Device and method for measuring yield of coal pyrolysis tar

Abstract

The invention relates to the field of coal processing and utilization, and discloses a coal pyrolysis tar yield measuring device and method.The measuring device comprises a reactor, a feeding assembly, a purging gas pipeline, a fluidizing gas pipeline, a gas-solid separator and a condensation filtering assembly, the fluidized gas pipeline is arranged to provide fluidized gas to the reactor to form a constant-temperature reaction area, the height of the constant-temperature reaction area is 10-20 cm, the feeding assembly is arranged to convey pulverized coal to the reactor through the feeding pipeline, the purging gas pipeline is arranged to provide purging gas to the feeding pipeline, and the purging gas pipeline is arranged to supply purging gas to the reactor. The gas-solid separator is configured to separate a gaseous product from a solid product. According to the technical scheme, the height of the constant-temperature reaction area formed by the fluidized heat carrier particles is reasonably designed, so that pulverized coal can be subjected to pyrolytic reaction more quickly, secondary cracking or condensation polymerization of tar is avoided or reduced, and the yield of the tar is increased.

Description

Technical Field

[0001] This invention relates to the technical field of coal processing and utilization, specifically to a device for measuring the yield of coal pyrolysis tar, and also to a method for measuring the yield of coal pyrolysis tar. Background Technology

[0002] Pulverized coal can produce pyrolysis gas, tar, pyrolysis water and pulverized coke after pyrolysis. Among these, measuring the yield of tar produced by coal pyrolysis can help assess the chemical value of coal resources themselves and guide their efficient and clean conversion.

[0003] Currently, the determination of coal low-temperature pyrolysis products mainly relies on the Gerkin low-temperature carbonization test method and the aluminum pot low-temperature carbonization test method. However, in these two methods, the coal heating rate is slow, the tar residence time in the reaction zone is too long, and some tar will undergo secondary cracking or condensation reaction, which fails to maximize the tar yield and leads to a large deviation in the measurement results. Summary of the Invention

[0004] The purpose of this invention is to overcome the problem of low tar yield in coal pyrolysis in existing technologies.

[0005] To achieve the above objectives, the present invention provides an apparatus for measuring the yield of coal pyrolysis tar, comprising a reactor internally containing heat carrier particles, a feed assembly connected to the reactor via a feed pipe, a purge gas pipe connected to the feed pipe, a fluidizing gas pipe connected to the reactor, a gas-solid separator connected to the reactor, and a condenser-filter assembly connected to the gas-solid separator. The fluidizing gas pipe is configured to supply fluidizing gas to the reactor to form a constant-temperature reaction zone in the reactor in which the heat carrier particles are distributed in a fluidized state. The height of the constant-temperature reaction zone is 10-20 cm. The feed assembly is configured to feed pulverized coal to the reactor via the feed pipe. The purge gas pipe is configured to supply purge gas to the feed pipe to allow the pulverized coal to enter the reactor. The gas-solid separator is configured to separate gaseous and solid products from the reactor. The condenser-filter assembly is configured to condense and filter tar and pyrolysis water from the gaseous products.

[0006] In some embodiments, the heat carrier particles are quartz sand particles with a particle size of 0.1~0.5mm.

[0007] In some embodiments, the inner diameter of the reactor is 20-30 mm; and / or, the reactor is provided with a sieve plate to support the quartz sand particles; and / or, the reactor contains 5-10 g of the quartz sand particles.

[0008] In some embodiments, the gas-solid separator is a cyclone separator, which includes a straight cylindrical section and a conical section. The inner diameter of the straight cylindrical section is 5-10 cm and the height is 3-5 cm, and the height of the conical section is 5-10 cm.

[0009] In some embodiments, the system further includes a heating furnace for housing and heating the reactor, an insulation box for housing and heating the gas-solid separator, and a coke collection container connected to the bottom of the gas-solid separator.

[0010] In some embodiments, the condensation filter assembly includes a collection tube, degreased cotton disposed in the collection tube, and a condensation jacket sleeved outside the collection tube, wherein the inner diameter of the collection tube is 20-50 mm, the length is 10-20 cm, and the filling amount of the degreased cotton is 2-5 g.

[0011] In some embodiments, the feeding assembly includes a screw feeder and a hopper connected to the feed inlet of the screw feeder, and the discharge outlet of the screw feeder is connected to the reactor via the feed pipeline.

[0012] In some embodiments, a thermocouple for detecting the temperature of the isothermal reaction zone is also included.

