Process and equipment for rapidly enriching light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar

Abstract

The invention provides a process and equipment for rapidly enriching light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar, which are characterized in that five solvent storage tanks are used for storing recovered solvents (acetone, carbon disulfide, petroleum ether, methanol and acetonitrile) in each step, so that the recovered solvents can be recycled in cycles; carrying out deliming treatment on the medium-low temperature coal tar by using an acetone / carbon disulfide mixed solvent; petroleum ether and methanol, petroleum ether and acetonitrile, and methanol and carbon disulfide are used for carrying out step-by-step double-solvent layered extraction on the de-ashed tar. The method provided by the invention realizes rapid enrichment of target components in medium-low temperature coal tar, provides extract oil which is simple in composition and easy to process for subsequent secondary upgrading, and solves the problems of high energy consumption, difficulty in large-scale commercialization and the like in the prior art.

Description

Technical Field

[0001] The invention relates to the technical field of coal chemical industry, and in particular to a process and equipment for rapidly enriching light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium- and low-temperature coal tar. Background Art

[0002] Medium and low temperature coal tar is a by-product of the production process of coal-to-coke. It is mainly composed of aliphatic hydrocarbons, aromatic hydrocarbons, phenols and asphaltene, and also contains a small amount of nitrogen / sulfur species and C=O compounds, such as aldehydes, ketones, carboxylic acids, esters, etc. The rich valuable group components make medium and low temperature coal tar an important chemical raw material for obtaining various fine chemicals. However, some undesirable characteristics, such as high moisture and ash content, high viscosity, and highly complex composition, increase the difficulty and cost of extracting value-added downstream products from it. The limitation of the traditional distillation method commonly used to split according to boiling point is that the composition of each fraction is still highly complex, and the interweaving or entrainment of group components makes it impossible to select a scientific and reasonable quality improvement plan in a targeted manner. At present, non-selective catalytic hydrogenation refining is mostly used to convert it into refined oil for composition splitting and sale. Sales volume is greatly affected by fluctuations in the fuel oil market, and the economic benefits need to be improved. Therefore, it is necessary to develop a reasonable rapid enrichment process technology to effectively separate the group components according to the composition distribution characteristics, and then select a suitable quality improvement processing plan based on the composition differences of each enriched oil, in order to significantly improve the value-added utilization level of medium and low temperature coal tar and improve economic benefits.

[0003] In current technology, medium and low temperature coal tar is mainly separated and processed by the following methods:

[0004] The first method is the distillation process technology that splits the fractions according to the difference in boiling points. Various tar fractions in different temperature ranges are obtained, and their intrinsic properties depend on the difference in boiling points of each fraction. Therefore, the composition of the derivative oil obtained by this process technology still mainly includes the above-mentioned various family components. Since there are overlapping boiling points between the various family components, the complexity of the composition is related to the entrainment between the various species during the distillation process. In other words, the secondary quality improvement processing of these tar fractions is still difficult. In addition, the boiling range of medium and low temperature coal tar is relatively wide, and the temperature range for full component splitting is from room temperature to 500°C. The high energy consumption and the undesirable phenomena such as coking that are easy to occur during high-temperature operation make this strategy need to be optimized. The current model has certain disadvantages and is not conducive to the refined utilization of medium and low temperature coal tar.

[0005] The second method is an extraction process technology that separates the components according to the solubility differences of different compounds. Various types of extracted oils with different distributions of components are obtained, and their intrinsic properties depend on the extraction characteristics of the solvent used. This process technology often uses low-boiling point, easily recyclable organic solvents, such as petroleum ether, n-heptane, methanol, ethanol, carbon disulfide, acetone, ethyl acetate, acetonitrile, dichloromethane, etc. The obtained extracted oil is subjected to normal pressure / medium pressure / high pressure column chromatography, combined with mobile phase modulation to achieve enrichment and purification of various types of components. On the one hand, this process usually uses a single solvent extraction (single pass or step by step), and the strong interaction between the components of the components leads to a decrease in the proportion of the target component and the loss of valuable compounds, and the extraction selectivity needs to be improved; on the other hand, the lengthy processing flow results in low processing efficiency and a single form of the product that can be obtained, which makes large-scale production difficult.

[0006] Therefore, it is particularly urgent to develop a process technology and related equipment that can not only efficiently separate light hydrocarbon oil, medium hydrocarbon oil and crude phenol from medium and low temperature coal tar, but also make full use of these components. This new process technology not only needs to achieve rapid enrichment of target components in medium and low temperature coal tar, and provide simple and easy-to-process extracted oil for subsequent secondary quality improvement, but also solve the problems of high energy consumption and difficulty in large-scale commercialization of existing technologies, enrich medium and low temperature coal tar derivatives in a green, environmentally friendly, economical and efficient way, and enhance its value-added utilization space. Summary of the invention

[0007] To solve the above-mentioned defects, the present invention provides a process and equipment for rapid enrichment of light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar. The present invention realizes the rapid enrichment of target components in medium and low temperature coal tar, provides an extracted oil with simple composition and easy processing for subsequent secondary quality improvement, and solves the problems of high energy consumption and difficulty in large-scale commercialization in the prior art.

[0008] In a first aspect, the present invention provides a rapid enrichment process for light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium-low temperature coal tar, which comprises: 1) placing the medium-low temperature coal tar as a raw material in a No. 1 extraction kettle (1), and conveying a mixed solvent of acetone and carbon disulfide to the No. 1 extraction kettle (1), extracting and separating into a solid phase and a liquid phase, and the liquid phase flows into a No. 1 distillation kettle (2), and distilling the solvent in the No. 1 distillation kettle (2) to obtain deashing tar; 2) conveying the deashing tar to a No. 2 extraction kettle (3), using petroleum ether and methanol for layered extraction, and waiting for the upper phase of petroleum ether and the lower phase of methanol, the upper phase of petroleum ether is conveyed to a No. 3 extraction kettle (4), adding acetonitrile to the No. 3 extraction kettle (4), and standing for layering to obtain a petroleum ether phase, a acetonitrile phase; the lower phase methanol is transported to the fourth extraction kettle (5), carbon disulfide is added to the fourth extraction kettle (5), and the mixture is allowed to stand for separation to obtain a methanol phase and a carbon disulfide phase; 3) the acetonitrile phase is transported to the second distillation kettle (6), and the solvent is evaporated in the second distillation kettle (6) to obtain a medium hydrocarbon oil acetonitrile soluble matter; the petroleum ether phase is transported to the third distillation kettle (7), and the solvent is evaporated in the third distillation kettle (7) to obtain a light hydrocarbon oil petroleum ether soluble matter; the carbon disulfide phase is transported to the fourth distillation kettle (8), and the solvent is evaporated in the fourth distillation kettle (8) to obtain a medium hydrocarbon oil carbon disulfide soluble matter; the methanol phase is transported to the fifth distillation kettle (9), and the solvent is evaporated in the fifth distillation kettle (9) to obtain a crude phenol methanol soluble matter.

