The Performance Prediction Model of W-Shaped Hydrocyclone Based on Experimental Research

Abstract

Fine particles misclassification in the underflow (UF) of grinding-classification hydrocyclones might result in ore over-grinding, leading to both reduced ball mill throughput and metal recovery. In the current research, a W-shaped hydrocyclone is proposed, to efficiently decrease the misclassification of fine particles in UF. The effects of the following parameters (including cross-effects) on W-shaped hydrocyclone classification performance were studied experimentally—inlet pressure, apex diameter, and vortex finder insertion depth and diameter. A mathematical model on the basis of the response surface method was established for the prediction of W-shaped hydrocyclone separation performance. The significance of the effects of the factors on the fine particle content in UF decreased in the following order—vortex finder diameter > inlet pressure > vortex finder insertion depth > apex diameter. The significance of influences of different factors on quality effectively decreased in the following order—inlet pressure > vortex finder insertion depth > vortex finder diameter > apex diameter. The significance of factor effects on the quantity efficiency decreased in the following order—inlet pressure > vortex finder insertion depth > apex diameter > vortex finder diameter. All influence factors were considered to obtain the optimal parameter configuration—an apex diameter of 0.14 D, a vortex finder diameter of 0.31 D, an insertion depth of 1.87 D, and an inlet pressure of 0.18 MPa. The corresponding optimal result was a −25 μm particle content (C₋₂₅) in UF of 11.92%, a quality efficiency of 42.48%, and a quantity efficiency of 98.99%.

1. Introduction

Hydrocyclones are extensively applied as separation and classification machines for grinding-classification. However, the hydrocyclone classification principle [1,2,3,4] can result in a “misclassification” phenomenon (misclassification of fine particles in underflow (UF) and coarse particles in overflow (OF)). When classifying high-concentration, coarse-grained materials, the settling velocity of multi-component particles in swirling flow fields, results in fine particle misclassification in UF, which in turn often causes ore over-grinding that reduces metal recovery and ball mill throughput. Therefore, preventing misclassification in hydrocyclones has become a challenging and active topic for research [5,6,7,8]. In a traditional hydrocyclone, the cylindrical-conical structure determines the main flow field boundary structure and the mechanisms that affect the separation sharpness and classification efficiency [9,10]. The cut size of a traditional cylindrical–conical hydrocyclone is directly proportional to the cone angle [11,12]. Using a traditional cylindrical–conical hydrocyclone for the classification of high-concentration coarse-grained materials results in a small cut size. In the grinding-classification, this small cut size often causes problems, such as an excessive circulating load, increased fine particle misclassification in UF, and easy clogging, which in turn give rise to low classification efficiency of the hydrocyclone, over-grinding of the mill, and a limited increase in the ball mill throughput [13,14,15].

Thus, numerous studies were conducted to optimize the hydrocyclone structure. Dueck [16] injected water into a certain conical section position at a predetermined speed. The outer vortex was broken up. The fine particles settled on wall were pushed to the hydrocyclone center and then re-entered the inner vortex, to be finally discharged from the vortex finder. This decreased the fine particle number reported to UF. Wang et al. [17,18] designed a membrane-shaped vortex finder, in which the overflow liquid could be collected separately through membrane infiltration, in the process of separation. Their studies showed that the membrane-shaped overflow tube could reduce the turbulence near the overflow tube and reduce the overflow. Yang et al. [19] developed a micro-cyclone with a pre-arrangement of particles by installing a flow passage around the cylinder, in front of the feed pipe. By comparing with the cylindrical cone cyclone, they found that the counter-rotating pre-arrangement device improved the particle separation efficiency. Yang [20] proposed replacing the traditional single-cone hydrocyclone with a double-cone model. Computational fluid dynamics studies showed that the double-cone hydrocyclone had a higher separation efficiency and sharpness than the traditional hydrocyclone. Fricker et al. [21] embedded the cyclone in the middle of the annular magnetic pole and designed a magnetic cyclone, which used the functions of gravity separation and magnetic separation for mineral separation, and had an obvious effect on the separation of fine-grained magnetic minerals. Ye et al. [22] addressed the difficulties in the classification of ultrafine particles by traditional hydrocyclones, by studying a conical section cross-section and designing a multi-section composite cone. Jokovica et al. [23,24] proposed a semi-inverted hydrocyclone and achieved encouraging results, significantly reducing the water split to coarse product and much coarser cut sizes. Tang et al. [25] used CFD technology to study the separation performance of hydrocyclone, under different inlet structure size and inlet velocity combinations. To reduce fine particle misclassification in UF, the author proposed a W-shaped hydrocyclone in the early study [26]. As shown in Figure 1, the main stage space of W-shaped structures was the upper column, while the lower W-shaped structures that make cyclone bottom had a high concentration circulating flow, in which the solid particles gathered into a circulating fluidized bed. In our previous research, the author obtained a flow field distribution inside the W-shaped hydrocyclone and compared it with the conventional one. The results showed that the W-shaped hydrocyclone had certain advantages in reducing the fine particle content in UF.