[0013] On the other hand, the present invention also provides a method for determining the yield of coal pyrolysis tar, wherein the apparatus for determining the yield of coal pyrolysis tar using the above scheme includes: S1, load m1 mass of pulverized coal into the feeding assembly, turn on the condensation and filtration assembly to the predetermined condensation temperature, and heat the reactor to the predetermined temperature; S2, open the purge gas pipeline and the fluidizing gas pipeline so that the constant temperature reaction zone reaches the pyrolysis temperature; S3, the feeding assembly is turned on to allow pulverized coal to enter the reactor, and after a first predetermined time, the feeding assembly is turned off; S4, after the second predetermined time, stop heating the reactor, and after the reactor cools down, shut down the fluidizing gas pipeline and the purging gas pipeline, and shut down the condenser filter assembly; S5, Weigh the remaining coal powder m2 in the feeding assembly; S6, Measure the amount of tar collected in the condensation filter assembly; S7, calculate tar yield.

[0014] In some embodiments, the condensation filter assembly includes a collection tube, degreased cotton disposed in the collection tube, and a condensation jacket sleeved outside the collection tube; S1 includes: weighing the mass m3 of the collection tube; S6 includes: removing and weighing the mass m4 of the collection tube, taking out the degreased cotton, adding it to the azeotropic solvent, distilling out the pyrolysis water and part of the azeotropic solvent by distillation and collecting it by condensation, letting the collected liquid stand and separating it, weighing the mass m5 of the pyrolysis water, and the mass of the tar is m4-m3-m5.

[0015] In some embodiments, the condensation temperature of the condensation jacket is set to 0 to -20°C.

[0016] In some embodiments, the feeding assembly includes a screw feeder and a hopper connected to the feed inlet of the screw feeder, and the outlet end of the screw feeder is connected to the reactor via a feed pipe; S1 includes: loading 10-30g of coal powder with a particle size of less than 0.3mm into the silo; S3 includes: the feeding speed of the screw feeder is 0.5~2g / min.

[0017] In some embodiments, the purge gas and the fluidizing gas are nitrogen, hydrogen, methane, or a mixture of the three, the gas velocity of the fluidizing gas is 0.5~1.5 L / min, and the gas velocity of the purge gas is 0.5~1.5 L / min.

[0018] In some embodiments, in S2, the temperature of the isothermal reaction zone is 550~700℃.

[0019] In some embodiments, the measuring apparatus includes a heating furnace for housing and heating the reactor, and an insulated box for housing and heating the gas-solid separator. S1 includes: turning on the heating furnace and the insulation box, wherein the predetermined insulation temperature of the insulation box is 250~450℃; S4 includes: shutting down the heating furnace and the insulation box.

[0020] By using the above technical solutions and rationally designing the height of the isothermal reaction zone formed by the fluidized heat carrier particles, the pulverized coal can complete the pyrolysis reaction more quickly, avoiding or reducing secondary cracking or condensation reactions of tar and improving the tar yield. Attached Figure Description

[0021] Figure 1 This is a schematic diagram of the structure of the coal pyrolysis tar yield measuring device according to an embodiment of the present invention.

[0022] Explanation of reference numerals in the attached figures 1-Hopper, 2-Screw feeder, 3-Reactor, 4-Gas-solid separator, 5-Powdered coke collection container, 6-Condensing jacket, 7-Collection pipe, 8-Insulation box, 9-Heating furnace, 10-Thermocouple, 11-Feeding pipeline, 12-Purge gas pipeline, 13-Fluidizing gas pipeline, 14-Sieve plate, 15-First pipeline, 16-Second pipeline. Detailed Implementation

[0023] The specific embodiments of the present invention will be described in detail below with reference to the accompanying drawings. It should be understood that the specific embodiments described herein are for illustration and explanation only and are not intended to limit the present invention.

[0024] refer to Figure 1 As shown, the present invention provides an apparatus for determining the yield of coal pyrolysis tar, comprising a reactor 3 with internal heat carrier particles, a feed assembly connected to the reactor 3 via a feed pipe 11, a purge gas pipe 13 connected to the feed pipe 11, a fluidizing gas pipe 12 connected to the reactor 3, a gas-solid separator 4 connected to the reactor 3, and a condenser filter assembly connected to the gas-solid separator 4. The fluidizing gas pipe 12 is configured to supply fluidizing gas to the reactor 3 to form a fluidizing gas in the reactor 3. The reactor 3 is a constant-temperature reaction zone containing fluidized heat carrier particles, the height of which is 10-20 cm. The feeding assembly is configured to feed pulverized coal into the reactor 3 through the feeding pipeline 11. The purge gas pipeline 13 is configured to provide purge gas into the feeding pipeline 11 so that the pulverized coal enters the reactor 3. The gas-solid separator 4 is configured to separate the gaseous and solid products from the reactor 3. The condensation and filtration assembly is configured to condense and filter tar and pyrolysis water from the gaseous products.

[0025] Reactor 3 can be heated so that the heat carrier particles therein reach a higher temperature. Fluidizing gas pipeline 12 delivers fluidizing gas to reactor 3, so that the heat carrier particles are fluidized. The area in reactor 3 in which the fluidized heat carrier particles are distributed forms an isothermal reaction zone.