[0009] Preferably, in step 1), the volume ratio of acetone to carbon disulfide is (0.8-1.2):1, the extraction temperature is room temperature, the extraction time is 10-30 min, and the extraction method is single-pass extraction.

[0010] Preferably, in step 2), the standing time for stratification is 10-30 min.

[0011] Preferably, step 2) is a group component separation process of medium and low temperature coal tar;

[0012] Preferably, in step 2), the volume ratio of petroleum ether to methanol in the second extraction kettle (3) is (1-3): 1;

[0013] Preferably, in step 2), the volume ratio of petroleum ether to acetonitrile in the third extraction kettle (4) is (1-3): 1;

[0014] Preferably, in step 2), the volume ratio of methanol to carbon disulfide in the fourth extraction kettle (5) is (1-3):1.

[0015] Preferably, in step 1) and step 3), the first distillation kettle (2), the second distillation kettle (6), the third distillation kettle (7), the fourth distillation kettle (8) and the fifth distillation kettle (9) are all heated to the boiling point of the corresponding solvent to recover the solvent;

[0016] Preferably, in step 1) and step 2), acetone, carbon disulfide, methanol and acetonitrile are all analytically pure; petroleum ether is selected with a boiling range of 60-90°C;

[0017] Preferably, in step 1) and step 3), the evaporated solvent enters storage tanks for recycling.

[0018] In a second aspect, the present invention provides a rapid enrichment device for light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium-low temperature coal tar, comprising: a No. 1 extraction kettle (1), a No. 1 distillation kettle (2), a No. 2 extraction kettle (3), a No. 3 extraction kettle (4), a No. 4 extraction kettle (5), a No. 2 distillation kettle (6), a No. 3 distillation kettle (7), a No. 4 distillation kettle (8), a No. 5 distillation kettle (9), a No. 1 storage tank (10), a No. 2 storage tank (11), a No. 3 storage tank (12), a No. 4 storage tank (13), a No. 5 storage tank (14), a No. 6 storage tank (15), a No. 7 storage tank (16), a No. 8 storage tank (17), a No. 9 storage tank (18), a No. 10 storage tank (19), a No. 11 storage tank (20), a No. 12 storage tank (21), a No. 13 storage tank (22), a No. 14 storage tank (23), a No. 15 storage tank (24), a No. 16 storage tank (25), a No. 17 storage tank (26), a No. 18 storage tank (27), a No. 19 storage tank (28), a No. 20 storage tank (29), a No. 21 storage tank (30), a No. 21 storage tank (31), a No. 21 storage tank (32), a No. 21 storage tank (33), a No. 21 storage tank (34), a No. 21 The top of the No. 1 extraction kettle (1) is connected to the No. 4 storage tank (13) and the No. 5 storage tank (14) through pipelines, and the bottom of the No. 1 extraction kettle (1) is connected to the No. 1 distillation kettle (2) through a pipeline; the top of the No. 1 distillation kettle (2) is connected to the horizontal tube heat exchanger (39) through a pipeline, and the bottom of the No. 1 distillation kettle (2) is connected to the No. 2 extraction kettle (3) through a pipeline; the top of the No. 2 extraction kettle (3) is connected to the No. 2 distillation kettle (2) through a pipeline. The storage tank (11) and the third storage tank (12) are connected to each other through pipelines, the bottom of the second extraction kettle (3) is connected to the third extraction kettle (4) and the fourth extraction kettle (5) through pipelines; the top of the third extraction kettle (4) is connected to the first storage tank (10) through a pipeline, the bottom of the third extraction kettle (4) is connected to the second distillation kettle (6) and the third distillation kettle (7) through a pipeline; the top of the fourth extraction kettle (5) is connected to the fifth storage tank (14) through a pipeline, and the top of the fourth extraction kettle (5) is connected to the fifth storage tank (15) through a pipeline. The bottom is connected to the No. 4 distillation kettle (8) and the No. 5 distillation kettle (9) through pipelines; the tops of the No. 2 distillation kettle (6), the No. 3 distillation kettle (7), the No. 4 distillation kettle (8), and the No. 5 distillation kettle (9) are respectively connected to the horizontal shell and tube heat exchanger (39), the horizontal shell and tube heat exchanger (39) is connected to the buffer tank (15), and the buffer tank (15) is respectively connected to the No. 1 storage tank (10), the No. 2 storage tank (11), the No. 3 storage tank (12), the No. 4 storage tank (13), and the No. 5 storage tank (14).

[0019] Preferably, the first extraction kettle (1) is provided with a magnetic stirring device (19), a coarse filter plate (84) and a fine filter plate (85), the upper part of the first extraction kettle (1) is provided with a feeding trough (28) and a pressure gauge (30), and the lower part of the first extraction kettle (1) is provided with a discharge trough (29).

[0020] Preferably, the second extraction kettle (3), the third extraction kettle (4) and the fourth extraction kettle (5) are all provided with a magnetic stirring device and an observation window for observing the extraction liquid level, and the upper parts of the second extraction kettle (3), the third extraction kettle (4) and the fourth extraction kettle (5) are all provided with a pressure gauge.

[0021] Preferably, the No. 1 distillation kettle (2), the No. 2 distillation kettle (6), the No. 3 distillation kettle (7), the No. 4 distillation kettle (8) and the No. 5 distillation kettle (9) are all provided with matching heating devices and magnetic stirring devices, and the No. 1 distillation kettle (2), the No. 2 distillation kettle (6), the No. 3 distillation kettle (7), the No. 4 distillation kettle (8) and the No. 5 distillation kettle (9) are all provided with pressure gauges on their upper parts.

[0022] Preferably, the valve pipeline of the horizontal shell-and-tube heat exchanger (39) is connected to the buffer tank (15) via an oil pump (17).