Various structural parameters, operating parameters, and physical property parameters influence W-shaped hydrocyclone separation performance. Cross-effects were observed among these factors [27,28,29]. Martínez et al. [30] investigated the effect of the insertion depth of a vortex finder on hydrocyclone separation performance. The results showed that an appropriate insertion depth reduced coarse particle misclassification in the OF from the flow of short-circuit. The highest efficiency of separation was obtained for an insertion depth of 10% of hydrocyclone total length. Tang et al. [31] investigated the effect of the structural parameters of vortex finder on the separation sharpness of the hydrocyclone and established a multiple regression model. The diameter of the vortex finder had the strongest influence on separation sharpness, followed by the depth of insertion, whereas the thickness of the vortex finder wall had the least significant influence on the separation sharpness. As the outlet for coarse-grained products, the apex has a critical effect on the multiphase flow in the hydrocyclone. Kilavuz [32] quantified the relationship between diameters of apex and vortex finder. An exponential relationship between fine particle content and cone ratio in UF was reported. Thus, the classification sharpness could be improved by controlling the cone ratio. Zhang et al. [33] studied how cross-effects between feed particle size and apex diameter influence the performance of separation. It was found that an appropriate increase in the diameter of apex mitigated the feed particle size fluctuation impact. Yu et al. [34] applied mini-hydrocyclones to separate rare earth particles. The comprehensive effects of different factors, such as feed concentration, split ratio, and flow rate on the efficiency of separation was studied using the response surface method. Bicalho [35] showed that appropriately increasing the feed flow rate improved the hydrocyclone separation efficiency, whereas an excessively high rate of flow decreased the particle’s effective residence times and thereby the efficiency of separation.

In this study, based on previous research, the factors affecting hydrocyclone separation performance were explored for specific engineering problems, and the mathematical model for predicting the separation performance of the W-shaped hydrocyclone was established, based on the response surface method, which has important guiding significance for optimizing the design of the hydrocyclone.

2. Materials and Methods

2.1. Apparatus

A hydrocyclone separation test system was developed for the determination of the performance of separation in a W-shaped hydrocyclone with Φ75 mm [36]; the structure parameters are shown in Figure 2. The main components of the system, as presented in Figure 3, included a hydrocyclone, a slurry pump, a mixing tank, valves, pipelines, flow meters, pressure gauges, and a frequency converter. In this research, quartz powder (98% purity with a main component of SiO₂) was applied for the elimination of the errors generated by the separation effect.

2.2. Materials

The size distribution of particles was obtained by a BT-9300S laser particle size analyzer (Bettersize Instruments Ltd., Danton, China), as shown in

Table 1. Distribution of particle size in the test material.

Mesh Number	Size (μm)	Content (%)	Negative Accumulation (%)
<60	>250	0.04	100
60–70	212–250	0.32	99.96
70–80	180–212	0.99	99.64
80–100	150–180	2.73	98.65
100–140	109–150	9.84	95.92
140–200	75–100	13.94	86.08
200–325	75–45	21.93	72.14
325–600	23–45	21.94	50.21
600–1250	10–23	15.61	28.27
>1250	<10	12.66	12.66

. Negative accumulation refers to the content of all solid phases less than the particle size. Particles with diameters less than 23 μm comprised 28.27% of the total amount of particles, those with diameters of below 45 μm made up 50.21%, and those greater than 100 μm in size comprised 13.92% of the total particle amount. Since 75 mm hydrocyclone cut size was 25–75 μm, this material was considered to be appropriate to test the W-shaped hydrocyclone separation performance. Particles with diameters of less than 23 μm were considered as fine particles, and those with sizes above 100 μm were assumed to be coarse particles.

