1 Introduction

As a valuable raw material and an important fine chemical intermediate, phenol compounds are widely used in pesticide, medicine, dyestuff and spices industry, which have high economic value (Ge and Jin 1995; Xue et al. 1998; Li et al. 2005; Liu et al. 2012). Because coal tar contains significant amounts of phenol compounds, especially in middle and low temperature coal tar, the research on extraction phenol from coal tar posse significant economic benefits.

The study of extraction phenol from coal tar is mainly based on the properties of polarity and acid. The mature alkali wash method, which is widely used in industry, is based on the acid properties of phenol compounds. However, the alkali washing method has some obvious drawbacks, including easy emulsification, equipment corrosion problems and serious pollution (Liu and Qang 2001; Jia and Jia 2008; Ye et al. 2010; Wang et al. 2011). The solvent extraction method is based on the polarity property of phenol, which will be the developing direction of extraction phenol from coal tar, and it has many advantages, such as low price, nontoxic extraction agent, corrosion-free, moderate operation conditions, no waste water and no exhaust gas in the course of production (Tiwari and Sen 1991; Wu et al. 2001; Liu and Xie 2014). The extraction method has been used in industry (Zong et al. 2013), yet the most adopted solvent extraction equipment is the mixer-settler, which have obvious disadvantages of large liquid holdup, significant solvent loss, long mixing and refining time, large land occupied and only intermittent operation. In contrast, centrifugal extractor has many advantages, such as compact structure, high treatment capacity, low liquid holdup, high mass transfer effect, convenient for starting and stopping, remote automatic control (Leonard et al. 1997; Fu 2004; Li and Yuan 2007). With the above advantages, some chemical plants have begun to treat phenol waste water with the centrifugal extractor (Xu et al. 1999; Yu et al. 2001; Wang et al. 2001; Tang et al. 2012; Mishra et al. 2016).

However, there are little systematic research on extracting phenol from coal tar with centrifugal extractor. In order to get rid of the drawbacks of annulus centrifugal extractor, such as high energy consumption, complex structure and hard dismantling (Chen et al. 2009; Yuan et al. 2010; Wang 2014; Li et al. 2016), the extraction phenol from coal tar by new-type high flux centrifugal extractor were systematically studied in this paper.

2 Experimental

2.1 Structure and work principle of HCE

Structure of HCE is shown in Fig. 1.

Fig. 1
figure 1

Structure schematic drawing of HCE. a heavy phase weir, b heavy phase collecting chamber, c light phase outlet, d drum, e feed terminal, f mixer, g feed guide vane, h mixing chamber, i vortex guide vane, j feed inlet, k light phase collecting chamber, and l heavy phase outlet

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High flux centrifugal extractor is composed of housing, rotary drum and mixing chamber. The rotating shaft connects with the drum. The heavy phase weir is arranged on the top of drum, and can be directly replaced without removing the drum from extractor. The mixer is arranged at the bottom of drum, which is located in mixing chamber. Heavy and light phase collecting chamber are set up between drum and lining. The whole centrifuge is equipped with suspension structure, without bottom bearings and mechanical seals. So, the centrifuge is in the status of low power consumption and low failure rate. The device can control the particle size of the droplet through the special mixing blade, so as to avoid emulsification. The main parameter of centrifugal extractor: diameter of rotating drum: 50 mm, length of rotating drum: 140 mm, output frequency: 40 Hz, separating factor: 0–1000 and rated flux (two phase mixing flux): 0–20 L/h (Figs. 2, 3).

Fig. 2
figure 2

Chromatography of acidic components in the medium and low temperature coal tar

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Fig. 3
figure 3

Chromatography of neutral oils in the medium and low temperature coal tar

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Extraction agent and raw oil enter the extractor from both sides of the feed inlet as a quantitative flow. Two phases flowed into the mixing chamber under the influence of gravity, mixed thoroughly with mixer, then entered into the drum through feed terminal. Finally, mixed phase was separated in the drum by centrifugal force. Heavy phase was thrown to the wall of the drum, clusters into a group, and flowed out through heavy collecting chamber and outlet. On the contrary, light phase gathered in the central regions of the drum, and flowed out through light collecting chamber.

2.2 Experimental raw materials

Typical medium and low temperature coal tar was selected as experiment material. Firstly, 170–230 °C fraction was obtained via distillation under vacuum. Secondly, density of the fraction was measured under normal temperature, phenol compounds content in the fraction was determined by using the standardization method of “Determination of the phenol content of washing oil” GB/T24207–2009.