[0023] In summary, the present invention provides a process and equipment for rapidly enriching light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar. The beneficial effects of the present invention are:

[0024] Due to the adoption of the above scheme, acetone, carbon disulfide, petroleum ether, methanol and acetonitrile with boiling points below 100°C are used as extractants, which is conducive to the recycling of solvents after rapid enrichment. Compared with traditional high-boiling point single solvent extraction, the combination of low-boiling point dual solvents is more flexible and diverse, and has lower toxicity, and can adapt to a variety of substrates or a variety of complex extraction scenarios; the extraction operation is carried out at room temperature, which significantly reduces energy consumption, and no three wastes are generated, which can effectively avoid environmental pollution; 4 types of dual solvent systems are combined with 5 kinds of extractants and applied to the extraction of medium and low temperature coal tar. Only three steps are required to obtain three types of valuable secondary oil products, namely light hydrocarbon oil (aliphatic hydrocarbons), medium hydrocarbon oil (aromatic hydrocarbons) and crude phenol (phenols), with high extraction efficiency. While effectively separating out valuable family components, it enriches the types of secondary oil products and improves the complexity of oil product composition, thereby reducing the difficulty and cost of subsequent secondary quality improvement. Among them, light hydrocarbon oil is rich in aliphatic hydrocarbons, which can be distilled into downstream products such as naphtha, gasoline / diesel, paraffin, etc.; medium hydrocarbon oil is rich in aromatic hydrocarbons, and can be obtained by extraction / distillation / column chromatography / recrystallization to obtain the corresponding pure products, or by catalytic hydrogenation to obtain alkylcycloalkanes, which can then be used to prepare high-density liquid fuels; crude phenol is rich in various phenol monomers, which can be obtained by extraction / distillation / column chromatography / recrystallization to obtain the corresponding pure products, or by selective hydrogenation to obtain alkylcycloalkanols, which can then be used in medicine, agriculture, forestry, animal husbandry and other fields. Ash can be used in adsorption materials or combustion power generation. This process has the characteristics of being green and mild, no three wastes discharged, short production cycle, easy continuous production, and high product added value. The combination of extractants can be flexibly adjusted according to the distribution characteristics of oil components to obtain various value-added oil products in a targeted manner. It is an innovative process path for efficient utilization of medium and low temperature coal tar.

[0025] The present invention obtains three types of secondary oil products, including light hydrocarbon oil, medium hydrocarbon oil and crude phenol. Downstream products such as naphtha, gasoline / diesel, and paraffin can be obtained from light hydrocarbon oil; fine chemicals such as alkylbenzene, alkylnaphthalene, alkylanthracene / phenanthrene can be obtained from medium hydrocarbon oil, and alkylcycloalkanes can be obtained through catalytic hydrogenation and refining, which can then be used to prepare high-density liquid fuels; fine chemicals such as phenol, alkylphenol, alkoxyphenol can be obtained from crude phenol, and alkylcycloalkanols can be obtained through selective hydrogenation. These downstream products can be widely used in the fields of energy, chemical industry, medicine, agriculture, forestry, and animal husbandry. The flexible and changeable oil properties and multiple downstream conversion pathways indicate that the process technology has good effects on the treatment of medium and low temperature coal tar and has the potential for future promotion.

[0026] The process of the present invention is simple to operate, has mild conditions, and is green, environmentally friendly, economical, efficient, low energy consumption, and has a short production cycle. Through the intelligent control platform, different components can be separated rationally and directionally according to the differences in the properties of different oil products, effectively improving production efficiency and product diversity. BRIEF DESCRIPTION OF THE DRAWINGS

[0027] Figure 1 This is a flow chart of the rapid enrichment process of light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar provided in Example 1.

[0028] Figure 2 This is a schematic diagram of the structure of the equipment for rapidly enriching light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar provided in Example 1.

[0029] Main element symbol description:

[0030] 1. Extraction kettle No. 1; 2. Distillation kettle No. 1; 3. Extraction kettle No. 2; 4. Extraction kettle No. 3; 5. Extraction kettle No. 4; 6. Distillation kettle No. 2; 7. Distillation kettle No. 3; 8. Distillation kettle No. 4; 9. Distillation kettle No. 5; 10. Storage tank No. 1; 11. Storage tank No. 2; 12. Storage tank No. 3; 13. Storage tank No. 4; 14. Storage tank No. 5; 15. Buffer tank; 16. Air compressor pump No. 1; 17. Buffer tank oil pump; 18. Air compressor pump No. 2; 19. Magnetic stirring device for extraction kettle No. 1; 20. Magnetic stirring device for distillation kettle No. 1; 21. Magnetic stirring device for extraction kettle No. 2; 22. Magnetic stirring device for extraction kettle No. 3; 23. Magnetic stirring device for No. 4 extraction kettle; 24. Magnetic stirring device for No. 2 distillation kettle; 25. Magnetic stirring device for No. 3 distillation kettle; 26. Magnetic stirring device for No. 4 distillation kettle; 27. Magnetic stirring device for No. 5 distillation kettle; 28. Feeding trough for extraction kettle; 29. ​​Discharging trough for extraction kettle; 30. Pressure gauge for No. 1 extraction kettle; 31. Pressure gauge for No. 1 distillation kettle; 32. Pressure gauge for No. 2 extraction kettle; 33. Pressure gauge for No. 3 extraction kettle; 34. Pressure gauge for No. 4 extraction kettle; 35. Pressure gauge for No. 2 distillation kettle; 36. Pressure gauge for No. 3 distillation kettle; 37. Pressure gauge for No. 4 distillation kettle; 38. Pressure gauge for No. 5 distillation kettle; 39. Horizontal tube exchange Heater; 40, control platform; 41, one valve; 42, two valves; 43, three valves; 44, four valves; 45, five valves; 46, six valves; 47, seven valves; 48, eight valves; 49, nine valves; 50, ten valves; 51, eleven valves; 52, twelve valves; 53, thirteen valves; 54, fourteen valves; 55, fifteen valves; 56, sixteen valves; 57, seventeen valves; 58, eighteen valves; 59, nineteen valves; 60, twenty valves; 61, twenty-one valves; 62, twenty-two valves; 63, twenty-three valves; 64, twenty-four valves; 65, twenty-five valves; 66, two Sixteen valves; 67, twenty-seven valves; 68, twenty-eight valves; 69, twenty-nine valves; 70, thirty valves; 71, thirty-one valves; 72, three-way valve No. 1; 73, three-way valve No. 2; 74, three-way valve No. 3; 75, three-way valve No. 4; 76, three-way valve No. 5; 77, three-way valve No. 6; 78, three-way valve No. 7; 79, three-way valve No. 8; 80, three-way valve No. 9; 81, three-way valve No. 10; 82, three-way valve No. 11; 83, three-way valve No. 12; 84, coarse filter sleeve; 85, fine filter plate; 86, observation window of extraction kettle No. 2; 87, observation window of extraction kettle No. 3; 88, observation window of extraction kettle No. 4. DETAILED DESCRIPTION

[0031] Combined with Figure 1 The process flow and attached Figure 2 The following embodiments are provided in detail to illustrate the present invention in detail.