[0026] The feeding assembly is used to transport pulverized coal into reactor 3. A purge gas pipeline 13 is connected to the feed pipeline 11, through which purge gas can be supplied to the feed pipeline 11, thereby driving the pulverized coal in the feed pipeline 11 to flow into reactor 3. Under the action of the purge gas and fluidizing gas, the pulverized coal enters the isothermal reaction zone and comes into contact with the heat carrier particles. The heat energy carried by the heat carrier particles is transferred to the pulverized coal, causing the pulverized coal to quickly reach the pyrolysis temperature for the pyrolysis reaction.

[0027] Among them, the purging gas allows the pulverized coal to enter the reactor 3 more quickly and mix evenly with the heat carrier particles.

[0028] In addition, the fluidizing gas pipeline 12 can be connected to the lower part or bottom of the reactor 3, and the feed pipeline 11 can be connected to the lower part of the constant temperature reaction zone of the reactor 3. The coal powder (and pyrolysis products) entering the reactor 3 through the feed pipeline 11 flow upward from the lower part of the constant temperature reaction zone through the constant temperature reaction zone.

[0029] The height of the isothermal reaction zone is 10-20 cm. The height of the isothermal reaction zone is an important factor affecting the residence time of pulverized coal in reactor 3. The fluidized heat carrier particles in the isothermal reaction zone will generate resistance to the upward flow of pulverized coal (and pyrolysis products). Therefore, the height of the isothermal reaction zone needs to be maintained within a suitable range. On the one hand, it provides sufficient heat energy for the pyrolysis of pulverized coal, and on the other hand, it reduces the resistance to pulverized coal (and pyrolysis products), ensuring that reactants and products can flow quickly through reactor 3 (especially the isothermal reaction zone), thereby avoiding or reducing secondary cracking or condensation reactions of tar and improving the yield of tar.

[0030] Pulverized coal pyrolysis produces pyrolysis gas, tar, water vapor, and pulverized coke, including both gaseous and liquid products. The products flow upwards and enter a gas-solid separator 4 through a first pipe 15 connected to the top of reactor 3. The gas-solid separator 4 separates the gaseous and liquid products. The gaseous products then enter a condenser-filter assembly through a second pipe 16 connected to the gas-solid separator 4. The condenser-filter assembly condenses the tar and water vapor, collecting the condensed tar and water vapor through filtration, while the pyrolysis gas is discharged.

[0031] The yield of tar produced by coal pyrolysis can be calculated by measuring the mass of tar collected by the condensation component and referring to the mass of coal powder entering reactor 3 for pyrolysis.

[0032] In this scheme, by rationally designing the height of the isothermal reaction zone formed by fluidized heat carrier particles, the pulverized coal can complete the pyrolysis reaction more quickly, avoiding or reducing secondary cracking or condensation reactions of tar, and improving the tar yield.

[0033] In some embodiments, the heat carrier particles are quartz sand particles with a particle size of 0.1-0.5 mm. Quartz sand has a high specific heat, allowing it to carry more thermal energy and heat the coal powder it contacts more quickly. The particle size of the quartz sand can be 0.2-0.25 mm, 0.15-0.2 mm, etc. In this embodiment, the fluidized quartz sand particles form a isothermal reaction zone of a predetermined height, enabling the coal powder entering reactor 3 to complete the pyrolysis reaction and leave reactor 3 within 3-10 seconds. In other embodiments, the heat carrier particles can also be ceramic powder, zirconium oxide powder, etc., with a particle size of 0.1-0.5 mm; that is, the particle size of the heat carrier particles can be 0.1-0.5 mm.

[0034] In some embodiments, the reactor 3 has an inner diameter of 25-30 mm; and / or, the reactor 3 is provided with a sieve plate 14 to support the quartz sand particles; and / or, the reactor 3 contains 5-10 g of quartz sand particles. The reactor 3 is generally a vertically extending tubular structure with an inner diameter of 20-30 mm. The sieve plate 14 is a plate-like structure with small holes, which is disposed in the reactor 3. The inner diameter of the holes in the sieve plate 14 is smaller than the particle size of the quartz sand particles to support them. The quartz sand particles detach from the sieve plate 14 under the action of fluidizing gas and become fluidized. The mass of the quartz sand particles in the reactor 3 can be determined according to the inner diameter of the reactor 3 to ensure that the height of the isothermal reaction zone meets the requirements after the quartz sand particles are fluidized.

[0035] In some embodiments, the gas-solid separator 4 is a cyclone separator, comprising a straight cylindrical section and a conical section. The inner diameter of the straight cylindrical section is 5-10 cm, and its height is 3-5 cm. The height of the conical section is 5-10 cm. The upper part of the cyclone separator is a straight cylindrical shape with a relatively uniform inner diameter of 5-10 cm and a height of 3-5 cm, while the lower part is a conical shape with a gradually decreasing inner diameter and a height of 5-10 cm. It can be seen that the dimensions of the reactor 3 and the gas-solid separator 4 are on the centimeter scale, allowing reactants and products to pass through quickly and avoiding excessive residence time that could lead to other side reactions.