The acidic components in the raw material were concentrated by means of alkali washing and acid extraction, then were analyzed qualitatively and quantitatively by the gas chromatograph using external standard method. The experimental conditions were as follows: capillary chromatographic column model of DB Petro-122-10A6 (100.0 m × 0.25 mmID × 0.5 μmdf), FID detector, inlet temperature of 280 °C, detector temperature of 300 °C. Heating procedures were as follows: oven temperature stayed at 70 °C for 2 min, then increased up to 200 °C at a rate of 4 °C per minute, stayed for 4 min and finally increased up to 280 °C at a rate of 2 °C per minute.

The neutral oil components were enriched by alkali washing, then were qualitatively analyzed by gas chromatographic–mass spectrometer (GC–MS). The experimental conditions were as follows: inlet and detector temperature of 300 °C, interface temperature of 320 °C, ionization source of EI, electron energy of 70 eV, the ionization temperature of 240 °C. Heating procedures were as follows: oven temperature stayed at 70 °C for 5 min, then increased up to 170° at a rate of 4 °C per minute, stayed for 3 min and finally increased up to 280° at a rate of 2 °C per minute.

2.3 Analysis methods

The phenol compounds contents in raw oil and light phase are determined by the standardization method of “Determination of the phenol content of washing oil”. The mass transfer efficiency of centrifugal extractor (E as phenol extraction efficiency) is calculated with Formula (1):

$$E = \left( {\frac{{C_{\text{in}} - C_{\text{out}} }}{{C_{\text{in}} }}} \right) \times 100\%$$
(1)

where C in, C out are phenol mass content of raw oil and light phase respectively.

Extraction agent mass content of light phase is determined with the gas chromatograph using external standard method. The loss rate of extraction agent (E s) is calculated with Formula (2), thus the index is used as a basis for the judging entrainment phenomenon.

$$E_{\text{s}} = \left( {\frac{{m_{\text{o}} \times C_{\text{s}} }}{{m_{\text{s}} }}} \right) \times 100\%$$
(2)

where m s is the mass of extraction agent feed into HCE, m o and C s are the mass and extraction agent mass content of the light phase (Table 1).

Table 1 Qualitative and quantitative analysis of acidic components in the coal tar
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3 Results and discussion

3.1 Analysis of raw materials and development of composite extractant

The chromatogram of acidic components in the medium and low temperature coal tar was as follows:

Phenolic compounds were identified 73% of the total acidic components, of which phenol and cresol accounted for about 40.69%, ethyl phenol and dimethyl phenol accounted for 23.91%. In summary, the lower-grade phenols content was relatively high.

The retrieved main neutral oils were listed in Table 2. The mass spectra of neutral oils were shown in Fig. 4.

Table 2 Retrieval results of major neutral oil compound
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Fig. 4
figure 4

MS spectrum of major neutral oil compounds. a Mass spectrum of Indene. b Mass spectrum of Methyl indane. c Mass spectrum of Naphthalene. d Mass spectrum of Methylnaphthalene

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The analysis results showed that the neutral oils of coal tar extraction material were mainly single or double ring aromatic hydrocarbon, due to interactions of π–π bond between phenolic compounds and aromatic hydrocarbons, single extractant was difficult to ensure the high extraction rate of phenol in the condition of high selectivity, therefore composite and highly effective phenol extraction agent YH-3 needed to be developed. According to polarity character and hydrogen bond interaction of phenolic compounds, an alcohol solvent was selected as a base extractant, and a kind of alkane compound with a large group is added. The alkane compound could increase the steric hindrance between the benzene rings and weak the π–π interaction, thus the amount of neutral oil entrained was effectively reduced (Figs. 5, 6).

Fig. 5
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Chromatography of solvent extraction phenol. a Chromatography of single solvent extraction phenol. b Chromatography of composite solvent extraction phenol

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Fig. 6
figure 6

Influence of flow ratio on the mass transfer efficiency and loss rate of extraction agent

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The results of qualitative and quantitative analysis to extraction phenol showed that the effective enrichment of the lower phenol was achieved by extraction, especially for phenol and cresol. Under the condition of ensuring the extraction efficiency, the entrainment rate of naphthalene (retention time was 29.45 min) and α-methyl naphthalene (retention time was 34.20 min) was effectively decreased.

