A New Spray Approach to Produce Uniform Ultrafine Coatings

A new spray approach is proposed to overcome the disadvantages of the traditional single-orifice nozzle, such as uneven coatings, overspray, and low efficiency. Both the experimental measurements and numerical simulation are used to investigate the spray characteristics of the multiorifice nozzle. +e results show the new nozzle structure is able to disperse the particles in a wider regime and reduce the central pressure. It is an effective way to produce uniform ultrafine coatings.


Introduction
Nanoparticles with size between a few nanometers and 100 nm have great potential for use in various industry applications such as nanostructured film deposition [1], drug carriers [2], superconductors [3], and catalyst.ere are a large number of techniques for the preparations of ultrafine particles [4].Among them, spray technology using suspension or solution precursors has been most widely used [5].e suspension or solution feeding is prepared by the coating material dispersing or dissolving in a liquid carrier, which allows the controlled injection of much finer particle than conventional thermal spraying [6,7].
One of the largest challenges of spray technology is how to control the spray pattern and droplet size distribution.As concern to the traditional spray technology, such as round jet and annular spray, there are some significant defects.For example, firstly, the droplets tend to concentrate in the center axis which gives rise to the highly uneven distribution of liquid fragments.Second, the pressure is too high in the spray center, which always results in overspray.ird, the spray efficiency is low since the spatial distribution is narrow.ese problems are particularly important for ultrafine coating due to its strict requirements.In order to solve these problems, the common practices are optimization design of the operating parameters such as adjustment of pressure, nozzle orifice, and gas-to-liquid flow ratio [8][9][10][11].ese approaches can alleviate the uneven spray pattern, whereas the effect is limited and not essential to solve the above problems.
In this paper, a new spray approach with nozzle structure of multiple gas orifices is introduced to greatly improve the uniformity of the ultrafine coatings.Both the diagnostic measurements and numerical modeling are used to investigate the differences in flow behavior of multiorifice spray and traditional single-hole spray.For the experimental setup, hot-wire anemometer is used to measure the distributions of gas velocity, and laser particle analyzer is introduced to obtain the data of the particle size distribution.For the numerical calculation, based on the commercial software, discrete particle model (DPM) is adopted to simulate the gas-liquid two-phase flow.Taylor analogy breakup (TAB) model is used to describe the droplet breakup.e calculation results are compared by the experimental data.After validation, spatial distribution of pressure and velocity field is analyzed in detail to reveal the spray pattern characteristics of the multiorifice nozzle.en, the particle size and spatial distributions are discussed, and the advantages of the new spray approaches are concluded.ere are three types of ori ces, which include central ori ce, auxiliary gas ori ces, and fan gas ori ces.Based on an extremely large relative velocity between gas and liquid (more than 100 m/s), the central ori ce can be able to facilitate primary atomization.e auxiliary gas ori ces are used to carry out secondary atomization and alleviate the phenomenon of entrainment.For the fan gas ori ces, gas was provided at a constant slope angle.By controlling gas ux and pressures, the gas ow from fan ori ce can be used to adjust the spray shape.

Computing Model.
Using the commercial software, the discrete particle model (DPM) was adopted to describe the gas-liquid two-phase ow.DPM is a multiphase ow model based on the Eulerian-Lagrangian method, in which the gas governing equation is solved as a continuous phase in the Euler coordinate system [12,13].e particles are considered as a discrete phase in the Lagrangian coordinate system.Initially, the gas ow eld was numerically calculated by k-ε turbulent model and pressure-based solver.en, the droplet particle was added subsequently by using solid-cone injection type, dynamic drag model, and Taylor analogy breakup (TAB) model [14,15].e equation of motion of particles is shown below: where ρ p is the density of the particle, ρ g is the density of the uid, u p (u p , v p , w p ) and u g (u g , v g , w g ) are, respectively, the velocity vectors of discrete phase particle and continuous phase uid, g is the gravitational acceleration, and Δ is an additional acceleration term for unit particle mass.e dynamic drag coe cient model which is incorporated in FLUENT software has been used in Δ. τ r is the discrete phase particle relaxation time.
e droplet distortion equation of TAB model for droplet breakup can be expressed as below: where x is the displacement of the droplet equator from its spherical position.e coe cients of ( 2) are determined by Taylor analogy [16]: Figure 2 shows the computational regime of the numerical model.e nozzle is located in a cuboid computational domain with size of 200 mm * 200 mm * 400 mm.21 million computational cells were used in the whole domain.Finer meshes are used for the core region of the spray.e grid dependency has been validated, and the computational results are convergence under the present mesh size.Pressure inlet boundary conditions are applied on the orices of the nozzle.e injection pressures of central and auxiliary gas ori ces are 120 KPa and 50 KPa for the fan gas ori ces.e wall boundary condition is used at the plane ADHE.Pressure outlet boundary conditions are applied on the planes ABCD, EFGH, DCGH, ABFE, and BCGF.For discrete particles, the parcels are introduced in the system at the central ori ce exit, which has the original size of 65 μm with Rosin-Rammler distribution and original velocity of 50 m/s.Usually, a total number of 10,000 computational parcels are injected into the ow for each case.ese initial conditions are provided and validated by the experimental data.