[0036] In some embodiments, the apparatus for determining the coal pyrolysis tar yield further includes a heating furnace 9 for housing and heating the reactor 3, an insulation box 8 for housing and heating the gas-solid separator 4, and a coke powder collection container 5 connected to the bottom of the gas-solid separator 4. The heating furnace 9 can heat the reactor 3 as a whole, bringing its interior to the pyrolysis temperature. The insulation box 8 keeps the gas-solid separator 4 at a high temperature, preventing premature condensation of the gaseous products flowing through it. The coke powder collection container 5 can receive the solid products from the gas-solid separator 4. The reactor 3 can also employ other heating methods, such as installing internal heating elements.

[0037] In some embodiments, the condensation filter assembly includes a collection tube 7, degreased cotton disposed in the collection tube 7, and a condensation jacket 6 fitted over the outside of the collection tube 7. The collection tube 7 has an inner diameter of 20-50 mm and a length of 10-20 cm, and the degreased cotton has a filling amount of 2-5 g. The condensation jacket 6 can be connected to a refrigeration unit to form a circulation loop. The refrigeration unit cools the condensing medium to a predetermined temperature and circulates the condensing medium in the circulation loop to maintain the collection tube 7 in a low-temperature environment. The collection tube 7 is connected to the outlet end of the second pipeline 16. Gaseous products enter the collection tube 7. Under low temperature conditions, tar and pyrolysis water (gaseous) condense into liquid, which is then filtered and adsorbed by the degreased cotton. The pyrolysis gas flows through the collection tube 7 and is discharged to the outside. The degreased cotton allows small oil droplets formed by tar condensation to adhere to its surface, preventing or reducing the high-speed passage of tar through the collection tube under the action of fluidizing gas and purging gas. As can be seen, the collecting pipe 7 and the condensing jacket 6 collect tar and pyrolysis water through condensation and filtration, so as to measure the yield of tar generated after separating tar and pyrolysis water. The condensing medium can be ethylene glycol, and the condensation temperature is -10℃.

[0038] In some embodiments, the feeding assembly includes a screw feeder 2 and a hopper 1 connected to the inlet of the screw feeder 2. The outlet of the screw feeder 2 is connected to the reactor 3 via a feed pipe 11. Powdered coal can be added to the hopper 1 through its upper inlet. The screw blades in the screw feeder 2 can move the powdered coal to be conveyed into the feed pipe 11. After adding the powdered coal, the hopper 1 and the screw feeder 2 can be kept sealed to prevent leakage of the powdered coal to the outside under the action of purging gas.

[0039] In some embodiments, the device for determining the coal pyrolysis tar yield further includes a thermocouple 10 for detecting the temperature of the isothermal reaction zone. The thermocouple 10 is used to detect the temperature of the isothermal reaction zone, and in conjunction with the adjustment of the heating furnace 9, ensures that the isothermal reaction zone is within the target temperature range.

[0040] On the other hand, this solution also provides a method for determining the yield of coal pyrolysis tar, wherein the apparatus for determining the yield of coal pyrolysis tar described in the above solution includes: S1, load m1 mass of pulverized coal into the feeding assembly, turn on the condensation and filtration assembly to the predetermined condensation temperature, and heat the reactor 3 to the predetermined temperature; S2, the purge gas pipeline 13 and the fluidizing gas pipeline 12 are opened, so that the constant temperature reaction zone reaches the pyrolysis temperature; S3, the feeding assembly is turned on to allow pulverized coal to enter the reactor 3, and after a first predetermined time, the feeding assembly is turned off; S4, after the second predetermined time, stop heating the reactor 3, and after the reactor 3 cools down, close the fluidizing gas pipeline 12 and the purging gas pipeline 13, and close the condenser filter assembly; S5, Weigh the remaining coal powder m2 in the feeding assembly; S6, Measure the amount of tar collected in the condensation filter assembly; S7, calculate tar yield.

[0041] In step S1, after the feed assembly is filled with pulverized coal, it can be sealed. In step S2, the purge gas line 13 and the fluidizing gas line 12 are opened, causing the heat carrier particles in reactor 3 to form a stable fluidized state, creating a temperature-stable isothermal reaction zone. In step S3, pulverized coal is fed into the feed line 11 through the feed assembly. Under the action of the purge gas, the pulverized coal enters the isothermal reaction zone of reactor 3. After a first predetermined time, most of the pulverized coal in the feed assembly enters reactor 3, and then the feed assembly can be closed. The first predetermined time corresponds to the time during which the feed assembly delivers pulverized coal. In step S4, after feeding is completed, fluidizing gas and purge gas are continuously introduced for 5-10 minutes, i.e., the second predetermined time, to fully purge out the tar and pyrolysis gas remaining inside reactor 3 and gas-solid separator 4, ensuring complete tar collection. Subsequently, heating is stopped, the fluidizing gas and purge gas are turned off, and the condenser filter assembly is shut down. In S5, the mass of the remaining coal powder is measured. Combined with the previously measured mass of the coal powder that was loaded, the mass of coal powder that entered reactor 3 to participate in the pyrolysis reaction can be calculated.