2.3. Experimental Design

First, the other parameters were kept fixed and only one factor was changed to conduct a multi-level test, for the determination of the effect rule of each factor on separation performance.

Table 2. Table of factor-level for single factor tests.

Level	Apex Diameter (mm)	Vortex Finder Diameter (mm)	Vortex Finder Insertion Depth (mm)	Inlet Pressure (MPa)
1	9	25	80	0.14
2	12	25	80	0.14
3	15	25	80	0.14
4	18	25	80	0.14
5	21	25	80	0.14
6	12	15	80	0.14
7	12	20	80	0.14
8	12	25	80	0.14
9	12	30	80	0.14
10	15	25	60	0.14
11	15	25	80	0.14
12	15	25	100	0.14
13	15	25	120	0.14
14	15	25	140	0.14
15	15	25	80	0.10
16	15	25	80	0.12
17	15	25	80	0.14
18	15	25	80	0.16
19	15	25	80	0.18

summarizes the level table of factors applied in single-factor tests. Then, the results were used to establish a central composite design, based on the response surface method [37]. Each test point of the design was uniformly sampled within the variation range of the factors. A test table was formed by the uniform distribution, permutation, and combination of factors. The central composite design based on the response surface method was highly representative and reflected some of the characteristics of the comprehensive experiment. Multiple linear regression equations were established by considering a certain performance indicator to be a function of one or more factors. The optimal configuration was thus obtained more intuitively. The structure parameters such as the vortex finder and the apex were dimensionless, based on the hydrocyclone main diameter (D). The diameter of dimensionless apex (X₁), the diameter of vortex finder (X₂), vortex finder insertion depth (X₃), and the inlet pressure (X₄) were subjected to a four-factor, three-level central composite design. The Expert Design 11 software (V11.1.2.0, Stat-Ease Inc., Minneapolis, MN, USA) was employed for the data analysis.

Table 3. Scheme of center composite design based on the response surface method (the dimensionless factor).

Level	Apex Diameter (D)	Vortex Finder Diameter (D)	Vortex Finder Insertion Depth (D)	Inlet Pressure (MPa)
1	0.12	0.20	1.33	0.14
2	0.28	0.20	1.33	0.14
3	0.12	0.40	1.33	0.14
4	0.28	0.40	1.33	0.14
5	0.20	0.30	0.80	0.10
6	0.20	0.30	1.87	0.10
7	0.20	0.30	0.80	0.18
8	0.20	0.30	1.87	0.18
9	0.12	0.30	1.33	0.10
10	0.28	0.30	1.33	0.10
11	0.12	0.30	1.33	0.18
12	0.28	0.30	1.33	0.18
13	0.20	0.20	0.80	0.14
14	0.20	0.40	0.80	0.14
15	0.20	0.20	1.87	0.14
16	0.20	0.40	1.87	0.14
17	0.12	0.30	0.80	0.14
18	0.28	0.30	0.80	0.14
19	0.12	0.30	1.87	0.14
20	0.28	0.30	1.87	0.14
21	0.20	0.20	1.33	0.10
22	0.20	0.40	1.33	0.10
23	0.20	0.20	1.33	0.18
24	0.20	0.40	1.33	0.18
25	0.20	0.30	1.33	0.14
26	0.20	0.30	1.33	0.14
27	0.20	0.30	1.33	0.14
28	0.20	0.30	1.33	0.14
29	0.20	0.30	1.33	0.14

summarizes the variation range of each factor—X₁: 0.12 D to 0.28 D; X₂: 0.2 D to 0.4 D; X₃: 0.8 D to 1.87 D; and X₄: 0.10 MPa to 0.18 MPa. Additionally, separation performance was analyzed by considering the cut size, particle content, quality efficiency, and quantity efficiency as evaluation indices [38].

