BALANCE DE MATERIA Capacidad de planta Dias habiles Produccion diaria Urea de 98% pureza
390000.00 300.00 1300.00 54166.6
Co!posicion del producto "inal Urea #iuret $u!edad
98.00% 1.00% 1.00%
Conersion &'&()
95.00% REACCIONES PRINCIPALES PRINCIPALES 1* CO_2+2NH_3 ↔ NH_2 COONH_4 +* NH_2 1* , +* COONH_4↔ NH_2 CONH_2+H_2 O
CO_2+2NH_3↔NH_2 CONH_2+H_2 O
REACTOR
34.00%
"lu-o (!oniaco reaccionado reaccionado (!oniaco producido producido (!oniaco sin reaccionar reaccionar C'+ sin reaccionar lu-o de carba!ato
ENTRADA Al!"#$&'!o$ /$3
1561+.45 30438.16 30438.16 89.40 15308.48 15308.48 +03.19 69006.46
Flujo (kg/hr 30348.6
C'+ /$3 de reciclo Carba!ato de reciclo TOTAL DE ENTRADA SALIDA Pro-u'o Urea (ua #iuret
41463.5 15308.48 69006.46 )*+,.4) Flujo (kg/hr 53083.33 16114.3+ 16114.3+ 541.6
Carba!ato S!$ r#&''!o$&r C'+ /$3 TOTAL DE SALIDA
69006.46 +03.19 15308.48 )*+,.4)
DESCOMPONEDORES ENTRADA Urea aua biuret C'+ /$3
Flujo (kg/hr 53083.33 16114.3+ 541.6 +03.19 15308.48 ,+0.
SALIDA #''!o$ 1&j& Urea aua biuret
53083.33 16114.3+ 541.6 *,3.3+
To2# C'+ /$3
+03.19 15308.48 ,3.*,
Carba!ato S!$ r#&''!o$&r C'+ /$3 TOTAL DE SALIDA
69006.46 +03.19 15308.48 )*+,.4)
DESCOMPONEDORES ENTRADA Urea aua biuret C'+ /$3
Flujo (kg/hr 53083.33 16114.3+ 541.6 +03.19 15308.48 ,+0.
SALIDA #''!o$ 1&j& Urea aua biuret
53083.33 16114.3+ 541.6 *,3.3+
To2# C'+ /$3
+03.19 15308.48 ,3.*,
/$3 /$3 de reciclo Carba!ato de reciclo
tonano dia tondia 2hr
53083.333333 53083.3333333333 3333 2hr 541.666666666 541.666666666 2hr 541.666666666 541.666666666 2hr
REACCION SECNDARIA 3*
〖 2NH 〗 _2 CONH_2→ NH_2 CONHCONH_2+NH_3 CONHCONH_2+NH_3
REA 2hr 2hr 2hr 2hr 2hr 2hr
Por'#$&j#
lujo (k"ol/hr 19.44%
185.++
+6.56% 9.81% 44.+0% 00.00%
94+.36 900.50 884.0 4)+.,
34.00% 10.3+% 0.35%
884.+ 895.+4 5.+6
Por'#$&j#
44.+0%
884.0
1.33% 9.81% 00.00%
4.1+ 900.50 3*,.)4
60.93% 18.50%
884.+ 895.+4
0.6+% +.38% 1.5%
5.+6 4.1+ 900.50
00.00%
+,3+.4
6.1+% +3.11% 0.8%
884.+ 895.+4 5.+6
00.00%
,).++
11.93% 88.0%
4.1+ 900.50
00.00%
4,.*+
Por'#$&j#
P#o "ol#'ul&r# C'+ /$3 /$+C''/$4 /$+C'/$+ $+' /$+C'/$C'/$+
44 1 8 60 18 103
r#l&'!o$ "ol&r -# #$r&-& &l r#&'or N Urea conertida en biuret Urea producida (!oniaco reaccionado C'+ reaccionado (!oniaco utilizado C'+ utilizado (ua producida
2or'#$&j# 39.56% +0.88% 19.95% 19.60% 00.00%
+4.46% +4.5% 0.15%
+4.46% 1.30% +4.89% 00.00%
3+.3% 3+.6% 0.19% 1.+% 3+.95% 00.00%
49.56% 50.15% 0.+9% 00.00% 4.9% 95.03% 00.00%
+059.805501618 1039.03+168+85 10+0.805643644 4.,340**4*
50.00% +5.++% +4.8% 00.00%
53/CO+
3 631.0 2hr 5314.40 2hr 30438.16 2hr 39390.56 2hr 4565.+4 2hr 41463.5 2hr 16114.3+ 2hr
STRIPPER ENTRADA
Flujo (kg/hr
Pro-u'o -#l r#&'or Urea (ua #iuret Carba!ato S!$ r#&''!o$&r C'+ /$3 TOTAL DE ENTRADA
SALIDA S#''!o$ 1&j& Urea aua biuret C'+ /$3
o2#
53083.33 16114.3+ 541.6 69006.46 +03.19 15308.48 )*+,.4) Flujo (kg/hr 53083.33 16114.3+ 541.6 +03.19 15308.48 ,+0.
