ISRN Thermodynamics

Volume 2013 (2013), Article ID 253437, 4 pages

http://dx.doi.org/10.1155/2013/253437

Research Article

A New Cryogenic Air Separation Process with Flash Separator

Zeinab A. M. Khalel, Ali A. Rabah, and Taj Alasfia M. Barakat

Department of Chemical Engineering, Faculty of Engineering, University of Khartoum, P.O. Box 321, Khartoum 11111, Sudan

Received 15 May 2013; Accepted 13 June 2013

Academic Editors: R. R. Burnette, T. Chen, P. Espeau, and P. Trens

Copyright © 2013 Zeinab A. M. Khalel et al. This is an open access article distributed under the Creative Commons Attribution License, which permits unrestricted use, distribution, and reproduction in any medium, provided the original work is properly cited.

Abstract.

A new cryogenic air separation process with flash separator is developed. A flash separator is added to the conventional double-column cryogenic air separation process. The flash separator is used to replace the turbine required to recover a portion of the energy in the double-column air separation process. The flash separator served dual purposes of throttling and separation. Both the conventional and the new processes are simulated using Aspen Plus version 11.1 the model air flow rate and compositions are taken as 50000 Nm³/h of air at standard conditions of 1 atm and 25°C and feed composition of 79.1% N₂ and 20.9% O₂. The new process decreases the energy consumption and increases the productivity.

1. Introduction

There are mainly three methods of air separation, cryogenic distillation, pressure swing absorption, and membrane separation. Although the latter two methods have become more competitive, cryogenic distillation remained the dominant choice for mass production of high-purity O₂. The first cryogenic distillation unit with single-column was built in 1902 and shortly followed by double-column process. The double column consists of compressors, low- and high-pressure columns, and two sets of heat exchangers. The low- and high-pressure columns are thermally interconnected [1].

Although the double-column process is widely used, its high energy consumption remains challenging. Therefore in the recent past, the double column has been subjected to many energy-efficient modifications such as changing the operation condition of the low-pressure column from low to moderate pressure [2]. This modification resulted in smaller size of the column and 10% energy savings. The modification has also the advantage of argon recovery (up to 5% greater argon recovery over the conventional). Another modification is the addition of a heat pump to a side rectifier which is thermally linked to the two columns. The heat pump enhances the separation by providing a supplementary crude argon condensing duty [3]. Reference [4] did an exergy analysis of the double-column air separation process. It found that more than half of the exergy loss takes place in the liquefaction unit and almost one-third in the air compression unit, and minor exergy losses are taking place in the distillation unit and the main heat exchangers. Reference [5] has changed the design of the double column to single column using self-heat recuperation technology (i.e., heat from the top vapor stream is recuperated and exchanged with heat in the bottom liquid and feed streams). The author’s modifications have improved the energy consumption by around 36% of the conventional process.

This work is aimed to develop an energy-efficient air separation process. Flash separator has the advantage of working as throttling device on one hand and vapor liquid separation unit on the other hand. It is introduced into the conventional double-column air separation process to replace the turbine needed to expand the air prior to injection to lower-pressure distillation column.

2. Process Description

Figure 1 shows schematic presentation of the conventional double-column cryogenic air separation process. It consists of two compressors (C1 and C2), a turbine (T), two thermally linked distillation columns (low-pressure column (LPC) and high-pressure column (HPC)), and two sets of heat exchangers (HX1, HX2). The air is compressed from atmospheric pressure to 6 atm in C1. The compressed air is then split into two streams; one stream for HPC (hereafter is called HPC split) and the other stream for LPC (hereafter is called LPC split). The LPC split is compressed in C2 further to 7.5 atm, cooled in HX1, throttled in T to 1.3 atm, and finally fed to LPC. The HPC split is cooled in HX1 and then fed to HPC. The products of LPC are pure N₂ (top), pure O₂ (bottom), and waste N₂ (side stream). The products of HPC are pure N₂ (top) and air-enriched oxygen (bottom). The pure N₂ of HPC is working as reflux to the LPC and the air-enriched oxygen of HPC is an extra feed to the LPC. The two columns are thus thermally linked by exchanging the latent heat of vaporization via condenser of the HPC and reboiler of the LPC. The products of the LPC are liquid pure oxygen from the bottom, gas pure nitrogen from the top, and side product of waste nitrogen; all these products are heated in the two sets of heat exchangers prior to be sent as final products.