3. Results and Discussion

3.1. Effect of the Diameter of Vortex Finder on Separation Performance

Vortex finder diameter effects on separation performance indicators, such as classification efficiency and product particle size, were studied for the vortex finder diameter range of 15–30 mm.

Figure 4 reveals that the diameter of vortex finder strongly affected the classification efficiency curve, which represented the recovery of the specific particle size to UF. As the diameter of the vortex finder enhanced, the classification efficiency curve was significantly shifted to right, and recoveries of all particle size ranges to UF were considerably decreased [39]. For a diameter of vortex finder of 15 mm, fine particle recovery to the UF was more than 25%, indicating the misclassification of fine particles in UF. For a diameter of vortex finder of 30 mm, the hydrocyclone did not recover all coarse particles, indicating significant misclassification of coarse particles in OF. An analysis of the results revealed that at too large vortex finder diameters, the air core created by hydrocyclone occupied the majority of the apex space, significantly affecting the UF discharge. Both resulting UF split ratio and yield were low.

Classification efficiency curve rightward shift revealed the cut size increase. As the vortex finder diameter was increased from 15 mm to 30 mm, a sharp increase from 45 μm to 236 μm was observed in the cut size.

Table 4. Vortex finder diameter effect on classification performance.

Vortex Finder Diameter (mm)	Cut Size (μm)	C−25 (%)		Quality Efficiency (%)	Quantity Efficiency (%)
		OF	UF
15	45	47.09	15.03	37.77	74.48
20	62	42.11	9.50	35.29	88.90
25	144	35.22	10.76	18.00	93.18
30	236	31.94	7.39	6.44	98.57

shows that as the diameter of the vortex finder enhanced, both OF and UF became coarser. A −25 μm particle content (C₋₂₅) in OF decreased from 47.09% to 31.94%, whereas that in UF decreased from 15.03% to 7.39%. At the same time, the quality efficiency was gradually reduced, while quantity efficiency was enhanced. For 30 mm vortex finder diameter, despite high quantity efficiency of 98.57%, 6.44% quality efficiency was achieved. Hence, enhancing the vortex finder diameter could decrease the fine particle misclassification in UF to a certain amount, but is not recommended. Beyond a certain vortex finder diameter, coarse particle misclassification in OF becomes significant and severely reduces the quality efficiency.

3.2. Vortex Finder Insertion Depth Effect on Separation Performance

Vortex finder insertion depth effects on separation performance indicators, such as classification efficiency and product particle size, were investigated at insertion depths of 60–140 mm.

Figure 5 shows the unique effect of vortex finder insertion depth on the classification efficiency curve. The smallest cut size and the highest number of fine particles entering the UF were obtained for a 60 mm insertion depth. The largest cut size was obtained at 140 mm insertion depth, and the recoveries of all particle sizes were very small. Other insertion depths (80 mm, 100 mm, and 120 mm) had little effect on the classification efficiency curve. In general, increasing the insertion depth tended to shift the classification efficiency curve to the right [40].

It can be seen from

Table 5. Vortex finder insertion depth effect on classification performance.

Insertion Depth (mm)	Cut Size (μm)	C−25 (%)		Quality Efficiency (%)	Quantity Efficiency (%)
		OF	UF
60	65	40.73	10.51	31.94	88.32
80	128	39.08	10.05	28.54	90.25
100	130	36.98	9.76	23.32	92.37
120	132	35.51	8.59	19.27	94.75
140	165	34.51	6.68	16.23	96.84

that with the increase of vortex finder insertion depth, both OF and UF particle size gradually decreased. The C₋₂₅ in OF decreased from 40.73% to 34.51%, whereas the content of fine particles in UF decreased from 10.51% to 6.68%. Particle size distribution analysis in hydrocyclones showed that particle size was gradually enhanced from top to bottom and from center to sidewall. Therefore, the increasing vortex finder insertion depth moved the inlet end of the vortex finder closer to the hydrocyclone bottom, increasing the possibility of the entrance of coarse particles to OF. With the increase in vortex finder insertion depth from 60 mm to 140 mm, quantity efficiency was enhanced from 88.32% to 96.84%, and quality efficiency was reduced by 49.19%, from 31.94% to 16.23%. Although increasing the insertion depth could decrease the fine particle content in UF and increase the quantity efficiency, an insertion depth that was too large would significantly reduce the quality efficiency, and coarse particles would be entrained in OF. However, an excessively short vortex finder could result in a short-circuit flow. Therefore, an appropriate vortex finder insertion depth that is neither too long nor too short should be used.

