph嘘"J欝"
Chí Minh
QUÁ TRÌNH ẮQ"V萎Q:
Sinh viên Khoa Cơng ngh羽"J„c"j丑e"- A衣k"j丑e"Dƒej"mjqc"Vjành ph嘘"J欝"Ej "Okpj
khĩa 2004 – 2009.
QUÁ TRÌNH CƠNG TÁC:
Cơng tác t衣k"Trung tâm Nghiên c泳w"xà Phát tri吋p"Cp"Vq p"x "O»k"vt逢運pi"F亥w"mj "
(CPSE) – Vi羽p"F亥w"mj "Xk羽v"Pco"*XRK+ t瑛"vjƒpi"5"p<o"422;"8院p"pc{0
Khí đồng hành V-08 C-05 E-07 V-03 Nước E-04 ME-24 Condensate C-01 V-15 E-01A/B Dầu nóng
Sơ đồ công nghệ chế độ AMF
Ký hiệu:
C – Tháp tách phân đoạn. V – Thiết bị tách.
SC – Slug-Catcher.
E – Thiết bị trao đổi nhiệt. P – Bơm. ME – Thiết bị đo đếm. SC E-09 TK-21 Dầu nóng
E-15 E-18 V-07 K-04 F-01 E-20 V-12 K-01 FV-1701 E-04 E-01A/B V-15 FV-1301 E-02 V-02 P-01A/B E-03 E-09 ME-24 ME-26 ME-25 E-07 V-03 Nước SP codensate Bupro Bupro Khí thương phẩm ME-13 C-01 C-02 Sơ đồ công nghệ chế độ MF Ký hiệu: C - Tháp tách phân đoạn. V - Thiết bị tách. SC – Slug-Catcher. E - Thiết bị trao đổi nhiệt. K - Máy nén.
P - Bơm.
ME - Thiết bị đo điếm. F - Thiết bị lọc.
Dầu nóng Dầu nóng
TK-21
V-21A V-21B
Propan
Khí đồng hành
Butan
Sơ đồ công nghệ chế độ GPP chuyển đổi
SDV-101 SC-01/02 E-07 V-03 V-08 K-1011A/B/C/D E-1015A/B/C/D V-06A/B E-14 C-05 CC-01 C-01 E-01A/B V-15 ME E-04 E-09 Khí thương phẩm SP Condensate V-12 K-01 C-02 P-01A/B E-17 E-02 V-02 E-03 C-03 E-10 E-11 V-05 P-03A/B E-12 Ký hiệu: C - Tháp tách phân đoạn. V - Thiết bị tách. SC - Slug catcher.
E - Thiết bị trao đổi nhiệt. CC - Turbo Expander. K - Máy nén.
P - Bơm.
ME - Thiết bị đo điếm. V-21A
V-21B
E-10 Sơ đồ công nghệ chế độ GPP V-06 E-15 E-18 E-13 E-19 E-09 E-12 F-01 CC-01 E-02 E-11 E-01 E-03 E-04 V-07 K-04 K-01 K-02 K-03 C-05 C-04 C-01 C-02 C-03 ME-13 E-08 E-07 nước V-14 V-13 FV-1802 V-12 FV-1701 FV-1201 FV-1301 V-15 V-02 E-17 P-01 V-05 P-03 SP codensate SP Butan SP Propan C - Tháp tách phân đoạn. V - Thiết bị tách. SC - Slug catcher.