[0032] The separation process proposed in the present invention is not limited to medium and low temperature coal tar. The technicians can easily understand the purpose of the present invention and extend and apply the present invention to the quality improvement of other chemical raw materials, including petroleum, heavy oil, oil sludge, tar residue, organic waste liquid and other types of chemical organic waste liquid, etc. However, as long as it does not deviate from the spirit of the present invention, it is within the protection scope of the present invention.

[0033] Example 1

[0034] A rapid enrichment process for light hydrocarbon oil, medium hydrocarbon oil and crude phenol in low-temperature coal tar, which uses five solvent storage tanks to store and access the recovered solvents (acetone, carbon disulfide, petroleum ether, methanol, acetonitrile) in each step so as to be recycled over and over again; uses acetone / carbon disulfide mixed solvent to deash the medium and low-temperature coal tar; uses petroleum ether and methanol, petroleum ether and acetonitrile, methanol and carbon disulfide to perform step-by-step double solvent layered extraction on the deashed tar. Figure 1 As shown, the specific steps are as follows:

[0035] Step 1: placing the raw material of medium-low temperature coal tar in the No. 1 extraction kettle 1 through the extraction kettle feeding tank 28, and conveying the mixed solvent of acetone and carbon disulfide to the No. 1 extraction kettle 1 in a volume ratio of 1:1, deashing the medium-low temperature coal tar to obtain ash residue; distilling off the solvent in the No. 1 distillation kettle 2 to obtain deashed tar;

[0036] Step 2: conveying the deashed tar to the second extraction kettle 3, using petroleum ether and methanol for layered extraction, obtaining an upper phase (petroleum ether) which is conveyed to the third extraction kettle 4, and a lower phase (methanol) which is conveyed to the fourth extraction kettle 5; using petroleum ether and acetonitrile, methanol and carbon disulfide in the third extraction kettle 4 and the fourth extraction kettle 5, respectively, to perform layered extraction to obtain a petroleum ether phase, an acetonitrile phase, a methanol phase and a carbon disulfide phase;

[0037] Step three: conveying the acetonitrile phase to the No. 2 distillation kettle 6, and distilling off the solvent in the No. 2 distillation kettle 6 to obtain medium hydrocarbon oil (acetonitrile solubles); conveying the petroleum ether phase to the No. 3 distillation kettle 7, and distilling off the solvent in the No. 3 distillation kettle 7 to obtain light hydrocarbon oil (petroleum ether solubles); conveying the carbon disulfide phase to the No. 4 distillation kettle 8, and distilling off the solvent in the No. 4 distillation kettle 8 to obtain medium hydrocarbon oil (carbon disulfide solubles); conveying the methanol phase to the No. 5 distillation kettle 9, and distilling off the solvent in the No. 5 distillation kettle 9 to obtain crude phenol (methanol solubles).

[0038] In the step 1:

[0039] Step 1-1: adding low-temperature coal tar in the raw material into the first extraction kettle 1 through the extraction kettle feeding tank 28, and closing the six valves 46 of the extraction kettle feeding tank 28;

[0040] Step 1-2: Open the upper and lower passages of the four valves 44, the five valves 45 and the six three-way valve 77. Transfer equal volumes of acetone stored in the fourth storage tank 13 and carbon disulfide stored in the fifth storage tank 14 to the first extraction kettle 1. Close the upper and lower passages of the four valves 44, the five valves 45 and the six three-way valve 77;

[0041] Step 1-3: Operate the control platform 40 of the first extraction kettle 1, start the magnetic stirring program, and stir for 10-30 minutes. Use the coarse filter sleeve 84 and the fine filter plate 85 to separate the solid and liquid phases. The solid phase is ash and the liquid phase is a mixture of soluble matter and solvent;

[0042] Step 1-4: The liquid phase flows into the first distillation kettle 2 through the eighth valve 48. When no liquid passes through, the eighth valve 48 is closed. The seventh valve 47 is opened, the ash (solid phase) is taken out from the extraction kettle discharge trough 29, and the seventh valve 47 is closed;

[0043] Step 1-5: Operate the control platform 40 of the No. 1 distillation kettle 2, start the heating and magnetic stirring program, and stir at the set temperature (the boiling point of carbon disulfide). Open the left and right passages of the No. 10 valve 50 and the No. 7 three-way valve 78, and start the horizontal shell and tube heat exchanger 39. Use the buffer tank oil pump 17 to transport the condensed and recovered carbon disulfide solvent to the buffer tank 15;

[0044] Step 1-6: Observe the liquid level of the buffer tank 15, open the 31st valve 71 and the lower right passage of the No. 5 three-way valve 76. Use the No. 2 air compressor pump 18 to transport the condensed and recovered carbon disulfide solvent to the No. 5 storage tank 14 for storage and standby use. When no recovered solvent flows out, close the 31st valve 71 and the lower right passage of the No. 5 three-way valve 76;

[0045] Step 1-7: operate the control platform 40 of the first distillation reactor 2 to raise the temperature to near the boiling point of acetone. Use the buffer tank oil pump 17 to transport the condensed and recovered acetone solvent to the buffer tank 15;

[0046] Step 1-8: Observe the liquid level of the buffer tank 15, open the 31st valve 71 and the lower right passage of the No. 4 three-way valve 75 and the left and right passages of the No. 5 three-way valve 76. Use the No. 2 air compressor pump 18 to transport the condensed and recovered acetone solvent to the No. 4 storage tank 13 for storage and standby use. When no recovered solvent flows out, close the 31st valve 71, the lower right passage of the No. 4 three-way valve 75 and the left and right passages of the No. 5 three-way valve 76;

[0047] Step 1-9: operate the control platform 40 of the No. 1 distillation kettle 2, turn off the heating and magnetic stirring programs, turn off the horizontal shell and tube heat exchanger 39, and close the left and right passages of the No. 10 valve 50 and the No. 7 three-way valve 78. At this time, the remaining material in the No. 1 distillation kettle 2 is deashing tar.