3.3. Apex Diameter Effect on Separation Performance

Hydrocyclone apex is coarse material outlet in the process of classification. Its diameter is an important factor affecting the hydrocyclone separation performance. Apex diameter effect on the separation performance indicators, such as classification efficiency and product particle size, were studied for an apex diameter range of 9–21 mm.

Figure 6 shows the apex diameter effect on the classification efficiency curve. Both the UF split ratio and the yield increased with the apex diameter, resulting in a great number of fine particles mixed into UF [41]. Consequently, recoveries of both fine and coarse particles to UF increased, the cut size decreased, and the efficiency curve shifted leftward.

Table 6. Apex diameter effect on the performance of classification.

Apex Diameter (mm)	Cut Size (μm)	C−25 (%)		Quality Efficiency (%)	Quantity Efficiency (%)
		OF	UF
9	204	34.65	7.21	16.65	96.42
12	138	38.46	9.09	27.40	91.91
15	81	42.85	10.36	36.13	87.07
18	40	52.91	12.42	47.21	77.44
21	38	57.02	14.40	47.26	70.60

shows that the apex diameter significantly affected the product particle size. Both the OF and UF product became finer when the apex diameter was increased. The C₋₂₅ in UF increased by seven percentage points from 7.21% to 14.40%, and the content of fine particles in OF enhanced from 34.65% to 57.02%. This result could be explained by the increased UF flow causing a solid phase portion originally entering the OF discharged from UF. In this solid phase portion, particles were finer than those in original UF but coarser than those in original OF. Hence, transfer of this solid particle portions from OF to UF made both new OF and UF finer.

The cut size was reduced from 204 μm to 38 μm as the diameter of apex was enhanced from 9 to 21 mm. This result indicated that apex diameter had a significant effect on the performance of hydrocyclone separation. Quality efficiency was enhanced from 16.65% to 47.26% and quantity efficiency was decreased from 96.42% to 70.60% (accounting for 26.78%). Too small an apex diameter would hinder the discharge of UF, and the majority of particles would discharge from OF. Additionally, a great amount of coarse particles report to OF, decreasing the quality efficiency. Too large apex diameters would result in an UF concentration that is too small and a solid yield that is too large, producing additional circulating loads. The resulting density of ball milling would be too low and affect the grinding. Hence, classification efficiency and the content of fine particles in UF need to be completely taken into account in determining appropriate apex diameters.

3.4. Inlet Pressure Effect on Separation Performance

Inlet pressure effect on the indicators of separation performance, such as classification efficiency and product particle size, were evaluated at inlet pressures of 0.10, 0.12, 0.14, 0.16, and 0.18 MPa.

Figure 7 shows that the recovery of each particle size to the UF increased with the inlet pressure. Higher number of particles reported to UF, which shifted the curve of classification efficiency toward left and decreased the cut size. An analysis of the data in

Table 7. Inlet pressure effect on classification performance.

Inlet Pressure (MPa)	Cut Size (μm)	C−25 (%)		Quality Efficiency (%)	Quantity Efficiency (%)
		OF	UF
0.10	153	32.94	6.52	10.49	98.02
0.12	149	34.41	7.57	15.79	96.37
0.14	138	35.36	8.22	18.86	95.16
0.16	128	36.44	9.19	21.94	93.42
0.18	98	38.30	9.31	26.92	91.77

shows that with the increase of inlet pressure, tangential velocity within hydrocyclone was enhanced, centrifugal force field was strengthened, and centrifugal inertial force on particles increased [42]. The particle portion originally entering OF gradually overcame the resistance of fluid and entered UF. Consequently, OF and UF both became finer. The C₋₂₅ increased from 32.94% to 38.3% in OF and from 6.52% to 9.31% in OF. Quantity efficiency was reduced from 98.02% to 91.77%, while quality efficiency was enhanced gradually from 10.49% to 26.92%. Previously performed analyses revealed that the main factor influencing quality efficiency was the contents of coarse particles in OF or fine particles in UF. Therefore, inlet pressure effect on the quality efficiency was mainly reflected in the reduced misclassification of coarse particles in OF.