[0042] In some embodiments, the condensation filtration assembly includes a collection tube 7, degreased cotton placed in the collection tube 7, and a condensation jacket 6 fitted over the outside of the collection tube 7. S1 includes: weighing the collection tube 7 by mass m3; S6 includes: removing and weighing the collection tube 7 by mass m4, removing the degreased cotton, adding it to an azeotropic solvent, distilling off the pyrolysis water and part of the azeotropic solvent, condensing and collecting the pyrolysis water, allowing the collected liquid to stand and separate, weighing the pyrolysis water by mass m5, and the tar by mass m4-m3-m5. In S1, after weighing the collection tube 7 filled with degreased cotton, it is installed in the condensation jacket 6, and then the condensation jacket 6 is turned on so that the collection tube 7 reaches a predetermined condensation temperature. In step S6, the mass m4 of the collection tube 7 is weighed, which includes the mass of the collected condensed tar and pyrolysis water. The degreased cotton containing the collected tar and pyrolysis water is removed and added to an azeotropic solvent (e.g., toluene or xylene). The pyrolysis water (and a portion of the toluene or xylene) in the toluene or xylene is distilled off. Then, the distilled pyrolysis water and toluene or xylene are separated by separation (e.g., using a separator). The mass m5 of the pyrolysis water can then be weighed. The mass of the tar is m4 - m3 - m5, and the tar yield is (m4 - m3 - m5) / (m1 - m2) * 100%. The boiling point of the azeotropic solvent is between that of tar and water, ensuring that water evaporates while the tar remains largely undiluted.

[0043] In some embodiments, the condensation temperature of the condensing jacket 6 is set to 0 to -20°C. The temperature of the condensing medium in the condensing jacket 6 can be controlled within 0 to -20°C to ensure that the condensation temperature is within the target range, allowing the gaseous tar and pyrolysis water to condense rapidly.

[0044] In some embodiments, the feeding assembly includes a screw feeder 2 and a hopper 1 connected to the inlet of the screw feeder 2. The outlet of the screw feeder 2 is connected to the reactor 3 via a feed pipe 11. S1 includes loading 10-30g of coal powder with a particle size less than 0.3mm into the hopper 1. S3 includes ensuring the feeding speed of the screw feeder 2 is 0.5~2g / min. After loading the coal powder, the inlet of the hopper 1 can be sealed. The coal powder has a particle size less than 0.3mm and a total weight of 10-30g, suitable for reactors 3 and gas-solid separators 4 with centimeter-level dimensions.

[0045] In some embodiments, the purge gas and the fluidizing gas are nitrogen, hydrogen, methane, or a mixture of the three. The velocity of the fluidizing gas is 0.5~1.5 L / min, and the velocity of the purge gas is 0.5~1.5 L / min. The purge gas and the fluidizing gas can be any one of nitrogen, hydrogen, and methane, or a mixture of the three, and the mixing ratio is not limited.

[0046] In some embodiments, the temperature of the isothermal reaction zone in S2 is 550~700℃, for example 600℃, 650℃, etc.

[0047] In some embodiments, the measuring device includes a heating furnace 9 for housing and heating the reactor 3, and a heat-insulating box 8 for housing and heating the gas-solid separator 4. S1 includes: turning on the heating furnace 9 and the heat-insulating box 8, with the predetermined heat-insulating temperature of the heat-insulating box 8 being 250~450℃; S4 includes: turning off the heating furnace 9 and the heat-insulating box 8. The reactor 3 is heated by the heating furnace 9, causing the heat carrier particles to form a fluidized state, and the isothermal reaction zone reaches a predetermined temperature, such as the 550~700℃ mentioned above. The predetermined heat-insulating temperature of the heat-insulating box 8 can be set to 250~450℃ to avoid or reduce the premature condensation of gaseous products into liquid in the gas-solid separator 4. Of course, the heat-insulating temperature should not be too high to avoid or reduce coking.