C&r1&"&o
*00*.4*
E6APORADOR AL 6ACIO Flujo (kg/hr
ENTRADA Urea (ua #iuret
53083.33 16114.3+ 541.6 *,3.3+
SALIDA To2# Agu&
)),+.*)
S#''!o$ 1&j& urea aua biuret
98% 53083.33 541.6 541.6 )4**.*********,
155+.65 aua 1 eaporador 10958.464+3948+ 608.804+4549
Por'#$&j#
lujo(k"ol/hr 34.00% 10.3+% 0.35% 44.+0% 0.00% 1.33% 9.81% 00.00%
Por'#$&j#
884.+++++++++ 895.+400+155 5.+58899664 884.698++4518 4.118958+4 900.4989+1+513 3*,.)3*)) lujo(k"ol/hr
60.93% 18.50% 0.6+%
884.+++++++++ 895.+400+155 5.+58899664
+.38% 1.5% 00.00%
4.118958+4 900.4989+1+513 +,3+.3,*0),3
00.00%
4.*++4),
6.1+% +3.11% 0.8%
884.+++++++++ 895.+400+155 5.+58899664
00.00%
,).++434,3*
00%
*).4,4++4
98.00% 1.00% 1.00%
884.+++++++++ 30.09+59+59+6 5.+58899664
00.00%
+0.0,3,44+
Por'#$&j#
aua + eaporador 4614.18 +56.343183+05
2or'#$&j# +4.46% +4.5% 0.15% +4.46% 1.30% +4.89% 00.00% 2or'#$&j# 3+.3% 3+.6% 0.19% 1.+% 3+.95% 00.00%
00%
49.56% 50.15% 0.+9% 00.00%
00%
96.16% 3.+% 0.5% 00.00%
BALANCE DE ENER7IA '2('&l/g" °C 0.48+8 0.54 0.++5 0.6+ 1
E2#'!# ur#& N53 CO+ C&r1&"&o &gu& 1!ur#
INTERCAMBIADOR DE CALOR ANTES DE ENTRAR Calenta!iento de C'+ /$3 de la ali!entacion ntrada !olh C'+ 94+.36 /$3 185.++ ++.58 Cp pro! '&lor &'u"ul&-o !7
39.41+19401 .)0E80, !
.10:03
INTERCAMBIADOR DE CALOR ANTES DE ENTRAR Calor
84330+96.515+
;apor utilizado
396.186888+ ++09.+8816046
Calor de salida
.+3:0
CONDENSADOR DE CARBAMATO
Carba!ato aseoso
$+' de re"rieracion utilizada
DESCOMPONEDOR A PRESION MEDIA A 4 C()'< D /&<(D( =alida /$3 C'+ Urea >ater #iuret tope /$3 C'+
!asa !olar 450.+494606+6 +3.55894936+ 884.+ 895.+4 5.+6 ++).0+))+04 450.+494606+6 +3.55894936+ 4,3.040)*+
Cp pro! salida Calor de salida
85.46643+56+ +.1:0
cp pro! tope λ pro! tope Calor de &ope
38.5++0448953 +.46:04 1.4+:0
Usando aua de re"rieracion a +0C sale a 40 Calor anado por el aua ?+.14:06 !asa de aua +5599.+6+1
#r E6APORADOR ) C ntrada Urea >ater #iuret C&lor -# #$r&-& =alida de aua Cp pro! !ezcla C&lor &l!"#$&-o $ap a 0.+5 at! $ap a 4.5 at!
884.+ 895.+4 5.+6 ,).++ .40E80, 608.63+1461 98.+80335161 .4E80, 4115 38+1.6
C&lor 2or &gu& 9&2or!:&-& C&lor -#l 9&2or &ur&-o
+.,E80, +.*E80,
;apor sat a 4.5 at!