3.5. Mathematical Modeling

In this study, the results of the central composite experiment were analyzed by using the fine particle content in UF, quality efficiency, and quantity efficiency, as evaluation indicators. The results are shown in

Table 8. Central composite experimental results based on the response surface method.

Level	Apex Diameter X1	Vortex Finder Diameter X2	Insertion Depth X3	Inlet Pressure X4	C−25 Y1 (%)	Quality Efficiency Y2 (%)	Quantity Efficiency Y3 (%)
1	0.12	0.20	1.33	0.14	15.99	42.64	84.33
2	0.28	0.20	1.33	0.14	15.38	31.69	29.83
3	0.12	0.40	1.33	0.14	6.89	21.45	98.99
4	0.28	0.40	1.33	0.14	15.48	54.58	83.10
5	0.20	0.30	0.80	0.10	9.43	35.58	69.57
6	0.20	0.30	1.87	0.10	5.54	18.45	80.98
7	0.20	0.30	0.80	0.18	12.09	51.49	64.62
8	0.20	0.30	1.87	0.18	8.20	34.37	76.04
9	0.12	0.30	1.33	0.10	8.15	18.78	92.28
10	0.28	0.30	1.33	0.10	12.84	40.37	62.81
11	0.12	0.30	1.33	0.18	11.51	33.74	98.06
12	0.28	0.30	1.33	0.18	14.81	57.23	57.14
13	0.20	0.20	0.80	0.14	14.61	43.17	44.10
14	0.20	0.40	0.80	0.14	10.11	32.58	83.07
15	0.20	0.20	1.87	0.14	10.72	26.04	55.52
16	0.20	0.40	1.87	0.14	6.22	15.45	94.49
17	0.12	0.30	0.80	0.14	5.31	13.38	69.08
18	0.28	0.30	0.80	0.14	20.77	64.97	65.96
19	0.12	0.30	1.87	0.14	12.89	45.30	97.57
20	0.28	0.30	1.87	0.14	5.42	18.79	40.30
21	0.20	0.20	1.33	0.10	12.28	22.02	60.23
22	0.20	0.40	1.33	0.10	7.35	14.53	96.98
23	0.20	0.20	1.33	0.18	14.51	41.04	53.07
24	0.20	0.40	1.33	0.18	10.45	27.34	94.26
25	0.20	0.30	1.33	0.14	9.86	34.89	78.08
26	0.20	0.30	1.33	0.14	9.86	34.89	78.08
27	0.20	0.30	1.33	0.14	9.86	34.89	78.08
28	0.20	0.30	1.33	0.14	9.86	34.89	78.08
29	0.20	0.30	1.33	0.14	9.86	34.89	78.08

. A multiple linear regression analysis was performed on the test data to obtain regression equations to approximate the true response functions. Equations (1)–(3) show the functional relationships between the responses (C₋₂₅ in UF (Y₁), the quality efficiency (Y₂), and the quantity efficiency (Y₃)), and the dimensionless variables (the apex diameter (X₁), the vortex finder diameter (X₂), the vortex finder insertion depth (X₃), and the inlet pressure (X₄)).

