Removal of Dissolved Oxygen from Water by Nitrogen Stripping Coupled with Vacuum Degassing in a Rotor–Stator Reactor

Abstract

Oxygen is a harmful substance in many processes because it can bring out corrosion and oxidation of food. This study aimed to enhance the removal of dissolved oxygen (DO) from water by employing a novel rotor–stator reactor (RSR). The effectiveness of the nitrogen stripping coupled with vacuum degassing technique for the removal of DO from water in the RSR was investigated. The deoxygenation efficiency (η) and the mass transfer coefficient (K_La) were determined under various operating conditions for the rotational speed, liquid volumetric flow rate, gas volumetric flow rate, and vacuum degree. The nitrogen stripping coupled with vacuum degassing technique achieved values for η and K_La of 97.34% and 0.0882 s⁻¹, respectively, which are much higher than those achieved with the vacuum degassing technique alone (η = 89.95% and K_La = 0.0585 s⁻¹). A correlation to predict the K_La was established and the predicted K_La values were in agreement with the experimental values, with deviations generally within 20%. The results indicate that RSR is a promising deaerator thanks to its intensification of gas–liquid contact.

1. Introduction

Oxygen plays a key role in the treatment of wastewater [1,2]. Nevertheless, oxygen is a harmful substance and removal of dissolved oxygen (DO) from water is an essential step carried out in power plants in order to prevent corrosion in boilers and pipes, improve heat transfer and enhance plant efficiency [3,4,5]. This operation is not only adopted in the power industry but is also necessary in the semiconductor, pharmaceutical, biotechnology and food industries, which also have stringent requirements for DO levels in water [6,7]. It is thus indispensable to remove DO from water prior to its use in many industries.

Various physical techniques, such as thermal degassing, vacuum degassing and nitrogen stripping, are currently employed by industries to remove DO from water. It has been reported that nitrogen stripping is the most effective approach for DO removal among these techniques [8]. Coupled techniques, such as thermal degassing with vacuum degassing or thermal degassing with nitrogen stripping, are also promising means for DO removal [8,9]. However, these techniques are conventionally carried out in packed towers/columns that exhibit poor mass transfer performance and, as a result, suffer limitations related to low efficiency, bulkiness, high costs and inflexibility in operation [10,11,12]. It is therefore necessary to develop a simple and efficient technique to remove DO from water, and a gas–liquid contactor capable of good mass transfer performance is desirable.

The rotor–stator reactor (RSR) is a novel multiphase contactor comprising a series of rotor rings and stator rings alternately configured in a radial direction [13]. In an RSR, a high-gravity environment several orders of magnitude greater than the Earth’s gravitational field can be created as a result of the huge centrifugal force produced by rapid rotation of the rotor. Consequently, the liquid stream in the RSR is broken into small elements and thin films [14,15,16]. There is also increased turbulence of the gas and liquid streams, in addition to rapid renewal of the gas–liquid interface [17,18]. All of these properties can greatly enhance the mass transfer rate in an RSR. Thus, RSRs have successfully been employed in degradation of organic pollutants [19,20], nanomaterial synthesis [21], CO₂ capture [22] and other applications.

This work therefore employed an RSR to intensify the removal of DO from water through nitrogen stripping coupled with vacuum degassing (vacuum–N₂–H₂O–O₂ system). The effects of various operating conditions, such as the rotational speed of the RSR, the liquid volumetric flow rate, the gas volumetric flow rate and the vacuum degree of the RSR, on the deoxygenation efficiency, as well as on the mass transfer coefficient, were investigated. Separate experiments involving nitrogen stripping (N₂–H₂O–O₂ system) and vacuum degassing (vacuum–H₂O–O₂ system) were also carried out for comparison. Additionally, a correlation to predict the mass transfer coefficient (K_La) in the RSR was also established.

2. Materials and Methods

2.1. Structure of RSR

The structure of the RSR is shown in Figure 1a. The RSR consisted primarily of a liquid distributor, rotor seat, shaft, seal, rotor and stator. The rotor was comprised of six circular rings (named rotor rings) located on a rotor seat, which was connected to a motor by a shaft, while the stator consisted of five layers of pins (named stator rings) mounted concentrically on a cover cap. As shown in Figure 1b, the open space between pins in the same layer and the perforations in the rotor provide the flow channels for fluids in the RSR [15].

As shown in

Table 1. Specifications of the RSR.