.3:0+
Cp pro! salida C&lor -# &l!-&
110.+0+65566 .0E80,
E$r!&-or &$# -# #$r&r &l #gu$-o #9&2or&-or E$r&-& lu-o Calor
) 116.459+88 1.10:0
S&l!-& Calor
+, 3.50:06
Calor @ue se necesita retirar
.5+:06
Agu& -# #$r!&"!#$o (+0;40 C
).00E803
L!& -# E
=alida
I$#r'&"1!&-or -# '&lor
STRIPPER
ntrada =alida
Co$-#$&-or -# '&r1&"&o
D#'o"2o$#-or & 2r#!o$ "#-!&
D#'o"2o$#-or & 1&j& 2r#!=$
E9&2or&-or &l 9&'>o 0.+3 &"
ntrada =alida
ntrada =alida
ntrada =alida
E9&2or&-or &l 9&'>o 0.03 &"
Torr# -# gr&$ul&'!=$
ntrada =alida
'2(@j/@"ol °C
?(@j/@g 1+1.09 38.3 41.38 +0+.14 5.+4 183.80
1300 1666.666666666 +10 +1+0.6
L REACTOR DE 40 A 0
%!olar 34.55% 65.45% 100.00%
u!l!:&r 9&2or -# &gu& & ).4 &" 'o$ T 2h
L STRIPPER DE 0 A ) 2-h 2h 2!olh
+00
$+' a +5 C ;apor saturado a 100
Carba!ato li@uido
carba!atoanadopor$+' !carba!ato λc !auaACp ∆T+λa) !asa de aua
13341.59 9630.0883+90809
C 3.9+:0 porcenta-e !olar 19.93% 1.04% 39.16% 39.63% 0.+3% 00.00% 95.03% 4.9%
2-2!olC
2hr
49.56% 50.15% 0.+9% 00.00% k/h 2!olh -!olBC k/h 2!ol 2!ol k/h k/h !olh -!olBC k/h
C 2!olh 2h C 2h 2h k"ol/h
Corr!#$# 1 ? C'+ 19 ? /$3 6&2or S&ur&-o & +00 C ).4 &" 1 ?C'+ 1+ ? Carba!ato /$ 3 /$3 + ? Urea (ua #iuret Carba!ato C' + /$3 Agu& -# #$r!&"!#$o + ? Urea (ua #iuret Carba!ato C' + /$3 6&2or S&ur&-o & +00 C ).4 &" + ? Urea (ua #iuret Carba!ato C' + /$3 3 ? Urea (ua #iuret C'+ /$3 13 ? Carba!ato 6&2or S&ur&-o & +00 C ).4 &" 13 ? Carba!ato Agu& -# #$r!&"!#$o 3 ? /$3 C'+ urea aua biuret 14 ? /$3 C'+ 4 ? /$3 C'+ urea aua biuret Agu& -# #$r!&"!#$o 4 ? /$3 C'+ urea aua biuret 5 ? Urea (ua #iuret 15 ? /$3 C'+ Agu& -# #$r!&"!#$o 6 ? Urea aua biuret ? Urea aua biuret 1 ? (ua Aapor* 6&2or &ur&-o & 4.) &" 8 ? Urea aua biuret
Flujo (k"ol/h 94+.36 185.++ ,0,.04 94+.36 350.4+ 361.54 34. 361.54 0*3. 361.54 +3+.84 884.0 *33.* 884.0 *30.0 +3+.84 43.81 ++59.03 4++.+ ++59.03 185.++ 43.81 3,.* 185.++ 116.46 608.6 ,,3.44 116.46
Agu& -# #$r!&"!#$o 8 ? Urea aua biuret 9 ? Urea aua biuret 18 ? (ua Aapor* 6&2or &ur&-o & 4.) &" 1011 ? Urea aua biuret Corriente de aire
4,.0 116.46 9+0.15 +56.31 30,.+0 9+0.15 5+8.86
E$&l2!& -# r#&''!o$ -# l& ur#& 2calr!ol
22!ol ?31.3+
?13091.6
REACTOR
0
E$r&-& /$3 C'+ Carba!ato /$3 de reciclo
te!peratura
S&l!-& Urea (ua #iuret Carba!ato C'+ /$3
te!peratura
cp pro!
180 180 180 180
180 180 180 180 180 180
108.0+5069959
STRIPPER S&l!-& Urea (ua #iuret C'+ /$3 cp pro!
