CN103205268B - Low-order coal pyrolysis tar device and pyrolysis method of low-order coal pyrolysis tar - Google Patents

Abstract

The invention relates to the technical field of pyrolysis tar, and relates to a low-rank coal pyrolysis tar device and a pyrolysis method for low-rank coal pyrolysis tar; the low-rank coal pyrolysis tar device includes a pump, a preheater, and a fixed-bed reactor and condenser; on the preheater, there are air inlet, liquid inlet and gas outlet respectively, the liquid outlet of the pump and the liquid inlet of the preheater are fixedly connected together through the first pipeline, and the gas outlet of the preheater It is fixedly connected with the inlet end of the fixed bed reactor through the second pipeline. In the present invention, low-rank coal is used as raw material, and the hydrogenation pyrolysis of low-rank coal is carried out under the atmosphere of water and CO, and the pure hydrogen supplied by traditional coal pyrolysis is replaced by highly active hydrogen produced by CO shift reaction, which saves the traditional hydrogenation The process of drying and dehydrating medium and low-rank coal has the characteristics of wide and cheap sources of raw gas and high yield of coal tar, which simplifies the process, reduces production costs, and improves production efficiency.

Description

Low-rank coal pyrolysis tar device and pyrolysis method for low-rank coal pyrolysis tar

technical field

The invention relates to the technical field of pyrolysis tar, and relates to a low-order coal pyrolysis tar device and a pyrolysis method for low-order coal pyrolysis tar.

Background technique

In recent years, large-scale coal fields have been continuously discovered in my country's Inner Mongolia, Xinjiang and other places. These coal fields are mainly high-volatility low-rank coals, accounting for more than 50% of my country's coal resource reserves. Pyrolysis is a coal conversion method most suitable for handling these coal resources. Coal pyrolysis technology appeared in the 19th century, but due to technical limitations, the products produced were relatively simple. At that time, it was mainly used to make kerosene and wax. Since the 1970s, compared with general fast pyrolysis, coal hydropyrolysis not only has a high yield of tar, but also has a large content of benzene, phenol and naphthalene, but pure hydrogen is expensive, the hydrogen production process is complicated, and equipment investment The cost is high, the operating conditions are harsh, and the operating cost is high, so hydropyrolysis has been stuck in the pilot test stage. With the rising international crude oil prices and oil shortages reappearing, pyrolysis and subsequent hydrogenation of coal tar to produce fuel oil has attracted attention. At present, the pyrolysis process research for the purpose of increasing the tar yield mainly contains the following categories:

Pretreatment: Through various pretreatment processes, the physical and chemical structure of coal can be changed to a certain extent, thereby increasing the yield of pyrolysis tar. Graff et al. pyrolyzed Illinois #6 coal pretreated with subcritical steam at 320°C to 360°C and 5 MPa and found that the tar yield increased by 30%. They believe that subcritical steam pretreatment can fully destroy the bridge bonds in coal molecules, but the test results have not been repeated by other researchers so far.

Changing the reaction atmosphere: Scholars at home and abroad have also proposed to use coke oven gas instead of pure hydrogen as the hydropyrolysis reaction gas. The research results show that co-pyrolysis of coal to coke oven gas can obtain The hydropyrolysis tar yield is similar, but the tar yield still cannot exceed the coal tar yield under pure hydrogen atmosphere. Chinese patent CN1664069A discloses that methane is used as the reaction gas, and 0 to 20% oxidant is added to the methane. After the methane and the oxidant are mixed, they enter the pyrolysis reactor through the gas inlet. 60min; the research results show that the tar yield of coal pyrolysis with methane as reaction atmosphere is higher than that under pure hydrogen atmosphere, but the tar yield is still lower than 10% at 500 °C.

Catalytic pyrolysis: Coal hydropyrolysis experiments with the addition of 0.5% (mass fraction) MoS2 showed that, compared with the hydrogenation reaction without catalyst, the addition of catalyst increased the yield of light oil and PCX, and the The content of S and N decreased, and the quality of oil was obviously improved. At the same time, catalytic hydropyrolysis can be performed at lower temperatures and improves the utilization of hydrogen. However, these catalysts are expensive, and the recovery is very troublesome, which brings great difficulties to industrial implementation.

Contents of the invention

The present invention provides a low-rank coal pyrolysis tar device and its pyrolysis method, which overcomes the above-mentioned deficiencies in the prior art, and can effectively solve the problems of low tar yield and high production cost in the existing low-rank coal pyrolysis process question.