Figure 1: Conventional double-column cryogenic air separation process.

Figure 2 shows schematic presentation of the new cryogenic air separation process with flash separator. The air is compressed in C3 from atmospheric pressure to 4 atm instead of 6 atm as in the conventional process then split into two streams. The HPC split is compressed in C4 further to 6 atm and subsequently cooled in HX1 and then injected to HPC. Hence this stream is maintained at the same conditions as these in the conventional process. The LPC split is cooled in HX1 and then throttled in a flash separator (F) to 1.3 atm. The bottom product of the flash separator is air-enriched O₂ and the top product is a waste N₂. The waste N₂ is a final product (mixed with the waste nitrogen from the LPC). The bottom product of the flash (air-riched O₂) is fed to the LPC. The rest of the process remains the same as in the conventional process.

Figure 2: New cryogenic air separation process with flash separator.

Clearly the flash separator replaces the turbine of the conventional double column. Although the turbine is used to recover part of the work introduced into the compressors, the other point to be noticed in this new design is that the LPC split is compressed to 4 atm only rather than 7.5 atm as in the conventional process.

3. Simulation

Both the conventional and the new cryogenic air separation processes are simulated using Aspen Plus version 11.1 with the Peng-Robinson equation of state as a fluid package [6].

The following assumptions are considered in this work.

(1)The model air is assumed to gain 5 K in the processes of drying and cleaning prior to the inlet of the main compressor. (2)The pressure drop across the heat exchangers is taken as 0.1 atm. (3)The pressure drop along the HPC and the LPC is 0.1 atm. (4)The minimum temperature approach is 1.5 K for the HX1 and 2.5 K for HX2.(5)5 kW is lost during the thermal integration between the two columns.

The model air flow rate and composition are shown in Table 1.

Table 1: Model air specification.

Parameter
Value
Unit

Flow rate
50000
Nm³/h

Pressure
1
atm

Temperature
298
°K

N₂
79.1
Mole %

O₂
20.9
Mole %

The compressors C1, C3, and C4 are simulated as multistage compressors (two stages), while C2 is simulated as single stage because the pressure difference is only 1.5 atm. The cooling duty for multistage compressor is neglected as cooling water is assumed to be taken from large reservoir like the electrical energy consumed in pumps. The pumps are considered as auxiliary devices and common in both conventional and new processes. The distillation columns in both processes are simulated by a block known as RadFrac. The two sets of heat exchangers (HX1, HX2) are simulated by block called MHeatX.

4. Results and Discussion

The core of any cryogenic air separation process is distillation unit; here and as mentioned before the HPC split specification remains the same in the conventional and new processes, so the value of the condenser duty of the HPC from the first run is input as the value of the reboiler duty of the LPC. These values are shown in Table 2. Also the number of stages of the HPC and the LPC is adjusted using the composition profile; the number of stages is taken when there is no much difference in the product purities with the increased number of states; the number of stages is given in Table 2.

Table 2: Design and operating conditions of distillation columns.

Parameter
Column

LPC
HPC

No. of stages
20
15

Reboiler duty
2141 kW
—

Condenser duty
—
2146 kW

Table 3 shows the simulation result of products flow rates and composition. It can be seen that there is no significant difference in the product purity of both process, but in the new process there is an increase in the flow rate of oxygen by 14.3% and nitrogen by 5.4%, while the flow rate of the waste nitrogen (undesirable product) decreased by 5.5%.

Table 3: Specification of product streams.