The value of HWD was set as 29.0 mm, according to the density and viscosity of raw oil and extraction agent. In this context, entrainment phenomenon was avoided by regulating the rotation speed.

3.2 Influence of flow ratio on the mass transfer efficiency and loss rate of extraction agent

The samples in each condition experiments were collected from heavy and light phase outlet after total transition flow reached 800 mL. The effects of flow ratio on the mass transfer efficiency and rate of extraction agent loss were investigated under the fixed conditions including 200 mL/min of total flow rate and 2400 r/min of rotation speed.

According to the above figure, when the volume ratio of solvent agent to feed was in the range of 0.6–2.6:1, the mass transfer efficiency was up to 80%, which increased firstly, then decreased with the increasing of flow ratio. Because the total phenol content in raw feed was high, all phenol could not be extracted completely, given that the feeding rate of solvent agent was low. However, the mass transfer efficiency decreased with the increasing of flow ratio, when the feed quantity of solvent agent was enough. The reason for the above phenomenon might be explained with the following description. A phase was dispersed in the form of liquid droplets in another in HCE equipment. The size of the interface area in per unit volume of mixed phase was determined by the average diameters of droplets and the holdup of dispersed phase. When other processing parameters were fixed, the holdup of dispersed phase and the interface area in per unit volume of mixed phase were both small under the condition of high volume ratio of solvent agent to feed. Furthermore, with the increasing of phase ratio, the result easily leaded to mix unevenly and decreased the interface area, thus mass transmission and mass transfer efficiency decreased due to the influence of limited phase contact time.

The rate of extraction agent loss showed the trend of increase, with the increasing of flow ratio of solvent agent to feed. When the flow ratio was more than 1.8, the loss rate was significantly increased. The increasing of flow ratio corresponded to the increasing of the solvent agent volume fraction in per unit volume. While the volume fraction of solvent agent was controlled within a rational range, light and heavy phase could be efficiently separated in a relatively short residence time, and the entrainment rate of solvent agent rates was ensured at a low level. When the volume fraction further increased, the amount of heavy phase increased correspondingly. The phase interface moved towards the device center, then light phase layer then enforced to be thinner, and flowed into the light phase overflow weir together with entrainment heavy phase easily. Consequently, the loss rate of solvent agent significantly increased. Overall, the optimum range of flow ratio was 1–1.4:1.

3.3 Influence of total flow rate on the mass transfer efficiency and loss rate of extraction agent

The effects of total flow rate on the mass transfer efficiency and loss rate of extraction agent were investigated under the fixed conditions including 1:1 of flow ratio and 2400 r/min of rotation speed.

Figure 7 showed that the mass transfer efficiency decreased gradually with the increasing of total flow rate of raw material and solvent agent. When total flow rate was more than 200 mL/min, the mass transfer efficiency was dramatically reduced. Once the flow rate was up to 320 mL/min, the mass transfer efficiency was less than 80%. The major reason for above phenomenon was two phase finite contact time. When valid volume of HCE was fixed, with the increasing of total flow rate, the average residence and mixing time of two phase in HCE became shorter. Meanwhile, when rotate speed was fixed, the total input power kept constant. When total flow rate was increasing, the input power of mixed phase in per unit volume decreased, the mixed-degree was obviously reduced. Accordingly, with the increasing of total flow rate, the mass transfer efficiency decreased.

Fig. 7
figure 7

Influence of total flow rate on the mass transfer efficiency and loss rate of extraction agent

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The rate of solvent agent loss showed a rising trend with the increasing of total flow rate. When the total flow rate was more than 240 mL/min, the loss rate was dramatically increased. The separation performance of HCE was attached to residence time. Given enough time, the process finished well, which the heavy phase moved towards the walls, and the light phase moves towards the center of HCE respectively. Under the condition of low total flow rate, the residence time was long enough to separate effectively, so the loss rate of extraction agent was small. On the contrary, the residence time became shorter with the increasing of total flow rate. The short residence time corresponded to short separation time. It aroused the deteriorating separation performance. Therefore, the smaller the total flow rate, the better the separation efficiency, the lower the loss rate of extraction agent. Ultimately, the optimum range of total flow rate was 160–240 mL/min (Figs. 8, 9).