Item	Unit	Value
Layer number of rotor rings	-	6
Layer number of stator rings	-	5
Number of perforations in rotor rings	-	180, 240, 294, 348, 408, 462
Number of pins in stator rings	-	12, 16, 20, 24, 24
Diameter of perforations in rotor rings	mm	4
Diameter of pins in stator rings	mm	5
Inner diameter of rotor rings	mm	70, 94, 118, 142, 166, 190
Inner diameter of stator rings	mm	80, 104, 128, 152, 176
Inner diameter of the RSR	mm	300
Axial depth of rotor rings	mm	61
Axial depth of stator rings	mm	60
Axial depth of the RSR	mm	65
Internal volume of the RSR	cm3	4592

, the inner diameter of the rotor rings ranged from 70 to 190 mm and thus could provide centrifugal acceleration ranging from 28.48 to 1395.68 m²/s. The stator rings (diameter ranges from 80 to 176 mm) allow the redistribution of liquid in an RSR.

2.2. Experimental Procedure

Figure 2 shows the experimental setup for the vacuum–N₂–H₂O–O₂ system. The liquid inlet and outlet of the RSR were connected to a centrifugal pump and sealed tank, respectively, whereas the gas inlet and outlet were connected respectively to a nitrogen gas cylinder and a vacuum system, which was made up of a vacuum pump and a buffer tank. The buffer tank helped to maintain the pressure balance in the DO removal system. Tap water was pumped via the liquid distributor into the RSR vacuumized below atmospheric pressure and allowed to flow radially outward through the rotor rings and stator rings, while nitrogen gas was introduced into the RSR via a gas inlet and allowed to flow inward through the rotor rings and stator rings. The nitrogen gas stream made contact in a counter-current with the water stream in the RSR, leading to removal of DO from the water by both vacuum degassing and nitrogen stripping. The gas and liquid streams finally exited the RSR via the gas and liquid outlets, respectively. The DO concentration in the tap water and deoxygenated water was measured using a DO detector (Rex, SJG-203A, CHN; detection limits: 0~19.99 mg/L). The composition of the gas used in this study was 99.5% N₂ and 0.5% O₂.

Experiments involving nitrogen stripping or vacuum degassing were performed in the same way as with the vacuum–N₂ technique.

The operating conditions were set as follows: rotational speed = 200–1400 rpm, liquid volumetric flow rate = 0.35–0.6 m³/h, gas volumetric flow rate = 1–7 m³/h, vacuum degree = 0.02–0.06 MPa, inlet liquid temperature = 300 ± 2 K (ambient temperature) and initial DO concentration in tap water = 7.85–8.01 mg/L.

2.3. Calculation of K_La and η

The equation for the experimental K_La (Equation (1)) was obtained by referring to literature [23]:

$$K_{\mathrm{L}}a=\frac{Q_{\mathrm{L}}}{H\pi R^2}\times \frac{x_{\mathrm{in}}-x_{\mathrm{out}}}{{\left(x-x_{\mathrm{e}}\right)}_{\mathrm{in}}-{\left(x-x_{\mathrm{e}}\right)}_{\mathrm{out}}}\ln \left(\frac{{\left(x-x_{\mathrm{e}}\right)}_{\mathrm{in}}}{{\left(x-x_{\mathrm{e}}\right)}_{\mathrm{out}}}\right)/c_{\mathrm{M}}$$

(1)

where x_e is the equilibrium molar fraction of O₂ in liquid which was obtained using Equation (2):

$$x_{\mathrm{e}}=\frac{L}{m\mathrm{G}}\left(x-x_{\mathrm{out}}\right)$$

(2)

The deoxygenation efficiency (η) was determined by the molar concentration of O₂ at the liquid inlet (c_in) and the outlet (c_out) (Equation (3)):

$$\eta =\frac{c_{\mathrm{in}}-c_{\mathrm{out}}}{c_{\mathrm{in}}}\times 100\%$$

(3)

3. Results and Discussion

3.1. Effect of Rotational Speed

The effect of the rotational speed on η and K_La is illustrated in Figure 3. Both η and K_La increased from 96.32% and 0.0803 s⁻¹ to 97.34% and 0.0882 s⁻¹, respectively, with an increase in rotational speed from 200 to 600 rpm, beyond which both η and K_La showed little change with increasing rotational speed. Higher rotational speeds caused a larger centrifugal force, which split the liquid into finer elements and thinner films. Consequently, there was increased turbulence in the gas and liquid streams, a larger gas–liquid interfacial area and a faster renewal rate of the gas–liquid interface, resulting in thinner gas and liquid boundary layers. All of these factors led to an enhanced gas–liquid mass transfer rate and thereby a larger K_La and higher η.

Nonetheless, increasing rotational speed brought about increased liquid velocity, which reduced liquid residence time in the RSR and liquid holdup declined accordingly, perhaps leading to a decrease in the gas–liquid interfacial area. The effect of the phenomena at rotational speeds greater than 600 rpm offset the aforementioned benefits of higher rotational speeds in this study, resulting in almost stable η and K_La.

