填料塔设计



填料塔设计

设计：

塔编号

:

校核：

项目编号

:

日期：

客户

:

工程项目

:

#

参数输入

介质

:

HCL Vap.

填料类型Packing type

=

Intallox Saddles

填料尺寸Packing size

=

25

mm

填料材质Packing MOC

=

304

压损Gas pr. Drop / m bed

=

15

mmWC / m packing height

=

147.1

(Pa)/m

填料总高Total packing height

=

3.2

m (including all packed beds)

流体参数

气相质量流率

=

0

kg/h

OR

3000

m3/h

=

0.0000

kg/s

=

0.833333

m3/s

气相进口压力

=

1.0000

atm

气相进口温度

=

30.00

oC

=

303.00

oK

气相摩尔质量

=

29

清洗组分

组分名字

=

甲醇 Vap

组分质量流率

=

9

Kg/h

气相体积浓度％

=

0.2

% (v/v)

(presumed) / (given by client) / (by process cal.)

组分摩尔质量

=

34

吸收液参数

吸收液

=

H2O

液相流率, L

=

6000

kg/h

=

1.6667

kg/s

=

1000

kg/m3

Conversion :

粘度, µL

=

0.0035000

Ns/m2

3.5

Cp          =

0.00350000

Ns/m2

填料F因子, Fp

=

21

m-1

干填料因子r,Cf

=

52

Ref. Table 6.3, Characterstics of Random packings

转换系数, J

=

1.0

factor for adequate liquid distribution & irrigation across the bed

计算

塔径计算

塔底为大流量喷淋，因此塔径由塔釜条件计算。

气体密度计算

摩尔质量

=

29.45

Kg / Kmol

给定质量流率 kg/h

给定体积流率m3/h

Gas in   =

0

Kmol/s

Gas in

= (m3/s) x     273

x

pr. in atm

x    1

T in kelvin

1.0 atm

22.4

=

(kmol/s) x T in kelvin x  1.0 atm  x 22.4

273          pr. In atm      1

=

0.033519

Kmol/s

=

0.000000

m3/s

=

0.987134

Kg/s

由上述条件选择流率

质量流率

=

0.9871339

Kg/s

体积流率

=

0.8333333

m3/s

摩尔流率

=

0.033519

Kmol/s

气相密度

=

1.1846

Kg/m3

(mass flow rate / vol. Flow rate)

To find L', G' and Tower c/s area

Assuming essentially complete absorbtion,

脱除组分质量流率

=

0.0023

Kg/s

(摩尔流率 x 组分浓度 x 组分摩尔质量)

液相质量流率L‘

=

1.6689

Kg/s

(输入液相流率+脱除组分流率)

0.5

=

0.05819

以

0.05819

为纵坐标

查询 fig.6.34  压损（Gas pr. Drop ）为

147.1

(N/m2)/m

=

0.04

(查表)

气相质量流速 G'

=

0.5

Cf  µL0.1 J

=

1.2657

Kg / m2.s

塔截面积c/s area

=

0.7799

m2

( c/s area =质量流率 / G' )

塔径

=

0.9965

m

=

996.5

mm

圆整

=

500

mm

校核塔截面积c/s area

=

0.1963

m2

估算功率需求

风机效率

=

60

%

assumed / given

压降计算

淹塔压降

=

470.72

N/m2

(pressure drop per m packing  x total ht. of packing)

干填料压降

惰性气体质量流率

=

5.0158

Kg / m2.s

(Gas inlet flow rate - Component removed) / c/s area

惰性气体压力

=

100854.28

N/m2

(subtracting pressure drop across packing)

气体密度

=

gas o/l pr.

=

1.1605

Kg/m3

CD

=

96.7

Ref. Table 6.3, Characterstics of Random packings

=

Z

=

2096.42

N/m2

填料压降

=

2567.14

N/m2

(irrigated packing + dry packing)

内构件压力

=

25

mmWC

(packing supports and liquid distributors)

=

245.17

N/m2

气体流速

=

7.5

m/s

进出口局部损失

=

1.5 x Velocity heads

=

1.5 x (V2 / 2g)

=

42.19

N m / Kg

=

49.97

N/m2

(divide by density)

总压降

=

2862.28

N/m2

(packing + internals + losses)

风机输出功率

=

O/L gas density, Kg/m3

=

2429.14

N .m / s

=

2.43

kW

电动机功率

=

4.05

kW

(fan power output / motor efficiency)

=

5.43

hp

塔径/水力校核

两相流动参数, FLV

=

(L / V) x   (    V /     L)

=

0.0581

压损初值

15

mm H2O /m packing

雾沫夹带分率K4 v/s FLV,

K4

=

0.85

泛点雾沫夹带分率K4

=

6.50

Trial % 泛点百分率

=

(     (K4 / K4 at flooding)     )   x 100

=

36.1620

气相质量流速, Vm

=

=

3.5833

kg/m2.s

校核塔截面积 c/s area

=

V / Vm

(Trial As)

=

0.2755

m2

校核塔径., D

=

0.5922

m

D =

圆整至标准直径

D

=

0.500

m

塔截面积C/S area, As

=

0.1963

m2

As =

(pi/4) x D2

%泛点百分率

=

50.7361

% flooding = Trial % flooding x (Trial As / As)

结论

填料塔泛点百分率范围为 50% -- 85%.

如果要降低泛点百分率,

(i) 选择大尺寸的填料重复上面步骤.

(ii)增加塔径，重复上面步骤.

HETP 预算

诺顿关联式：

ln HETP  =  n - 0.187 ln      +  0.213 ln  µ

适用于，液相表面张力>4,<36dyne/cm

液相粘度，>0.08,<0.83cp

Conversion :

参数输入

0.018

N/m    =

18

dyne/cm

液相

表面张力

=

20

dyne/cm

Norton's Correlation Applicable

粘度

μ

=

3.5

cP

Norton's Correlation NOT applicable

n

=

1.13080

计算

Ln（HETP）

=

0.8374366

HETP

=

2.3104368

ft

=

0.7042211

m

低于15快理论板数的分离器，取20％的设计安全系数。

考虑20％安全系数校核

HETP

=

0.8450653

m

15～25理论板数的分离器，取15％的设计安全系数。

考虑15％安全系数校核

HETP

=

0.8098543

m