Velocity Measurements.
e schematic of hot-wire anemometry measuring system is shown in Figure 3. is system can be used to obtain the velocity data of gas ow led.e gas source is provided by an air pump which can satisfy actual working conditions.e air ow pressure can be measured by the piezometer.Before measurement, the velocity calibration should be conducted.en, a traverse measurement system is applied to acquire velocity data by a hot-wire probe.e measuring results include the velocity data on planes X-Y and X-Z (shown in Figure 2). 2 Journal of Nanotechnology 3.2.Particle Size Measurements.Figure 4 illustrates the laser particle analyzer measurement system.e laser particle analyzer device includes the emitter and receiver part.ese two parts are set upon the different position of spray gun to ensure laser traversing measuring area.e receiver device must be calibrated before the first measurement.e lid of the receiver is used to ensure that no natural light distorts the accuracy of measurements.A traverse coordinate system is used to measure particle size data from various cross sections.Sources of gas and liquid are provided with air pump and diaphragm pump, respectively.e pressure and flow rate can be measured by the piezometer and flow meter, respectively.e gas media is air, and the liquid media is water.e agreement between the predictions and measurements is qualitatively achieved.Results show the gas velocity reaches highest in the center of the spray core at the nozzle exit.With the evolution of the spray, gas velocity declined dramatically from 70 m/s to lower than 10 m/s.Due to the effects of fan gas orifice, the spray angle on the X-Y plane is much larger than that on the X-Z plane, which is totally different from the single round or annular orifice jet.

Result and Discussion
Figure 6 illustrates the quantitative comparison of the velocity evolution along with the Y-axis and X-axis.In Figure 6(a), d represents the distance between the cross section and the nozzle orifice.As the d increases, the velocity curve of the gas filed along with the Y-axis tends to be flat progressively, which means the velocity field approaches to homogenization.As Figure 6(b) indicates, the gas velocity decays at the downstream of the spray due to the entrainment effects.In Figure 6, the calculated results agreed with experimental data well.

Spatial Distribution of Pressure and Velocity Field.
Among the investigations of the spray filed, the distribution of pressure and velocity is the primary interest.Figures 7 and  8 compare the velocity and pressure contours between single-hole nozzle spray and multiorifice nozzle spray, respectively.In Figures 7(a) and 8(a), for the single-orifice case, the velocity and pressure contours are almost symmetrical at the X-Y plane and X-Z plane, whereas, for the multiorifice case, with the help of auxiliary gas orifices and fan gas orifices, the spray pattern becomes totally different.e differences can be concluded in three points: firstly, in the single-nozzle case, the jet pattern is similar to a cylinder.e spray angles for both X-Y and X-Z planes are small.While for the multiorifice case, the spray range becomes larger on the X-Y plane after leaving the orifice for a distance.On the contrary, the spray angle becomes smaller on the X-Z plane beyond 15 mm from the nozzle exit.Second, at the downstream of the spray, the central pressure of the multiorifice jet is lower than that of the single-orifice jet, which can relieve the phenomenon of overspray in the center.Finally, due to the effect of spray entrainment, the nozzle exits are used to be polluted by the whirling gas and    small droplets.is problem can be improved by the introduction of auxiliary gas ori ces. is is because some droplets dissolved in the spray led in the experimental setup.

Gas-Liquid Two-Phase Flow
ese phenomena can not be calculated by the present model.Generally, as indicated in Figure 9(c), particle size distributions of the experiment and simulation are consistent.Both of them have the Sauter mean diameter (de ned as the ratio of volumesurface mean diameter) around 55 μm.

Droplet Spatial and Size Distributions.
In Figure 10, the horizontal coordinate presents the location of the droplet particles, and the vertical coordinate presents the diameter of the particles.As we can see from Figure 10(a), according to the particle spatial distribution on the plate, the shape of the multiori ce spray is oval.From the Y-axis, the droplets are dispersed between −25 and 25 mm.From the Z-axis, the droplets are concentrated between −10 and 10 mm.In order to compare, a further simulation analysis for the spray with single ori ce is conducted.In Figure 10(b), without the auxiliary gas ori ces and fan gas ori ces, the atomization e ect deteriorates, the larger droplet increases, and most of the droplets are concentrated in a circular region with radius about 10 mm.

Conclusions
A new nozzle structure which can improve the spray coating uniformity was proposed in the present paper.Both the

Data Availability
e data used to support the findings of this study are available from the corresponding author upon request.

4. 1 .
Single-Phase Flow Field 4.1.1.Validation.Figure 5 shows a comparison of experimental data and model predictions for the gas velocity distributions of the multiorifice nozzle.Both the experiments and calculations are conducted under the same operating conditions that are presented in Section 2.2.

Figure 5 :
Figure 5: Comparison of computational and experimental gas velocity distribution.(a) Contours on the X-Y plane (left: calculation; right: experiment); (b) contours on the X-Z plane (left: calculation; right: experiment).

Figure 6 :
Figure 6: Comparison of computational and experimental gas velocity evolution.(a) Gas velocity along with the Y-axis for di erent measuring points; (b) gas velocity along with the X-axis.

Field 4 . 2 . 1 .
Droplet Size Distribution.Figure9indicates the histogram of experimental and calculated drop size distributions.Figure9(a) shows the experimental size distribution of the atomized droplets with the size range mainly between 2.31 μm and 74.82 μm.Figure9(b) presents the calculated results based on the DPM model, in which the droplet size range is mostly between 26.6 μm and 70.13 μm.Due to the droplet collision and coalescent e ect, both the experiment and simulation have larger particles with a diameter larger than 150 μm.Although the calculated results match the experimental data well, the signi cant divergence also exists for the smaller particles.e ner droplets with size between 2.31 μm and 26.6 μm take certain percentage for experiments.

Figure 9 :
Figure 9: Droplet size distribution.(a) Histogram of experimental drop size distribution, (b) histogram of calculated drop size distribution, and (c) comparison of experimental data with calculated results.