According to Henry’s law, the lowest equilibrium oxygen concentration in liquid is 0.2028 mg/L at 25 °C. Thus, the highest deoxygenation efficiency is 97.47% for tap water with an initial DO concentration of 8.01 mg/L. The deoxygenation efficiency of 97.34% in this study was close to the highest one, suggesting the good deoxygenation effect of the RSR.

3.2. Effect of Liquid Volumetric Flow Rate

Figure 4 shows the effect of the liquid volumetric flow rate on η and K_La. It was noted that η decreased by 4.22% (from 97.39 to 93.28%) while K_La increased by 27.98% (from 0.0772 to 0.0988 s⁻¹) with an increase in liquid volumetric flow rate from 0.35 to 0.6 m³/h. A higher liquid volumetric flow rate resulted in more liquid droplets and, consequently, a larger gas–liquid interface area, leading to an increase in K_La. Moreover, oxygen is sparingly soluble in water and the removal of DO from water is controlled by a liquid film. Thus, a higher liquid volumetric flow rate can result in a larger K_La. However, at a given gas–liquid equilibrium, vacuum degree and gas volumetric flow rate, a higher liquid volumetric flow rate led to a decline in η. A higher liquid volumetric flow rate led to a shorter liquid residence time in the RSR. This probably caused more liquid to exit the RSR before the maximum DO removal was achieved.

3.3. Effect of Gas Volumetric Flow Rate

As shown in Figure 5, both η and K_La increased from 95.97 to 97.34% and 0.0791 to 0.0882 s⁻¹, respectively, with an increase in the gas volumetric flow rate from 1 to 3 m³/h, and thereafter they remained almost stable with further increases in the gas volumetric flow rate. This was because a higher gas volumetric flow rate resulted in increased turbulence in the gas and liquid streams, leading to a larger gas–liquid interfacial area and faster renewal rate of the gas–liquid interface, thereby resulting in the observed increase in η and K_La. However, as the gas volumetric flow rate further increased over 3 m³/h, the oxygen might have reached equilibrium between the gas and liquid phases. Thus, the increase in the gas–liquid interfacial area and the renewal rate of the gas–liquid interface had no effect on the oxygen transfer from water to gas. Therefore, both η and K_La remained stable when the gas volumetric flow exceeded 3 m³/h.

3.4. Effect of Vacuum Degree

The effect of the vacuum degree on η and K_La is shown in Figure 6. Both η and K_La increased from 95.03 to 97.06% and 0.0728 to 0.0856 s⁻¹, respectively, when the vacuum degree rose from 0.02 MPa to 0.04 MPa. This was because a higher vacuum degree causes more water vapor and lower oxygen partial pressure in the gas phase. Therefore, a high vacuum degree and more water vapor in the gas phase resulted in an increased mass transfer driving force and, consequently, higher η. A higher vacuum degree also results in a thinner mass transfer boundary layer [24]. Consequently, there was reduced mass transfer resistance and, hence, K_La was larger, which is also conducive to oxygen removal from water.

However, the DO concentration was low and the mass transfer driving force was small when the vacuum reached a high degree. Furthermore, the oxygen approached equilibrium between the gas and liquid phases under such conditions. Hence, both η and K_La increased slowly from 97.06 to 97.34% and 0.0856 to 0.0882 s⁻¹, respectively, with an increase in the vacuum degree from 0.04 to 0.06 MPa.

3.5. Comparison of Different Deoxygenation Systems in RSR

Figure 7 shows the values for η and K_La achieved by the N₂–H₂O–O₂, vacuum–H₂O–O₂ and vacuum–N₂–H₂O–O₂ systems in the RSR, respectively. It is evident that the vacuum–N₂–H₂O–O₂ system achieved the highest values for K_La and η among the three systems. This can be attributed to the synergistic effect of nitrogen stripping and vacuum degassing, as oxygen partial pressure in the gas phase of the vacuum–N₂–H₂O–O₂ system at a certain vacuum degree was lower than that of the N₂–H₂O–O₂ system at atmospheric pressure or the vacuum–H₂O–O₂ system at the same vacuum degree. Thus, according to Henry’s law, the equilibrium concentration of DO in water in the vacuum–N₂–H₂O–O₂ system was lower than that in the N₂–H₂O–O₂ system at atmospheric pressure or the vacuum–H₂O–O₂ system at the same vacuum degree. In addition, it was also deduced that there was stronger turbulence in the vacuum–N₂––H₂O–O₂ system in the RSR due to a faster gas velocity. This resulted in a larger gas–liquid interfacial area and a higher renewal rate of the gas–liquid interface, thereby leading to higher K_La and η.