) porcenta-e !olar 3+.3% 3+.6% 0.19% 1.+% 3+.95% .55903311+
2hr
DESCOMPONEDOR A PRESION BAA A 0 C Calor de entrada =alida Urea >ater #iuret &ope /$3 C'+
+.1:0 !asa !olarA!olhr* 884.+ 895.+4 5.+6 ,).++ 450.+494606+5 +3.55894936+ 4,3.040)*
Cp pro! salida Calor de salida
98.+8 1.40:0
Cp pro! &ope λ pro! tope Calor de tope
38.5+ +.46:04 1.31:0
Calor total Usando aua de re"rieracion a +0 C sale a 40 !asa de aua
?5.59:04 668.865960838 3.159++08935
+-o E6APORADOR +, C ntrada Urea (ua #iuret C&lor -# #$r&-& =alida de aua Cp pro! !ezcla C&lor &l!"#$&-o $ap a 0.03 at! $ap a 4.5 at!
884.+ +86.48 5.+6 ,*.4),+0+* 3.)0E80* +56.30+18169 110.+0+65566+ 3.50:06 45806.4 38+1.6
C&lor 2or &gu& 9&2or!:&-& C&lor -#l 9&2or &ur&-o
.,E80, .,E80,
;apor sat a 4.5 at!
3.0:0+
Cp pro! salida C&lor -# &l!-&
119.94 +.E80*
PRILLIN7 E$r&-& lu-o Calor
+, 9+0.150106+5 +.98:06
S&l!-& Calor
+) +.6:06
Calor @ue se retira
+.+1:05
A!r# (+);+* C
,.)3E803
Cp del aire Easa !olecular del aire
1.01+ +8.9
T#"2#r&ur& C° E$r&-&
C&lor k/h
S&l!-& 40 40 +00 180 180 ? +0 180 +00 185 ?
+00 185 +0 185
+0 140
+0 80
4, 85
180 180 +00 180 180 180 40 185 +00 185 185 +00 185 40 140 140 40 80 80 40 85 85 4, +
5.46:06 9.59:06 ;.)0E80, .0+:06 0.00:00 .03:0 ).+)E80, 1.95:06 ;+.+)E80* .+3:0 3.9+:0 4.6:0 ;.4)E80, ?1.45:0 .4)E80, 3.9+:0 1.4+:0 +.1:0 +.4E80* +.1:0 1.40:0 1.31:0 ).)E804 1.40:0 1.10:0 3.+6:0 +.*E80, ?.5+:06
+0 +
4, + +5
40 + + 4, +5 +6
,.)+E80* 3.50:06 +.98:06 1.+3:0 .,E80, ?+.+1:05 +.+1:05
C '&lor -# r#&''!o$
calor A2-hr* 1+33059.5 01939.96 3+190686.++ 6+194.8 ).,E80,
C&lor o&l #$ r#&'or
porcenta-e !olar
&gu& -# r#r!g#r&'!o$ & +) !cpF& reaccion !
+4.46% +4.5% 0.15% +4.46% 1.30% +4.89% 100.00% C&lor -# S&l!-&
∆5r
,.03E80, kj/hr
C '&lor '&r1&"&o !cpF&:!7 acu!ulad 4.6:0 calor total en =tripper '&lor u"!$!r&-o 2or 9&
!7total ! apor C&lor -# &l!-&
3.+E80,
porcenta-e !olar 49.56% 50.15% 0.+9% 00% 95.03% 4.9%
2-2!olC -h
2hr
5.+0% +4.35% 0.45% 00.00% k/h 2!olh -!olBC 2h 22!ol 2!ol k/h k/h !olh -!olBC k/h
C 2!olh 2h C 2h 2h k"ol/h
=alida Urea (ua #iuret
22BC 22!ol
+9.3164 22!olBC
C&lor -# R
C&lor l&#$# λ (kJ/kg)
C2 (@j/@"olC 41.38 38.3
? ++0.*
41.38 0.00 108.03 ,).+4 108.03
?1.16:08
++0.*
+10 ++0.* +10
+464.45
+464.45
4115 3+,.*
108.03 .56 +0+.14
,).+4 .56 38.5+ 85.5 ,).+4 85.5 98.+8 38.5+ ,).+4 98.+8 110.+0 5.+4 110.+0
45806.4 3+,.*
,).+4 110.+0 119.94 5.+4 119.94 +9.3+
?1.16:08 2hr
;.03E80 k/h
C h&& 40 68609.34 2!olh 3811.63 2h
o 1.45:0 or -# &gu& & ).4 &" 'o$ T 6.83:03 2h
+00
884.+++++++++ 30.169588+1 5.+58899664 +0.)0,0*+),
96.15% 3.+8% 0.5%
C