[0048] The following will describe in more detail the method for determining the coal pyrolysis tar yield in this scheme, including: S1, load m1 mass of coal powder into silo 1, weigh m3 mass of collection pipe 7 filled with degreased cotton, install collection pipe 7 in condensing jacket 6, open condensing jacket 6 to predetermined condensing temperature, open heating furnace 9 to heat reactor 3 to predetermined temperature, open insulation box 8 to predetermined insulation temperature. S2, open the purge gas pipeline 13 and the fluidizing gas pipeline 12. The fluidizing gas causes the quartz sand particles in the reactor 3 to form a fluidized state, and causes the isothermal reaction zone to reach the pyrolysis temperature and remain stable. The height of the isothermal reaction zone is 10-20cm. S3, turn on the screw feeder 2 to allow the coal powder to enter the feed pipe 11, and the purging gas carries the coal powder into the constant temperature reaction zone of the reactor 3. After the first predetermined time, turn off the screw feeder 2. S4, after the second predetermined time, shut down the heating furnace 9 and the heat preservation box 8. After the heating furnace 9 and the heat preservation box 8 have cooled to room temperature, shut down the fluidizing gas pipeline 12 and the purging gas pipeline 13, and shut down the condensing jacket 6. S5, weigh the remaining coal powder m2 in silo 1 and screw feeder 2; S6, remove and weigh the mass m4 of the collection tube 7, take out the degreased cotton, add it to xylene, distill off the pyrolysis water and part of the xylene by distillation and collect it by condensation, let the collected liquid stand and separate (xylene and pyrolysis water), weigh the mass m5 of the pyrolysis water, wherein the mass of the tar is m4-m3-m5; S7, calculate the tar yield (m4-m3-m5) / (m2-m1)*100%.

[0049] In this method, pulverized coal can react rapidly in reactor 3, with a reaction time of less than 10 seconds. The total residence time of pulverized coal and its corresponding products (such as tar) in reactor 3 is 3-10 seconds. This can avoid or reduce secondary cracking or condensation reactions of tar.

[0050] Example 1 The raw coal was sourced from a coal mine in Yulin, Shaanxi Province. After crushing and grinding, the coal powder was obtained, with a particle size less than 0.2 mm. The mass (m1) of the coal powder loaded into the silo was 21.18 g. The mass (m3) of the tar collection pipe containing degreased cotton was 80.36 g. Quartz sand was used as the heat carrier particles, with a particle size of 0.2~0.25 mm, and an addition amount of 5 g. Nitrogen was used for both the fluidizing gas and the purge gas. The reactor inner diameter was 30 mm, and the fluidizing gas velocity was controlled at 1 L / min, while the purge gas velocity was 0.5 L / min. The reactor temperature was 600℃, the insulation box temperature was 400℃, and the condensation temperature was -10℃. After feeding, the total mass of coal powder remaining in the collection bin and screw feeder is 4.76g (m2), the mass of tar collection pipe is 84.68g (m4), and the mass of pyrolysis water collected by distillation is 1.93g (m5). The calculated tar yield of the coal sample from rapid pyrolysis is 14.56%.

[0051] Example 2 The raw coal was sourced from a coal mine in Datong, Shanxi Province. After crushing and grinding, the coal powder was obtained, with a particle size less than 0.3 mm. The mass (m1) of the coal powder loaded into the silo was 15.02 g. The mass (m3) of the tar collection pipe containing degreased cotton was 81.51 g. Quartz sand was used as the heat carrier particles, with a particle size of 0.15~0.2 mm, and an addition amount of 10 g. Nitrogen was used for both the fluidizing gas and the purge gas. The reactor inner diameter was 30 mm, and the fluidizing gas velocity and purge gas velocity were controlled at 1 L / min and 1 L / min respectively. The reactor temperature was 650℃, the insulation box temperature was 450℃, and the condensation temperature was -10℃. After feeding, the total mass of coal powder remaining in the collection bin and screw feeder is 0.74g (m2), the mass of tar collection pipe is 84.56g (m4), and the mass of pyrolysis water collected by distillation is 1.21g (m5). The calculated tar yield of this coal sample is 12.89%.

[0052] Example 3 The raw coal was sourced from the Naomuhu area of ​​Hami, Xinjiang. After crushing and grinding, the coal powder was obtained, with a particle size less than 0.15 mm. The mass (m1) of the coal powder loaded into the silo was 15.21 g. The mass (m3) of the tar collection pipe containing degreased cotton was 81.84 g. Quartz sand was used as the heat carrier particles, with a particle size of 0.15~0.2 mm, and an addition amount of 10 g. Nitrogen was used for both the fluidizing gas and the purge gas. The reactor inner diameter was 30 mm, and the fluidizing gas velocity and purge gas velocity were controlled at 0.5 L / min and 0.5 L / min respectively. The reactor temperature was 600℃, the insulation box temperature was 450℃, and the condensation temperature was -10℃. After feeding, the total mass of coal powder remaining in the collection bin and screw feeder is 0.45g (m2), the mass of tar collection pipe is 86.52g (m4), and the mass of pyrolysis water collected by distillation is 1.96g (m5). The calculated tar yield of this coal sample is 18.43%.