[0048] In the step 2:

[0049] Step 2-1: Open the upper and lower passages of the eleventh valve 51 and the eight-way valve 79, and transfer the deashed tar in the first distillation kettle 2 to the second extraction kettle 3, and then close the upper and lower passages of the eleventh valve 51 and the eight-way valve 79. Open the second valve 42, the third valve 43 and the left lower passage of the eight-way valve 79, and transfer the methanol stored in the second storage tank 11 and the petroleum ether in the third storage tank 12 to the second extraction kettle 3 according to a certain volume ratio (petroleum ether / methanol=3 / 1, 2 / 1 or 1 / 1), and close the second valve 42, the third valve 43 and the left lower passage of the eight-way valve 79;

[0050] Step 2-2: operate the control platform 40 of the second extraction kettle 3, start the magnetic stirring program, and stir for 10-30 minutes at room temperature. After completion, operate the control platform 40 of the second extraction kettle 3, turn off the magnetic stirring program, and let it stand for 10-30 minutes until the liquid phase separates;

[0051] Step 2-3: Open the sixteenth valve 56 and the eighteenth valve 58, monitor the liquid level in the second extraction kettle 3 through the observation window 86 of the second extraction kettle, transfer the lower phase (methanol) in the second extraction kettle 3 to the fourth extraction kettle 5, and close the sixteenth valve 56 and the eighteenth valve 58;

[0052] Step 2-4: Open the fourteenth valve 54 and the sixteenth valve 56, monitor the liquid level in the second extraction kettle 3 through the observation window 86 of the second extraction kettle, transfer the upper phase (petroleum ether) in the second extraction kettle 3 to the third extraction kettle 4, and finally close the fourteenth valve 54 and the sixteenth valve 56;

[0053] Step 2-5: Open the first valve 41 and the thirteenth valve 53, and transfer the acetonitrile stored in the first storage tank 10 to the third extraction kettle 4 according to a certain volume ratio (petroleum ether / acetonitrile=3 / 1, 2 / 1 or 1 / 1), and then close the first valve 41 and the thirteenth valve 53;

[0054] Step 2-6: Open the 19th valve 59 and the upper right passage of the No. 6 three-way valve 77, and transfer the carbon disulfide stored in the No. 5 storage tank 14 to the extraction kettle 5 according to a certain volume ratio (methanol / carbon disulfide=3 / 1, 2 / 1 or 1 / 1), and then close the 19th valve 59 and the upper right passage of the No. 6 three-way valve 77;

[0055] Step 2-7: Operate the control platform 40 of the No. 3 extraction kettle 4 and the No. 4 extraction kettle 5 to start the magnetic stirring program and extract for 10-30 minutes at room temperature. After the extraction, operate the control platform 40 of the No. 3 extraction kettle 4 and the No. 4 extraction kettle 5 to turn off the magnetic stirring program and let it stand for 10-30 minutes until the liquid phase separates;

[0056] Step 2-8: Open the upper left passage of the No. 20 valve 60 and the No. 9 three-way valve 80, monitor the liquid level in the No. 3 extraction kettle 4 through the No. 3 extraction kettle observation window 87, and use the No. 1 air compression pump 16 to transport the lower phase (acetonitrile) in the No. 3 extraction kettle 4 to the No. 2 distillation kettle 6 for storage and standby use;

[0057] Step 2-9: close the upper left passage of the No. 9 three-way valve 80, open the left and right passages of the No. 9 three-way valve 80 and the upper left passage of the No. 10 three-way valve 81, and use the No. 1 air compression pump 16 to transport the upper phase (petroleum ether) in the No. 3 extraction kettle 4 to the No. 3 distillation kettle 7 for storage and standby use;

[0058] Step 2-10: close the twenty valves 60 and the upper left passage of the No. 10 three-way valve 81, open the twenty-one valves 61, the left and right passages of the No. 10 three-way valve 81 and the upper left passage of the No. 11 three-way valve 82, monitor the liquid level in the No. 4 extraction kettle 5 through the No. 4 extraction kettle observation window 88, and use the No. 1 air compression pump 16 to transport the lower phase (carbon disulfide) in the No. 4 extraction kettle 5 to the No. 4 distillation kettle 8 for storage and standby use;

[0059] Step 2-11: Close the upper left passage of the eleventh three-way valve 82, open the left and right passages of the eleventh three-way valve 82 and the upper left passage of the twelveth three-way valve 83, use the first air compressor pump 16 to transport the upper phase (methanol) in the fourth extraction kettle 5 to the fifth distillation kettle 9 for storage, close the twenty-first valve 61 and the upper left passage of the twelveth three-way valve 83. Open the left and right passages of the twelveth three-way valve 83, vent the pipeline, and then close the nineth three-way valve 80, the tenth three-way valve 81, the eleventh three-way valve 82, and the twelveth three-way valve 83.

[0060] In the step three:

[0061] Step 3-1: operate the control platform 40 of the No. 2 distillation kettle 6, start the heating and magnetic stirring program, stir at the set temperature (acetonitrile boiling point), open the twenty-two valves 62 and the lower right passage of the No. 7 three-way valve 78, start the horizontal shell-and-tube heat exchanger 39, use the buffer tank oil pump 17 to transport the condensed acetonitrile solvent to the buffer tank 15, observe the liquid level of the buffer tank 15, open the thirty-one valves 71, the lower right passage of the No. 1 three-way valve 72 and the left and right passages of the No. 2 three-way valve 73, the No. 3 three-way valve 74, the No. 4 three-way valve 75, and the No. 5 three-way valve 76, and use the No. 2 air compression pump 18 to transport the recovered acetonitrile solvent to the No. 1 storage tank 10 for storage and standby use;

[0062] Step 3-2: When no recovered solvent flows out, close the horizontal shell-and-tube heat exchanger 39, close the twenty-two valves 62 and the thirty-one valves 71, close the No. 1 three-way valve 72 and the right lower passage of the No. 7 three-way valve 78, close the No. 2 three-way valve 73, the No. 3 three-way valve 74, the No. 4 three-way valve 75, and the left and right passages of the No. 5 three-way valve 76. At this time, the remaining substance in the No. 2 distillation kettle 6 is medium hydrocarbon oil;

[0063] Step 3-3: operate the control platform 40 of the No. 3 distillation kettle 7, start the heating and magnetic stirring program, stir at the set temperature (boiling point of petroleum ether), open the twenty-three valves 63 and the lower right passage of the No. 7 three-way valve 78, start the horizontal shell-and-tube heat exchanger 39, use the buffer tank oil pump 17 to transport the condensed petroleum ether solvent to the buffer tank 15, observe the liquid level of the buffer tank 15, open the thirty-one valves 71, the lower right passage of the No. 3 three-way valve 74 and the left and right passages of the No. 4 three-way valve 75 and the No. 5 three-way valve 76, and use the No. 2 air compression pump 18 to transport the recovered petroleum ether solvent to the No. 3 storage tank 12 for storage and standby use;

[0064] Step 3-4: When no recovered solvent flows out, close the horizontal shell-and-tube heat exchanger 39, close the twenty-three valves 63 and the thirty-one valves 71, close the right lower passage of the No. 3 three-way valve 74 and the No. 7 three-way valve 78, and close the left and right passages of the No. 4 three-way valve 75 and the No. 5 three-way valve 76. At this time, the remaining substance in the No. 3 distillation kettle 7 is light hydrocarbon oil;