3.6. Correlation for K_La

It was assumed that the mass transfer coefficient K_La in the RSR was influenced by 14 major factors, as shown in

Table 2. Major influence factors of K_La.

Factor	Symbol	Value	Unit	Dimension
Liquid inlet velocity	uL	3.1~5.3	m/s	[LT−1]
Angular velocity of rotor	ω	21~147	s−1	[T−1]
Geometric radius of rotor	R	0.115	m	[L]
Liquid density	ρL	997	kg/m3	[ML−3]
Liquid viscosity	μL	8.94 × 10−4	kg/(m·s)	[ML−1T−1]
Liquid surface tension	σ	71.97	kg/s2	[MT−2]
Gravitational acceleration	g	9.81	m/s2	[LT−2]
Temperature	T	25~29	°C	[Θ]
Inlet air humidity	φ	-	%	-
Gas inlet velocity	uG	8.85~61.95	m/s	[LT−1]
Gas density	ρG	0.5~1.25	kg/m3	[ML−3]
Gas viscosity	μG	1.78 × 10−5	kg/(m·s)	[ML−1T−1]
Oxygen diffusivity in water	DAB	2.41 × 10−9	m2/s	[L−2T]
Vacuum degree	P	0~0.06	MPa	[L−1MT2]

. The values of these factors were based on the experimental conditions and physical properties of the gas and liquid.

The basic dimensions of the variables were [T], [L] and [M]. According to the Buckingham pi theorem [25], K_La can be expressed as follows (Equation (4)):

$$Sh=\frac{K_{\mathrm{L}}a{R}^2}{D_{\mathrm{AB}}}=\mathsf{\alpha }{\left(R{e}_{\mathrm{L}}\right)}^{\beta }{\left(R{e}_{\mathrm{G}}\right)}^{\gamma }{\left(S{c}_{\mathrm{G}}\right)}^{\epsilon }{\left(E{u}_{\mathrm{L}}\right)}^{\theta }{\left(F{r}_{\mathrm{L}}\right)}^{\xi }$$

(4)

The coefficients of the correlation were obtained by fitting the experimental data to give the following equation (Equation (5)):

$$Sh=0.99{\left(R{e}_{\mathrm{L}}\right)}^{0.69}{\left(R{e}_{\mathrm{G}}\right)}^{-1.62}{\left(S{c}_{\mathrm{G}}\right)}^{-1.41}{\left(E{u}_{\mathrm{L}}\right)}^{-0.88}{\left(F{r}_{\mathrm{L}}\right)}^{-0.14}$$

(5)

As shown in Figure 8, the predicted K_La values were in agreement with the experimental K_La values, with deviations generally within 20%. Thus, the correlation can be used to predict K_La in an RSR.

Table 3. Comparison of different deoxygenation systems in various high gravity devices.

Reference	This Study	Lin et al.	Guan et al.
System	Vacuum–N2–H2O–O2	N2–H2O–O2	Vacuum–H2O–O2
High gravity device	RSR	RSR	Rotating packed bed
Liquid flow rate, m3/h	0.35~0.6	0.75~2.0	0.02~0.10
Gas flow rate, m3/h	1~7	1.5~4.0	-
Rotational speed, rpm	200~1400	300~1450	800~1400
Vacuum degree, MPa	0.02~0.06	0	0.08~0.1
Range of mass transfer coefficient, s−1	0.073~0.098	0.077~0.34	0.031~0.202
Reference	-	[26]	[27]

shows that the accuracy of the correlation obtained in this study was similar to that of other studies in the literature. Furthermore, the correlation could predict K_La at atmospheric pressure as well as at reduced pressure.

4. Conclusions

This study employed a coupled vacuum–N₂ technique to remove DO from water in an RSR. The effects of various operating conditions, including the rotational speed, the liquid volumetric flow rate, the gas volumetric flow rate and the vacuum degree, on the values of η and K_La were investigated. The optimum operating conditions in terms of deoxygenation efficiency and energy consumption were determined as a rotational speed of 600 rpm, a liquid volumetric flow rate of 0.4 m³/h, a gas volumetric flow rate of 3 m³/h and a vacuum degree of 0.06 MPa. Under these conditions, the vacuum–N₂–H₂O–O₂ system achieved values for η and K_La of 97.34% and 0.0882 s⁻¹, respectively. Additionally, a correlation to predict the K_La in the RSR was established, and the results show that the predicted values were in agreement with the experimental values, with deviations generally within 20%. These results indicate that the coupled technique carried out in an RSR is a feasible approach to remove DO from water under reasonable operating conditions thanks to the enhanced synergistic effect of nitrogen stripping and vacuum degassing under a high gravity environment.