Fig. 8
figure 8

Influence of rotation speed on the mass transfer efficiency and loss rate of extraction agent

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Fig. 9
figure 9

Work flow diagram of three stages counter current extraction. a high flux centrifugal extractor, b feed creeping pump, c light phase storage tank, d extractor agent storage tank, e raw oil storage tank, and f heavy phase storage tank

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3.4 Influence of rotation speed on the mass transfer efficiency and loss rate of extraction agent

The effects of rotation speed on the mass transfer efficiency and loss rate of extraction agent were investigated under the fixed conditions including 200 mL/min of total flow rate and 1:1 of flow ratio.

According to the above figure, under the conditions of fixed total flow rate and flow ratio, the effect of rotation speed on the mass transfer efficiency was investigated. The adjustment range of rotary speed was 1800–2800 r/min. With the increasing of rotary speed, the mass transfer efficiency showed the trend of first increase and then decrease. When the rotation speed achieved about 2400 r/min, the efficiency reached the maximum. Because the rotational speed was low, the input power was a little, and the mixing intensity was weak, accordingly, the mass transfer efficiency was low. With the increasing of speed, the separation factor of HCE increased, the efficiency was gradually increased. However, when the speed exceeded the certain level, intensified mixed caused the poor phase separation. If the speed further increased, noise increasing and vibration intensified caused the HCE to work abnormally.

As the rotation speed was gradually improved, the loss rate of extraction agent showed a trend of first decrease and then sudden increase. In the process of improving the rotating speed, the separation ability was strong and the loss rate was small. However, once the speed exceeded the certain level, it caused the complicated vortex and turbulent easily. It led to the emulsion between light and heavy phase, which prevented the droplets coalescence and separation of two phase. Above all, the optimum of rotation speed was 2200–2600 r/min.

3.5 Three stages counter current extraction experiment

Theoretical calculations and experiments showed that multistage counter current extracting process was superior to multistage cross current extracting process. Consequently, the test of extracting phenol from coal tar was carried out with the three stages counter current extraction (Table 3).

Table 3 Physical property parameter of raw oil and extraction agent
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Raw oil and extraction agent entered into the centrifugal unit through the inlet at each end, then mixed thoroughly and separated efficiently, at the end, two phases flowed out from the unit through overflow vent respectively. In the whole process, extraction agent did not have to be added gradually, hence the amount of extraction agent was quite small. The three stages counter current tests were carried out at the operation condition of 29 mm of HWD, 1:1 of the flow ratio, 200 mL/min of the total flow rate and 2400 r/min of the rotation speed.

The experiment results were demonstrated in Table 4. The mass transfer efficiency of three stages counter current test raised from 84.5% to 92.6%. In the same extraction agent amount, the performance of three stages counter current test was much better than that of single stage extracting tests. However, the rate of extraction agent loss increased from 0.26% to 0.42% with increasing of extraction degree.

Table 4 Results of three stages counter current and single stage extraction experiment
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4 Conclusions

  1. (1)

    Phenolic compounds were identified with 73% of the total acidic components in medium and low temperature coal tar, in which the lower-grade phenols content accounted for more than 50%. The main factors affecting the purity of the extracted phenolic compounds were single or double ring aromatic hydrocarbon, such as indene, naphthalene, methylnaphthalene et al. Under the premise of high phenol extraction rate, composite YH-3 extraction agent reduces π–π interaction between phenolic compounds and aromatic hydrocarbons, thus decreasing the entrainment of neutral oil.

  2. (2)

    The HCE was used in the experiment of solvent extraction phenol from coal tar. The effects of phase ratio, total flow rate and rotation speed on the process should be taken into consideration. Once one of factors exceeded the reasonable range, two-phase entrainment rate would increase dramatically, and noise increasing or intensified vibration will result in the abnormal state of the HCE. In conclusion, the optimization of operation conditions was necessary. The single stage extraction tests were carried out at 29 mm of HWD, 1:1–1.4:1 of the flow ratio range, 160–200 mL/min of the total flow rate range, 2200–2600 r/min of the rotation speed range. At compatible conditions, the mass transfer efficiency was higher than 84%, and the loss-extraction agent rate was lower than 0.28%.

  3. (3)

    Three stages counter current test showed that the mass transfer efficiency was higher than 92.6%, under the optimum conditions such as HWD 29 mm, the flow ratio 1:1, the total flow rate 200 mL/min and the rotation speed 2400 r/min. The rate of extraction agent loss was a little more than the single stage test, however, the integral process fully met the requirements of industrial production. Overall, phenol in coal tar could be extracted effectively by taking YH-3 as extraction agent, in the process of multistage continuous count current centrifugal extraction.