[0065] Step 3-5: operate the control platform 40 of the No. 4 distillation kettle 8, start the heating and magnetic stirring program, stir at the set temperature (boiling point of carbon disulfide), open the 24th valve 64 and the lower right passage of the No. 7 three-way valve 78, start the horizontal shell and tube heat exchanger 39, use the buffer tank oil pump 17 to transport the condensed carbon disulfide solvent to the buffer tank 15, observe the liquid level of the buffer tank 15, open the 31st valve 71 and the lower right passage of the No. 5 three-way valve 76, and use the No. 2 air compression pump 18 to transport the recovered carbon disulfide solvent to the No. 5 storage tank 14 for storage and standby use;

[0066] Step 3-6: When no recovered solvent flows out, close the horizontal tube-and-tube heat exchanger 39, close the twenty-four valves 64 and the thirty-one valves 71, close the right lower passages of the No. 5 three-way valve 76 and the No. 7 three-way valve 78, and at this time, the remaining substance in the No. 4 distillation kettle 8 is medium hydrocarbon oil;

[0067] Step 3-7: operate the control platform 40 of the No. 5 distillation kettle 9, start the heating and magnetic stirring program, stir at the set temperature (methanol boiling point), open the twenty-five valves 65 and the lower right passage of the No. 7 three-way valve 78, start the horizontal shell and tube heat exchanger 39, use the buffer tank oil pump 17 to transport the condensed methanol solvent to the buffer tank 15, observe the liquid level of the buffer tank 15, open the thirty-one valves 71, the lower right passage of the No. 2 three-way valve 73 and the left and right passages of the No. 3 three-way valve 74, the No. 4 three-way valve 75, and the No. 5 three-way valve 76, and use the No. 2 air compression pump 18 to transport the recovered methanol solvent to the No. 2 storage tank 11 for storage and standby use;

[0068] Step 3-8: When no recovered solvent flows out, close the horizontal shell-and-tube heat exchanger 39, close the twenty-five valves 65 and the thirty-one valves 71, close the right lower passages of the No. 2 three-way valve 73 and the No. 7 three-way valve 78, and close the left and right passages of the No. 3 three-way valve 74, the No. 4 three-way valve 75 and the No. 5 three-way valve 76. At this time, the remaining substance in the No. 5 distillation kettle 9 is crude phenol;

[0069] Step 3-9: Open the twenty-seventh valve 67 to obtain light hydrocarbon oil, open the twenty-sixth valve 66 and the twenty-eighth valve 68 to obtain medium hydrocarbon oil, and open the twenty-nineth valve 69 to obtain crude phenol. Finally, close the twenty-sixth valve 66, the twenty-seventh valve 67, the twenty-eighth valve 68, and the twenty-nineth valve 69.

[0070] The compositions of light hydrocarbon oil, medium hydrocarbon oil and crude phenol were obtained by gas chromatography / mass spectrometry analysis. The compositions of light hydrocarbon oil, medium hydrocarbon oil and crude phenol are shown in Table 1.

[0071] Table 1

[0072]

[0073] Example 2

[0074] like Figure 2As shown, a rapid enrichment device for light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium-low temperature coal tar comprises: an extraction kettle No. 1, a distillation kettle No. 1, a distillation kettle No. 2, a extraction kettle No. 3, a extraction kettle No. 3, a extraction kettle No. 4, a distillation kettle No. 5, a distillation kettle No. 2, a distillation kettle No. 6, a distillation kettle No. 3, a distillation kettle No. 4, a distillation kettle No. 5, a storage tank No. 10, a storage tank No. 2, a storage tank No. 11, a storage tank No. 3, a storage tank No. 4, a storage tank No. 5, a buffer tank 15 and a horizontal tube-and-buffer heat exchanger 39. The top of the extraction kettle No. 1 is connected to the storage tank No. 4 and the storage tank No. 5 by pipelines, respectively, and the bottom of the extraction kettle No. 1 is connected to the distillation kettle No. 2 by pipelines; the top of the distillation kettle No. 2 is connected to the horizontal tube-and-buffer heat exchanger 39 by pipelines, and the bottom of the distillation kettle No. 1 is connected to the extraction kettle No. 3 by pipelines; the top of the extraction kettle No. 2 is connected to the storage tank No. 2 11, No. 3 storage tank 12 are connected respectively by pipelines, the bottom of No. 2 extraction kettle 3 is connected to No. 3 extraction kettle 4 and No. 4 extraction kettle 5 by pipelines; the top of No. 3 extraction kettle 4 is connected to No. 1 storage tank 10 by pipeline, and the bottom of No. 3 extraction kettle 4 is connected to No. 2 distillation kettle 6 and No. 3 distillation kettle 7 by pipeline; the top of No. 4 extraction kettle 5 is connected to No. 5 storage tank 14 by pipeline, and the bottom of No. 4 extraction kettle 5 is connected to No. 4 distillation kettle 8 and No. 5 distillation kettle 9 by pipeline; the tops of No. 2 distillation kettle 6, No. 3 distillation kettle 7, No. 4 distillation kettle 8 and No. 5 distillation kettle 9 are respectively connected to horizontal shell and tube heat exchanger 39, the horizontal shell and tube heat exchanger 39 is connected to buffer tank 15, and buffer tank 15 is respectively connected to No. 1 storage tank 10, No. 2 storage tank 11, No. 3 storage tank 12, No. 4 storage tank 13 and No. 5 storage tank 14.

[0075] The top of the No. 1 extraction kettle 1 is provided with an extraction kettle feeding tank 28 with six valves 46, a No. 1 extraction kettle pressure gauge 30 and a No. 1 extraction kettle magnetic stirring device 19. The top of the No. 1 extraction kettle 1 is connected to the No. 4 storage tank 13 and the No. 5 storage tank 14 through the four valves 44, the five valves 45, the No. 6 three-way valve 77 and related pipelines; the inner layer of the No. 1 extraction kettle 1 is provided with a coarse filter sleeve 84 and a fine filter plate 85. The side of the No. 1 extraction kettle 1 is connected to the external control platform 40, and the bottom is provided with an extraction kettle discharge tank 29 connected to the seven valves 47, and is connected to the top of the No. 1 distillation kettle 2 through the eight valves 48 and related pipelines;

[0076] The upper part of the No. 1 distillation kettle 2 is provided with a No. 1 distillation kettle magnetic stirring device 20, a No. 1 distillation kettle pressure gauge 31 and a vent connected with a nine-valve 49; the upper part of the No. 1 distillation kettle 2 is connected to the left part of the horizontal shell-and-tube heat exchanger 39 through ten valves 50, seven three-way valves 78 and related pipelines; the outer layer of the No. 1 distillation kettle 2 is a distillation kettle heating device and is connected to the external control platform 40 on the side; the lower part of the No. 1 distillation kettle 2 is connected to the upper part of the No. 2 extraction kettle 3 through eleven valves 51, eight three-way valves 79 and related pipelines;