Product

Conventional process
New process

Flow rate
O₂
N₂
Flow rate
O₂
N₂

O₂ (g)
8038
99.99
0.01
9189
99.98
0.02

N₂ (g)

10602
0.13
99.87
11178
0.13
99.87

Waste N₂ (g)
31360
7.65
92.35
29633
4.21
95.79

The flow rate in Nm³/h and composition in mole %

This is attributed to the change in LPC feed. In the new process the feed to LPC is reduced by the early separation of the waste N₂ in the flash separator. Hence the feed is less in quantity and enrich in O₂ than that in the conventional process. This change in the feed quantity and composition is expected to have either influence on the LPC unit specification or the quality of the product. Since the LPC column specifications are maintained similar to those in the conventional process, the feed change is reflected in the products quantity.

Also it is important to mention that in the conventional process the outlet pressure of C2 controlled the pressure drop across the turbine and then the temperature drop across it, and it also affects the amount of recovered energy; on the other hand the outlet pressure of C3 in the new process manipulates the liquid fraction of air to the flash separator and, subsequently, the quantity and composition of the LPC feed from the bottom of the flash separator “the air-enriched oxygen”, which is directly reflected on the oxygen flow rate and purity. The effect of the outlet pressure of C3 on product oxygen purity and flow rate is shown in Figures 3 and 4, respectively.

Figure 3: The outlet pressure of C3 versus product oxygen purity.

Figure 4: The outlet pressure of C3 versus product oxygen flow rate.

The main consumption of energy in both processes is in the compressors, while other utilities energy consumption like pumps is excluded, because it is almost the same in the new and the conventional processes.

The summary of the energy consumption in the two processes is shown in Table 4. It can be seen that portion of the energy consumed in C1 and C2 of the conventional process is recovered by the turbine; however still the net energy consumption of the new process is lower due to the decrease in the compression duty.

Table 4: Specification of energy consumption units.

Block
Conventional process
New process

Pressure (atm)
Work (kW)
Pressure (atm)
Work (kW)

In
Out
In
Out

C1
1
6
4390
—
—
—

C2
6
7.5
79
—
—
—

C3
—
—
—
1
4
3296

C4
—
—
—
4
6
748

Turbine/flash
7.4
1.3
−81
3.9
1.3
—

Net energy consumption

4388 kW

4044 kW

Specific energy consumption

0.55 kWh/Nm³ O₂

0.44 kWh/Nm³ O₂

For comparison between two processes, the specific energy consumption (SEC) may be a more meaningful measure than the net energy consumption. The SEC is defined as the net energy consumption per Nm³/h of the product, that is, Nm³/h of O₂. Hence SEC for the conventional process and new process is 0.55 kW·h/Nm³ O₂ and 0.44 kW·h/Nm³ O₂, respectively, as shown in Table 4. This is equivalent to an enhancement in SEC by about 20%; this decrease is because the new process produces more oxygen and consumes less energy than the conventional process.

5. Conclusion

A new cryogenic air separation process with flash separator is developed and simulated using Aspen Plus software. In the new process the turbine of conventional double column process is replaced by a flash separator. From thermodynamic point of view the new design is better than the conventional design in two aspects: (1) the SEC is lower than that of the conventional by 20% and (2) the pure O₂ produced is increased by 14.3% and pure N₂ is increased by 5.4%. On the other hand flash separator is more reliable than the turbine as it contains no moving parts.

References

F. G. Kerry, Industrial Gas Handbook: Gas Separation and Purification, CRC & Taylor & Francis, New York, NY, USA, 2006.

H. Cheung, “Moderate-pressure cryogenic air separation process,” Gas Separation and Purification, vol. 5, no. 1, pp. 25–28, 1991.

R. Agrawal, D. W. Woodward, and T. F. Yee, “Argon production from air distillation: use of a heat pump in a ternary distillation with a side rectifier,” Gas Separation and Purification, vol. 8, no. 1, pp. 37–43, 1994.

R. L. Cornelissen and G. G. Hirs, “Exergy analysis of cryogenic air separation,” Energy Conversion and Management, vol. 39, no. 16–18, pp. 1821–1826, 1998.

Y. Kansha, A. Kishimoto, T. Nakagawa, and A. Tsutsumi, “A novel cryogenic air separation process based on self-heat recuperation,” Separation and Purification Technology, vol. 77, no. 3, pp. 389–396, 2011.

Aspen Technology, Aspen Plus User Guide, Aspen Technology, Cambridge, Mass, USA, 2000.