[0053] Example 4 The raw coal was sourced from the Naomuhu area of ​​Hami, Xinjiang. After crushing and grinding, the coal powder was obtained with a particle size of 0.15~0.2mm. The mass (m1) of the coal powder loaded into the silo was 15.15g. The mass (m3) of the tar collection pipe filled with degreased cotton was 80.89g. Quartz sand was used as the heat carrier particles, with a particle size of 0.2~0.3mm, and an addition amount of 10g. Nitrogen was used for both the fluidizing gas and the purge gas. The reactor inner diameter was 30mm, and the fluidizing gas velocity and purge gas velocity were controlled at 1L / min. The reactor temperature was 600℃, the insulation box temperature was 450℃, and the condensation temperature was -10℃. After feeding, the total mass of coal powder remaining in the collection bin and screw feeder is 0.54g (m2), the mass of tar collection pipe is 85.50g (m4), and the mass of pyrolysis water collected by distillation is 1.87g (m5). The calculated tar yield of this coal sample is 18.75%.

[0054] Example 5 The raw coal was sourced from a coal mine in Shuozhou, Shanxi Province. After crushing and grinding, the coal powder was obtained with a particle size of 0.1–0.2 mm. The mass (m1) of the coal powder loaded into the silo was 14.71 g. The mass (m3) of the tar collection pipe containing degreased cotton was 80.73 g. Quartz sand was used as the heat carrier particles, with a particle size of 0.2–0.3 mm, and an addition amount of 5 g. Nitrogen was used for both the fluidizing gas and the purge gas. The reactor inner diameter was 30 mm, and the fluidizing gas velocity and purge gas velocity were controlled at 1 L / min and 1 L / min respectively. The reactor temperature was 650℃, the insulation box temperature was 450℃, and the condensation temperature was -10℃. After feeding, the total mass of coal powder remaining in the collection bin and screw feeder is 0.72g (m2), the mass of tar collection pipe is 83.22g (m4), and the mass of pyrolysis water collected by distillation is 0.87g (m5). The calculated tar yield of the coal sample from rapid pyrolysis is 11.57%.

[0055] Comparative Example 1 The raw coal was taken from a coal mine in Yulin, Shaanxi Province. The tar yield of the raw coal was 10.95% according to the Gram-Kinsey low-temperature dry distillation test method.

[0056] Comparative Example 2 The raw coal was taken from a coal mine in Datong, Shanxi Province. The tar yield of the raw coal was measured to be 8.55% according to the low-temperature dry distillation test method of coal.

[0057] Comparative Example 3 The raw coal was taken from the Naomuhu area of ​​Hami, Xinjiang. The tar yield of the raw coal was 16.47% according to the Geiger low-temperature dry distillation test method.

[0058] Comparative Example 4 The raw coal was taken from a coal mine in Shuozhou, Shanxi Province. The tar yield of the raw coal was measured to be 9.34% according to the Gram-Kinsey low-temperature dry distillation test method.

[0059] A comparison of Examples 1, 2, 3, 4, and 5 with comparative documents 1, 2, 3, and 4 shows that the measuring device and method of this scheme yields a higher tar yield in raw coal.

[0060] The preferred embodiments of the present invention have been described in detail above with reference to the accompanying drawings; however, the present invention is not limited thereto. Within the scope of the inventive concept, various simple modifications can be made to the technical solutions of the present invention, including combinations of various specific technical features in any suitable manner. To avoid unnecessary repetition, the present invention will not describe the various possible combinations separately. However, these simple modifications and combinations should also be considered as the content disclosed in the present invention and are all within the protection scope of the present invention.

Claims

1. An apparatus for determining the yield of coal pyrolysis tar, characterized in that, The reactor (3) includes a reactor with internal heat carrier particles, a feed assembly connected to the reactor (3) via a feed pipe (11), a purge gas pipe (13) connected to the feed pipe (11), a fluidizing gas pipe (12) connected to the reactor (3), a gas-solid separator (4) connected to the reactor (3), and a condenser filter assembly connected to the gas-solid separator (4). The fluidizing gas pipe (12) is configured to supply fluidizing gas to the reactor (3) to form a fluidized state distributed in the reactor (3). The heat carrier particles are in a constant temperature reaction zone with a height of 10-20 cm. The feeding assembly is configured to feed pulverized coal to the reactor (3) through the feeding pipeline (11). The purge gas pipeline (13) is configured to provide purge gas to the feeding pipeline (11) so that the pulverized coal enters the reactor (3). The gas-solid separator (4) is configured to separate the gaseous products and solid products from the reactor (3). The condensation and filtration assembly is configured to condense and filter the tar and pyrolysis water in the gaseous products.

2. The apparatus for determining the yield of coal pyrolysis tar according to claim 1, characterized in that, The heat carrier particles are quartz sand particles with a particle size of 0.1~0.5mm.