[0077] The upper part of the No. 2 extraction kettle 3 is provided with a No. 2 extraction kettle magnetic stirring device 21, a No. 2 extraction kettle pressure gauge 32 and a vent connected with twelve valves 52; the upper part of the No. 2 extraction kettle 3 is connected with the No. 2 storage tank 11 and the No. 3 storage tank 12 through two valves 42, three valves 43, eight three-way valves 79 and related pipelines; the No. 2 extraction kettle 3 is provided with a No. 2 extraction kettle observation window 86 on the side, and is connected to the external control platform 40; the lower part of the No. 2 extraction kettle 3 is connected with the upper parts of the No. 3 extraction kettle 4 and the No. 4 extraction kettle 5 through fourteen valves 54, sixteen valves 56 and eighteen valves 58;

[0078] The top of the No. 3 extraction kettle 4 is provided with a No. 3 extraction kettle magnetic stirring device 22, a No. 3 extraction kettle pressure gauge 33 and a vent connected to fifteen valves 55; the top of the No. 3 extraction kettle 4 is connected to the No. 1 storage tank 10 through a valve 41, thirteen valves 53 and related pipelines; the side of the No. 3 extraction kettle 4 is provided with a No. 3 extraction kettle observation window 87, and is connected to the external control platform 40; the bottom of the No. 3 extraction kettle 4 is connected to the related valve pipelines of the air compression pump 16 through twenty valves 60;

[0079] The No. 4 extraction kettle 5 is provided with a No. 4 extraction kettle magnetic stirring device 23, a No. 4 extraction kettle pressure gauge 34 and a vent connected to a seventeen-valve 57 on the top; the No. 4 extraction kettle 5 is connected to the No. 5 storage tank 14 through a nineteen-valve 59, a No. 6 three-way valve 77 and related pipelines; the No. 4 extraction kettle 5 is provided with a No. 4 extraction kettle observation window 88 on the side thereof, and is connected to an external control platform 40; the No. 4 extraction kettle 5 is connected to the related valve pipelines of the No. 1 air compression pump 16 through a twenty-one valve 61 on the bottom thereof;

[0080] The No. 2 distillation kettle 6 is provided with a No. 2 distillation kettle magnetic stirring device 24 and a No. 2 distillation kettle pressure gauge 35 on the upper part; the No. 2 distillation kettle 6 is connected to the left part of the horizontal tube heat exchanger 39 through a No. 22 valve 62, a No. 7 three-way valve 78 and related pipelines, and the upper inlet pipeline is connected to the related valve pipeline of the No. 1 air compression pump 16 through a No. 9 three-way valve 80; the outer layer of the No. 2 distillation kettle 6 is a distillation kettle heating device and is connected to the external control platform 40 on the side; the No. 2 distillation kettle 6 is provided with a discharge port connected by a No. 26 valve 66 at the bottom;

[0081] The top of the No. 3 distillation kettle 7 is provided with a No. 3 distillation kettle magnetic stirring device 25 and a No. 3 distillation kettle pressure gauge 36; the top of the No. 3 distillation kettle 7 is connected to the left part of the horizontal tube-in-tube heat exchanger 39 through a No. 23 valve 63, a No. 7 three-way valve 78 and related pipelines, and the upper inlet pipeline is connected to the related valve pipeline of the No. 1 air compression pump 16 through a No. 10 three-way valve 81; the outer layer of the No. 3 distillation kettle 7 is a distillation kettle heating device and is connected to the external control platform 40 on the side; the bottom is provided with a discharge port connected through a No. 27 valve 67;

[0082] The No. 4 distillation kettle 8 is provided with a No. 4 distillation kettle magnetic stirring device 26 and a No. 4 distillation kettle pressure gauge 37 on the top; the No. 4 distillation kettle 8 is connected to the left part of the horizontal shell-and-tube heat exchanger 39 through a 24-valve 64, a No. 7 three-way valve 78 and related pipelines, and the upper inlet pipeline is connected to the related valve pipeline of the No. 1 air compression pump 16 through a No. 11 three-way valve 82; the outer layer of the No. 4 distillation kettle 8 is a distillation kettle heating device and is connected to the external control platform 40 on the side; the No. 4 distillation kettle 8 is provided with a discharge port connected to a 28-valve 68 at the bottom;

[0083] The No. 5 distillation kettle 9 is provided with a No. 5 distillation kettle magnetic stirring device 27 and a No. 5 distillation kettle pressure gauge 38 on the upper part; the No. 5 distillation kettle 9 is connected to the left part of the horizontal tube heat exchanger 39 through a No. 25 valve 65, a No. 7 three-way valve 78 and related pipelines, and the upper inlet pipeline is connected to the related valve pipeline of the No. 1 air compression pump 16 through a No. 12 three-way valve 83; the outer layer of the No. 5 distillation kettle 9 is a distillation kettle heating device and is connected to the external control platform 40 on the side; the bottom of the No. 5 distillation kettle 9 is provided with a discharge port connected to a No. 29 valve 69;

[0084] The right side of the horizontal tube heat exchanger 39 is connected to the top of the buffer tank 15 through the buffer tank oil pump 17; the bottom of the buffer tank 15 is connected to the related valve pipeline of the No. 1 air compression pump 16 through the thirty-one valves 71 and related pipelines;

[0085] The upper part of the No. 1 storage tank 10 is connected to the No. 2 air compression pump 18 through a valve pipeline with a No. 1 three-way valve 72; the upper part of the No. 2 storage tank 11 is connected to the No. 2 air compression pump 18 through a valve pipeline with a No. 2 three-way valve 73; the upper part of the No. 3 storage tank 12 is connected to the No. 2 air compression pump 18 through a valve pipeline with a No. 3 three-way valve 74; the upper part of the No. 4 storage tank 13 is connected to the No. 2 air compression pump 18 through a valve pipeline with a No. 4 three-way valve 75; the upper part of the No. 5 storage tank 14 is connected to the No. 2 air compression pump 18 through a valve pipeline with a No. 5 three-way valve 76.

[0086] The above are only preferred embodiments of the present invention and are not intended to limit the present invention. For those skilled in the art, the present invention may have various modifications and variations. Any modification, equivalent replacement, improvement, etc. made within the spirit and principle of the present invention shall be included in the protection scope of the present invention.