E - Thiết bị trao đổi nhiệt. CC - Turbo Expander. K - Máy nén. P - Bơm. ME - Thiết bị đo đếm. Khí thương phẩm ME-24 ME-26 ME-25 TK-21 V-21B V-21A
Zƒe"8おpj"8じ thＸt thốt exergy cてa hう thぐng
V pj"vqƒp"8瓜 th医t thốt exergy và hi羽u su医t exergy cho m瓜t s嘘 thi院t b鵜:
- Aぐi vずi máy nén
- Aぐi vずi bじ hịa trじn
TĨM T溢T D頴 LI烏W"A井U VÀO DÙNG TRONG MƠ PH碓NG
FLUID PACKAGE: Basis-1
Property Package Type: PengRob
Component List - 1: / Nitrogen / CO2 / Methane / Ethane / Propane / i-Butane / n-Butane /
i-Pentane / n-Pentane / n-Hexane / n-Heptane / n-Octane / n-Nonane / n-Decane /
Cyclopentane / Mcyclopentan / Cyclohexane / Mcyclohexane / Benzene / H2O / TEGlycol
FLOWSHEET: Main
FLUID PACKAGE: Basis-1
STREAM: 10 (Material Stream)
Temperature = 24.7758066 C Pressure = 107.98675 bar_g
Molar Flow = 8486.72588 kgmole/h
Composition Basis (In Mole Fractions): Nitrogen = 0.00191966468 / CO2 = 0.000650591397 / Methane = 0.685527176 / Ethane = 0.185523114 / Propane = 0.0746873667 / i-Butane = 0.0146279863 / n-Butane = 0.0202589931 / i-Pentane = 0.00480811249 / n-Pentane = 0.00533707745 / n-Hexane = 0.00307279286 / n-Heptane = 0.00126244602 / n-Octane = 0.000686033186 / n-Nonane = 0.000236085468 / n-Decane = 6.79946834e-005 / Cyclopentane = 0.000343507398 / Mcyclopentan = 0.000293908703 / Cyclohexane = 0.000227014173 / Mcyclohexane = 0.000243774944 / Benzene =
0.000226226493 / H2O = 9.13013094e-009 / TEGlycol = 1.24540053e-007 /
UNIT OPERATION: TEE-101 (Tee)
Feed Stream = 10 Product Stream = 11 Product Stream = 13
UNIT OPERATION: K-101 (Expander)
Feed Stream = 13 Product Stream = 14 Energy Stream = h5
AdiabaticEfficiency = 58.49
STREAM: 14 (Material Stream)
Pressure = 32.48675 bar_g
UNIT OPERATION: C-05t (Absorber)
UseAsEstimateStatus = False TargetType = 0
Phase = Liquid
Specification Name = 10 Rate SpecConvergedStatus = Inactive
Specification Value = 1992.76984 kgmole/h
Specification Name = Comp Fraction SpecConvergedStatus = Inactive Specification Value = 0.01
UNIT OPERATION: E-101 (Heat Exchanger)
TubeInletStream = 11 TubeOutletStream = 12
TypeOfHeatLeak = Extremes HCurveName = 11-12
PassInterval = 2
HCurveName = 15-Sale gas2 PassInterval = 2
RatingUA = 1766000 kJ/C-h
ShellPressureDrop = 0.206842773 bar
Specification Name = E-101 UA SpecifiedValue = 1766000 kJ/C-h SpecTypeSelection = UA
STREAM: 12 (Material Stream)
Temperature = -35 C Pressure = 107.98675 bar_g
UNIT OPERATION: VLV-101 (Valve)
Feed Stream = 12 Product Stream = 12v ActuatorLinearRate = 0.01
STREAM: 12v (Material Stream)
Pressure = 32.48675 bar_g
UNIT OPERATION: E-102 (Heater)
Feed Stream = 12v Product Stream = 12e Energy Stream = h12v
Pressure Drop = 0.206842773 bar ViewVapourPhase = False
ViewLightLiqPhase = False ViewHeavyLiqPhase = False ViewMixedLiqPhase = True
STREAM: 12e (Material Stream)
Temperature = -60 C
STREAM: h12v (Energy Stream)
Utility Type= MP Steam
STREAM: Sale gas2 (Material Stream)
Temperature = 11.5 C
UNIT OPERATION: VLV-103 (Valve)
Feed Stream = 17 Product Stream = 18 Pressure Drop = 5.5 bar ActuatorLinearRate = 0.01
FLOWSHEET: COL7 (Owned By: C-05t)
FLUID PACKAGE: Basis-1
UNIT OPERATION: TS-1 (Tray Section)
StgNumber = 4 StgNumber = 5 StgNumber = 6 StgNumber = 7 StgNumber = 8 StgNumber = 9 StgNumber = 10 StgNumber = 11
TĨM T溢T D頴 LI烏W"A井U VÀO DÙNG TRONG MƠ PH碓NG
This Input Summary is generated by HYSYS
Date: Mon Aug 26 13:42:26 UTC+0700 2013
FLUID PACKAGE: Basis-1
Property Package Type: PengRob
Component List - 1: / Nitrogen / CO2 / Methane / Ethane / Propane / i-Butane / n-Butane / i-