A residual analysis was first performed on the response function models. The results are shown in Figure 8. The distribution of test points was even on both sides of the line and were relatively scattered. The correlation coefficients were R² = 0.995 (C₋₂₅ in UF), R² = 0.929 (quality efficiency), and R² = 0.988 (quantity efficiency). These results showed that the model had a high prediction accuracy. Figure 9 revealed a good agreement between the values predicted by the models and the actual experimental results.

$$\begin{array}{l}{Y}_1=11.37-0.2255X_1-174.354X_2+31.448X_3+66.33X_4+332.357X_1{X}_1\\ +287.5X_1{X}_2-133.937X_1{X}_3-108.594X_1{X}_4+144.583X_2{X}_2\\ +54.375X_2{X}_4-3.106X_3{X}_3-98.698X_4{X}_4\end{array}$$

(1)

$$\begin{array}{l}{Y}_2=-74.797-2.526X_1+10.121X_2+88.027X_3+568.719X_4+\\ 684.245X_1{X}_1+1377.5X_1{X}_2-456.191X_1{X}_3-441.958X_2{X}_2\end{array}$$

(2)

$$\begin{array}{l}{Y}_3=-28.038+108.756X_1+44.921X_2+135.101X_3-155.312X_4\\ -331.966X_1{X}_1+1206.562X_1{X}_2-316.297X_1{X}_3-894.531X_1{X}_4\\ -230.958X_2{X}_2-24.083X_3{X}_3\end{array}$$

(3)

The analysis of variance of the abovementioned test results is shown in

Table 9. Analysis of variance of Y₁ regression model.

Source	Sum of Squares	Df	Mean Square	F-Value	p-Value	Significance
Model	381.75	14	27.27	3,053,960	<0.0001
X1	47.84	1	47.84	5,358,095	<0.0001
X2	60.71	1	60.71	6,798,961	<0.0001
X3	45.36	1	45.36	5,080,030	<0.0001
X4	21.28	1	21.28	2,383,364	<0.0001
X1X2	21.16	1	21.16	2,369,920	<0.0001
X1X3	131.45	1	131.45	14,721,977	<0.0001
X1X4	0.48	1	0.48	54,098.8	<0.0001
X2X3	0	1	0	0	1
X2X4	0.19	1	0.19	21,193.2	<0.0001
X3X4	0	1	0	0	1
X12	29.35	1	29.35	3,286,976	<0.0001
X22	13.56	1	13.56	1,518,672	<0.0001
X32	5.13	1	5.13	574,372.8	<0.0001
X42	0.16	1	0.16	18,116.88	<0.0001
Residual	0.00013	14	8.93 × 10−6
Lack of Fit	0.00013	10	1.25 × 10−5
Pure Error	0	4	0
Cor Total	381.745	28

,

Table 10. Analysis of variance of Y₂ regression model.

Source	Sum of Squares	Df	Mean Square	F-Value	p-Value	Significance
Model	4532.46	14	323.75	13.07	<0.0001
X1	710.56	1	710.56	28.68	0.0001
X2	137.84	1	137.84	5.56	0.0333
X3	570.91	1	570.91	23.05	0.0002
X4	759.70	1	759.70	30.67	<0.0001
X1X2	485.76	1	485.76	19.61	0.0005
X1X3	1524.90	1	1,524.90	61.56	<0.0001
X1X4	0.90	1	0.90	0.04	0.8513
X2X3	0.00	1	0.00	0	1
X2X4	9.64	1	9.64	0.39	0.5427
X3X4	0.00	1	0.00	1.01 × 10−6	0.9992
X12	124.39	1	124.39	5.02	0.0417
X22	126.70	1	126.70	5.11	0.0401
X32	7.01	1	7.01	0.28	0.6030
X42	16.99	1	16.99	0.69	0.4214
Residual	346.75	14	24.768
Lack of Fit	346.75	10	34.675
Pure Error	0.00	4	0.000
Cor Total	4879.21	28

and

Table 11. Analysis of variance of Y₃ regression model.

Source	Sum of Squares	Df	Mean Square	F-Value	p-Value	Significance
Model	9289.75	14	663.554	74.27	<0.0001
X1	3372.45	1	3,372.45	377.48	<0.0001
X2	4174.24	1	4,174.24	467.23	<0.0001
X3	196.02	1	196.02	21.94	0.0003
X4	32.21	1	32.21	3.61	0.0784
X1X2	372.68	1	372.68	41.71	<0.0001
X1X3	733.05	1	733.05	82.05	<0.0001
X1X4	32.77	1	32.77	3.67	0.0761
X2X3	0.00	1	0.00	0	1
X2X4	4.92	1	4.92	0.55	0.4699
X3X4	0.00	1	0.00	2.8 × 10−6	0.9986
X12	29.27	1	29.27	3.27	0.0917
X22	34.60	1	34.60	3.87	0.0692
X32	308.22	1	308.22	34.50	<0.0001
X42	9.32	1	9.32	1.04	0.3242
Residual	125.07	14	8.93
Lack of Fit	125.07	10	12.51
Pure Error	0.00	4	0.000
Cor Total	9414.82	28