Claims

1. A rapid enrichment process for light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar, characterized in that: It includes: 1) placing low-temperature coal tar in the raw material into a No. 1 extraction kettle (1), and conveying a mixed solvent of acetone and carbon disulfide into the No. 1 extraction kettle (1), extracting and separating into a solid phase and a liquid phase, and the liquid phase flows into a No. 1 distillation kettle (2), and the solvent is distilled in the No. 1 distillation kettle (2) to obtain deashed tar; 2) The deashed tar is conveyed to the second extraction kettle (3), and petroleum ether and methanol are used for layered extraction, and the upper phase of petroleum ether and the lower phase of methanol are obtained. The upper phase of petroleum ether is conveyed to the third extraction kettle (4), acetonitrile is added to the third extraction kettle (4), and the layers are allowed to stand to separate to obtain a petroleum ether phase and an acetonitrile phase; the lower phase of methanol is conveyed to the fourth extraction kettle (5), carbon disulfide is added to the fourth extraction kettle (5), and the layers are allowed to stand to separate to obtain a methanol phase and a carbon disulfide phase; 3) The acetonitrile phase is transported to the No. 2 distillation kettle (6), and the solvent is evaporated in the No. 2 distillation kettle (6) to obtain medium hydrocarbon oil acetonitrile solubles; the petroleum ether phase is transported to the No. 3 distillation kettle (7), and the solvent is evaporated in the No. 3 distillation kettle (7) to obtain light hydrocarbon oil petroleum ether solubles; the carbon disulfide phase is transported to the No. 4 distillation kettle (8), and the solvent is evaporated in the No. 4 distillation kettle (8) to obtain medium hydrocarbon oil carbon disulfide solubles; the methanol phase is transported to the No. 5 distillation kettle (9), and the solvent is evaporated in the No. 5 distillation kettle (9) to obtain crude phenol methanol solubles.

2. The rapid enrichment process of light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar according to claim 1, characterized in that: In step 1), the volume ratio of acetone to carbon disulfide is (0.8-1.2):1, the extraction temperature is room temperature, the extraction time is 10-30 minutes, and the extraction method is single-pass extraction.

3. The rapid enrichment process for light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar according to claim 1, characterized in that: In step 2), the standing time for stratification is 10-30 minutes.

4. The rapid enrichment process for light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar according to claim 1, characterized in that: Step 2) is to separate and process the group components of the medium and low temperature coal tar; In step 2), the volume ratio of petroleum ether to methanol in the second extraction kettle (3) is (1-3): 1; In step 2), the volume ratio of petroleum ether to acetonitrile in the third extraction kettle (4) is (1-3): 1; In step 2), the volume ratio of methanol to carbon disulfide in the fourth extraction kettle (5) is (1-3):

1.

5. The rapid enrichment process of light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar according to claim 1, characterized in that: In step 1) and step 3), the first distillation kettle (2), the second distillation kettle (6), the third distillation kettle (7), the fourth distillation kettle (8) and the fifth distillation kettle (9) are all heated to the boiling point of the corresponding solvent to recover the solvent; In step 1) and step 2), acetone, carbon disulfide, methanol and acetonitrile are all analytically pure; petroleum ether is selected with a boiling range of 60-90°C; In step 1) and step 3), the evaporated solvents enter storage tanks for recycling.

6. Rapid enrichment equipment for light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar, characterized in that: It includes: No. An extraction kettle (1), a first distillation kettle (2), a second extraction kettle (3), a third extraction kettle (4), a fourth extraction kettle (5), a second distillation kettle (6), a third distillation kettle (7), a fourth distillation kettle (8), a fifth distillation kettle (9), a first storage tank (10), a second storage tank (11), a third storage tank (12), a fourth storage tank (13), a fifth storage tank (14), a buffer tank (15) and a horizontal shell-and-tube heat exchanger (39); the top of the first extraction kettle (1) is connected to the fourth storage tank (13) and the fifth storage tank (14) respectively through pipelines, and the bottom of the first extraction kettle (1) is connected to the first distillation kettle (2) through a pipeline; The top of the No. 1 distillation kettle (2) is connected to the horizontal shell-and-tube heat exchanger (39) through a pipeline, and the bottom of the No. 1 distillation kettle (2) is connected to the No. 2 extraction kettle (3) through a pipeline; The top of the second extraction kettle (3) is connected to the second storage tank (11) and the third storage tank (12) through pipelines, and the bottom of the second extraction kettle (3) is connected to the third extraction kettle (4) and the fourth extraction kettle (5) through pipelines; The top of the No. 3 extraction kettle (4) is connected to the No. 1 storage tank (10) through a pipeline, and the bottom of the No. 3 extraction kettle (4) is connected to the No. 2 distillation kettle (6) and the No. 3 distillation kettle (7) through a pipeline; The top of the No. 4 extraction kettle (5) is connected to the No. 5 storage tank (14) through a pipeline, and the bottom of the No. 4 extraction kettle (5) is connected to the No. 4 distillation kettle (8) and the No. 5 distillation kettle (9) through pipelines; The tops of the No. 2 distillation kettle (6), the No. 3 distillation kettle (7), the No. 4 distillation kettle (8), and the No. 5 distillation kettle (9) are respectively connected to the horizontal shell and tube heat exchanger (39), the horizontal shell and tube heat exchanger (39) is connected to the buffer tank (15), and the buffer tank (15) is respectively connected to the No. 1 storage tank (10), the No. 2 storage tank (11), the No. 3 storage tank (12), the No. 4 storage tank (13), and the No. 5 storage tank (14).

7. The rapid enrichment equipment for light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar according to claim 6, characterized in that: The first extraction kettle (1) is provided with a magnetic stirring device (19), a coarse filter plate (84) and a fine filter plate (85), the upper part of the first extraction kettle (1) is provided with a feeding trough (28) and a pressure gauge (30), and the lower part of the first extraction kettle (1) is provided with a discharge trough (29).

8. The rapid enrichment equipment for light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar according to claim 6, characterized in that: The second extraction kettle (3), the third extraction kettle (4) and the fourth extraction kettle (5) are all provided with a magnetic stirring device and an observation window for observing the extraction liquid level, and the upper parts of the second extraction kettle (3), the third extraction kettle (4) and the fourth extraction kettle (5) are all provided with a pressure gauge.

9. The rapid enrichment equipment for light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar according to claim 6, characterized in that: The first distillation kettle (2), the second distillation kettle (6), the third distillation kettle (7), the fourth distillation kettle (8) and the fifth distillation kettle (9) are all provided with matching heating devices and magnetic stirring devices, and the tops of the first distillation kettle (2), the second distillation kettle (6), the third distillation kettle (7), the fourth distillation kettle (8) and the fifth distillation kettle (9) are all provided with pressure gauges.

10. The rapid enrichment equipment for light hydrocarbon oil, medium hydrocarbon oil and crude phenol in medium and low temperature coal tar according to claim 6, characterized in that: The valve pipeline of the horizontal shell-and-tube heat exchanger (39) is connected to the buffer tank (15) through an oil pump (17).

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