3. The apparatus for determining the yield of coal pyrolysis tar according to claim 2, characterized in that, The reactor (3) has an inner diameter of 20-30 mm; and / or, the reactor (3) is provided with a sieve plate (14) to support the quartz sand particles; and / or, the reactor (3) contains 5-10 g of the quartz sand particles.

4. The apparatus for determining the yield of coal pyrolysis tar according to claim 1, characterized in that, The gas-solid separator (4) is a cyclone separator, which includes a straight cylindrical section and a conical section. The inner diameter of the straight cylindrical section is 5~10cm and the height is 3~5cm. The height of the conical section is 5~10cm.

5. The apparatus for determining the yield of coal pyrolysis tar according to claim 1, characterized in that, It also includes a heating furnace (9) for housing and heating the reactor (3), an insulation box (8) for housing and heating the gas-solid separator (4), and a coke collection container (5) connected to the bottom of the gas-solid separator (4).

6. The apparatus for determining the yield of coal pyrolysis tar according to claim 1, characterized in that, The condensation filter assembly includes a collection tube (7), degreased cotton disposed in the collection tube (7), and a condensation jacket (6) sleeved outside the collection tube (7). The inner diameter of the collection tube (7) is 20-50 mm, the length is 10-20 cm, and the filling amount of the degreased cotton is 2-5 g.

7. The apparatus for determining the yield of coal pyrolysis tar according to claim 1, characterized in that, The feeding assembly includes a screw feeder (2) and a hopper (1) connected to the feed inlet of the screw feeder (2). The discharge outlet of the screw feeder (2) is connected to the reactor (3) through the feed pipeline (11).

8. The apparatus for determining the yield of coal pyrolysis tar according to claim 1, characterized in that, It also includes a thermocouple (10) for detecting the temperature of the isothermal reaction zone.

9. A method for determining the yield of coal pyrolysis tar, characterized in that, The apparatus for determining the yield of coal pyrolysis tar as described in claim 1 comprises: S1, load m1 mass of pulverized coal into the feeding assembly, turn on the condensation and filtration assembly to the predetermined condensation temperature, and heat the reactor (3) to the predetermined temperature; S2, open the purge gas pipeline (13) and the fluidizing gas pipeline (12) so that the constant temperature reaction zone reaches the pyrolysis temperature; S3, the feeding assembly is turned on to allow pulverized coal to enter the reactor (3), and after a first predetermined time, the feeding assembly is turned off; S4, after the second predetermined time, stop heating the reactor (3), and after the reactor (3) cools down, close the fluidizing gas pipeline (12) and the purging gas pipeline (13), and close the condenser filter assembly; S5, Weigh the remaining coal powder m2 in the feeding assembly; S6, Measure the amount of tar collected in the condensation filter assembly; S7, calculate tar yield.

10. The method for determining the yield of coal pyrolysis tar according to claim 9, characterized in that, The condensation filter assembly includes a collection tube (7), degreased cotton placed in the collection tube (7), and a condensation jacket (6) sleeved outside the collection tube (7). S1 includes: weighing the mass m3 of the collection tube (7); S6 includes: removing and weighing the mass m4 of the collection tube (7), taking out the degreased cotton, adding it to the azeotropic solvent, distilling out the pyrolysis water and part of the azeotropic solvent by distillation and collecting it by condensation, letting the collected liquid stand and separating it, weighing the mass m5 of the pyrolysis water, and the mass of the tar is m4-m3-m5.

11. The method for determining the yield of coal pyrolysis tar according to claim 10, characterized in that, The condensation temperature of the condensation jacket (6) is set to 0~-20℃.

12. The method for determining the yield of coal pyrolysis tar according to claim 9, characterized in that, The feeding assembly includes a screw feeder (2) and a hopper (1) connected to the feed inlet of the screw feeder (2). The outlet end of the screw feeder (2) is connected to the reactor (3) through a feed pipe (11). S1 includes: loading 10~30g of coal powder with a particle size of less than 0.3mm into the silo (1); S3 includes: the feeding speed of the screw feeder (2) is 0.5~2g / min.

13. The method for determining the yield of coal pyrolysis tar according to claim 9, characterized in that, The purge gas and the fluidizing gas are nitrogen, hydrogen, methane, or a mixture of the three. The gas velocity of the fluidizing gas is 0.5~1.5 L / min, and the gas velocity of the purge gas is 0.5~1.5 L / min.

14. The method for determining the yield of coal pyrolysis tar according to claim 9, characterized in that, In S2, the temperature of the isothermal reaction zone is 550~700℃.

15. The method for determining the yield of coal pyrolysis tar according to claim 9, characterized in that, The measuring device includes a heating furnace (9) for housing and heating the reactor (3) and an insulation box (8) for housing and heating the gas-solid separator (4). S1 includes: turning on the heating furnace (9) and the heat preservation box (8), wherein the predetermined heat preservation temperature of the heat preservation box (8) is 250~450℃; S4 includes: shutting down the heating furnace (9) and the insulation box (8).

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