. The P values of the regression models Y₁, Y₂, and Y₃ were all below 0.001, proving statistical significance of the model at 0.95 confidence interval. An analysis of the F- and P-values of each model showed that in the prediction model for Y₁, all linear, quadratic, and interaction terms were significant, with the exception of the interaction terms X₂X₃ and X₃X₄. The significance of the effects of the factors on the fine particle content in the UF decreased in the following order—vortex finder diameter (X₂) > inlet pressure (X₄) > vortex finder insertion depth (X₃) > apex diameter (X₁). In the prediction model for Y₂, all terms were significant, with the exception of the terms X₁X₄, X₂X₃, X₂X₄, X₃X₄, X₃², and X₄². The significance of the influences of factors on quality efficiency decreased in the following order—inlet pressure (X₄) > vortex finder insertion depth (X₃) > vortex finder diameter (X₂) > apex diameter (X₁). In the prediction model for Y₃, all terms were significant, with the exception of the terms X₂X₃, X₂X₄, X₃X₄, and X₄². The significance of influences of factors on quantity efficiency decreased in the following order—inlet pressure (X₄) > vortex finder insertion depth (X₃) > apex diameter (X₁) > vortex finder diameter (X₂).

The ultimate objective in using the W-shaped hydrocyclone was to improve the quantity efficiency by decreasing the fine particle misclassification in UF. Optimal parameter combination was obtained by considering the influence factors in conjunction with the interaction among the content of fine particles in UF, quantity efficiency, and quality efficiency. The optimal parameter configuration was as follows—an apex diameter of 0.14 D, a vortex finder diameter of 0.31 D, an insertion depth of 1.87 D, and an inlet pressure of 0.18 MPa. The corresponding optimal result was a C₋₂₅ in the UF of 11.92%, a quality efficiency of 42.48%, and a quantity efficiency of 98.99%.

4. Conclusions

In the current work, the influences of inlet pressure, vortex finder insertion depth, vortex finder diameter, and apex diameter on W-shaped hydrocyclone classification performance were studied experimentally. A mathematical model was established on the basis of the response surface method for the prediction of W-shaped hydrocyclone separation performance.

(1) With the increase of the diameter of vortex finder, the cut size increased, and the OF product and UF became coarser. At the same time, the quality efficiency gradually decreased, and the quantity efficiency gradually increased. Although increasing vortex finder insertion depth might decrease the fine particle content in UF and increase the quantity efficiency, excessively large insertion depths significantly reduced the quality efficiency, and the coarse particles were entrained in the OF. As the apex diameter increased, the content of fine particles in UF was enhanced and the cut size was reduced. With the increase of inlet pressure, the cut size decreased, quality efficiency was enhanced, and the quantity efficiency decreased.

(2) The significance of the effects of the factors on the content of fine particles in UF decreased in the following order—vortex finder diameter > inlet pressure > insertion depth of vortex finder > apex diameter. The significance of the influences of factors on the quality efficiency decreased in the following order—inlet pressure > vortex finder insertion depth > vortex finder diameter > apex diameter. The significance of the influences of factors on quantity efficiency decreased in the following order—inlet pressure > vortex finder insertion depth > apex diameter > vortex finder diameter.

(3) By considering all of these influence factors, the following optimal parameter configuration was obtained—an apex diameter of 0.14 D, a vortex finder diameter of 0.31 D, an insertion depth of 1.87 D, and an inlet pressure of 0.18 MPa. The corresponding optimal result was a C₋₂₅ in the UF of 11.92%, a quality efficiency of 42.48%, and a quantity efficiency of 98.99%.

It needs to be specially stated that this model was applicable to the W-shaped hydrocyclone studied in this study, but might not be applicable to other structural forms or very special working conditions.