Pentane / n-Pentane / n-Hexane / n-Heptane / n-Octane / n-Nonane / n-Decane / Cyclopentane / Mcyclopentan / Cyclohexane / Mcyclohexane / Benzene / H2O / TEGlycol
FLOWSHEET: Main
FLUID PACKAGE: Basis-1
STREAM: feed (Material Stream)
Temperature = 25.6 C Pressure = 107.98675 bar_g
Molar Flow = 7578.96221 kgmole/h
Composition Basis (In Mole Fractions): Nitrogen = 0.00209980609 / CO2 = 0.00059994174 / Methane = 0.708502055 / Ethane = 0.134100389 / Propane = 0.0750002175 / i-Butane = 0.0165000479 / n-Butane = 0.0237000687 / i-Pentane = 0.00629941827 / n-Pentane = 0.00729932117 / n-Hexane = 0.00509951479 / n-Heptane = 0.00259970754 / n-Octane = 0.00179980522 / n-Nonane = 0.00079992232 / n-Decane = 0.00029997087 / Cyclopentane = 0.00049995145 / Mcyclopentan = 0.00049995145 / Cyclohexane = 0.00039996116 /
Mcyclohexane = 0.00049995145 / Benzene = 0.00039996116 / H2O = 0.0130000377 / TEGlycol = 0 /
UNIT OPERATION: SAPERATER (Separator)
Feed Stream = feed Vapour Product = gas Liquid Product = liquid
UNIT OPERATION: V-03 (3 Phase Separator)
Feed Stream = liquid-1 Vapour Product = gas-6 Liquid Product = 20 Heavy Product = water Energy Stream = heat-1 Volume = 10 m3 HeatExchanger = Duty
UNIT OPERATION: E-08 (Heat Exchanger)
TubeInletStream = 31 TubeOutletStream = 32 ShellInletStream = 20 ShellOutletStream = 21 TEMAType2 = F HCurveName = 31-32 HCurveName = 20-21 TubePressureDrop = 0 bar
UNIT OPERATION: C-01 (Reboiled Absorber)
8/26/2013 file://C:\Documents and Settings\lieupd\Local Settings\Temp\HYSBROW.htm
WithOilStreamBoolean = True TargetType = 0
Phase = Liquid
Specification Name = Bot Temp
SpecConvergedStatus = Inactive Specification Value = 109 C
Specification Name = Top Temp
SpecConvergedStatus = Inactive Specification Value = 60 C
Specification Name = Comp Fraction
SpecConvergedStatus = Yes Specification Value = 0.02
STREAM: 20 (Material Stream)
Temperature = 20 C
STREAM: 21 (Material Stream)
Temperature = 41 C Pressure = 73.98675 bar_g
UNIT OPERATION: VALVE-2 (Valve)
Feed Stream = liquid Product Stream = liquid-1 ValveOpening = 50 % ValveCurrent = 50 % ActuatorLinearRate = 0.01
STREAM: liquid-1 (Material Stream)
Pressure = 73.98675 bar_g
UNIT OPERATION: C-05 (Absorber)
WithOilStreamBoolean = True
STREAM: TEG_feed (Material Stream)
Temperature = 26 C
Pressure = 107.98675 bar_g Molar Flow = 40 kgmole/h
Composition Basis (In Mole Fractions): Nitrogen = 0 / CO2 = 0 / Methane = 0 / Ethane = 0 / Propane = 0 / i-Butane = 0 / n-Butane = 0 / i-Pentane = 0 / n-Pentane = 0 / n-Hexane = 0 / n- Heptane = 0 / n-Octane = 0 / n-Nonane = 0 / n-Decane = 0 / Cyclopentane = 0 / Mcyclopentan = 0 / Cyclohexane = 0 / Mcyclohexane = 0 / Benzene = 0 / H2O = 0 / TEGlycol = 1 /
UNIT OPERATION: E-14 (Heat Exchanger)
TubeInletStream = 2 TubeOutletStream = 3 ShellInletStream = 6
ShellOutletStream = Sale gas TEMAType2 = F
HCurveName = 2-3 HCurveName = 6-Sale gas ShellPressureDrop = 0 bar
UNIT OPERATION: TEE-100 (Tee)
Feed Stream = 1
8/26/2013 file://C:\Documents and Settings\lieupd\Local Settings\Temp\HYSBROW.htm
Product Stream = 2 Product Stream = 4
STREAM: 3 (Material Stream)
Temperature = -35 C
Pressure = 107.98675 bar_g
STREAM: 5 (Material Stream)
Pressure = 32.48675 bar_g
UNIT OPERATION: C-02 (Distillation)
TargetType = 0 Phase = Liquid Stage Pressure:
StageNumber = 1 / StagePressureValue = 9.98675 bar_g StageNumber = 32 / StagePressureValue = 10.03675 bar_g
Specs Summary:
SpecName= Temp top / SpecValue= 43 C
SpecName= Temp bottom / IsActive= True / SpecValue= 155 C SpecName= Butan bot / IsActive= True / SpecValue= 0.02
UNIT OPERATION: VLV-100 (Valve)
Feed Stream = 3