One of the technical solutions of the present invention is achieved by the following measures: a low-rank coal pyrolysis tar device, including a pump, a preheater, a fixed bed reactor and a condenser; , the liquid inlet end and the gas outlet end, the liquid outlet end of the pump and the liquid inlet end of the preheater are fixedly connected together through the first pipeline, and the gas outlet end of the preheater and the inlet end of the fixed bed reactor are fixed through the second pipeline connected together, the gas outlet of the fixed bed reactor and the inlet of the condenser are fixedly connected together through a third pipeline, and there are gas outlet and liquid outlet at the side and bottom of the condenser respectively.

The following is a further optimization or/and improvement to one of the technical solutions of the above invention:

The air inlet pipe is fixedly connected to the air inlet end of the preheater, the liquid inlet pipe is fixedly connected to the liquid inlet end of the pump, the air outlet pipe is fixedly connected to the air outlet end of the condenser, and the liquid outlet pipe is fixedly connected to the condenser liquid outlet end. A liquid outlet pipe is fixedly connected on the fixed bed reactor, and a thermometer is fixedly installed on the fixed bed reactor, and the temperature measuring end of the thermometer is located in the fixed bed reactor; or/and, in the inlet pipe, the liquid inlet pipe, the first pipeline, the outlet pipe and the Valves are respectively fixedly installed on the liquid outlet pipes.

The second technical solution of the present invention is achieved by the following measures: a method for pyrolysis of low-rank coal pyrolysis tar using a low-rank coal pyrolysis tar device, carried out according to the following steps: the first step, fixed bed reaction Filling of the reactor, filling the lower layer of the fixed bed reactor with low-rank pulverized coal, filling the middle layer of the fixed bed reactor with quartz wool, filling the upper layer of the fixed bed reactor with CO shift reaction catalyst, CO shift reaction catalyst and low The mass ratio of rank coal powder is 1:2 to 1:10; in the second step, after heating the preheater to 150°C to 300°C, feed raw gas containing CO and water into the preheater, and the water is In the heater, it is quickly vaporized into water vapor and mixed evenly with the raw material gas containing CO to form a reaction gas. The mass percentage of CO in the raw material gas in the reaction gas is 30% to 80%; the third step is the reaction in the preheater The gas enters the fixed bed reactor, and at a temperature of 450°C to 750°C, the reaction gas reacts with the low-order coal powder in the fixed bed reactor for 30 minutes to 60 minutes under the action of the CO shift reaction catalyst, and the pyrolysis The reacted mixed gas enters the condenser for condensation, and after condensation, a mixed liquid of coal tar and water and residual gas are obtained; in the fourth step, the mixed liquid of coal tar and water is separated to obtain coal tar.

The following is a further optimization or/and improvement to the second technical solution of the above invention:

The mass percent content of CO in the raw material gas is 2% to 99%.

The particle size of the CO shift reaction catalyst is 40 mesh to 60 mesh.

The above CO shift reaction catalyst is B205-1 catalyst or B113-1 catalyst or B208 catalyst. The heating rate of the above preheater is 10°C/min to 20°C/min; the heating rate of the fixed bed reactor is 10°C/min to 20°C/min.

Above-mentioned 4th step, the mixed solution of coal tar and water is separated according to ASTM D95-83 method and obtains coal tar.

The particle size of the above-mentioned low-rank coal powder is 60 mesh to 100 mesh.

The condensation temperature in the above-mentioned condenser is -5°C to -20°C, and the condensing agent is saturated brine or ethylene glycol or an aqueous solution of ethylene glycol with a mass percentage of 60% to 99%.

In the present invention, low-rank coal is used as raw material, and the hydropyrolysis of low-rank coal is carried out under the atmosphere of water and CO, and the pure hydrogen supplied by traditional coal pyrolysis is replaced by highly active hydrogen produced by CO shift reaction, which saves the traditional hydrogenation The process of drying and dehydrating medium and low-rank coal has the characteristics of wide and cheap sources of raw gas and high yield of coal tar, which simplifies the process, reduces production costs, and improves production efficiency.

Description of drawings

Accompanying drawing 1 is the structural representation and process flow diagram of the embodiment of the present invention.

The codes in the accompanying drawings are: 1 is the pump, 2 is the preheater, 3 is the fixed bed reactor, 4 is the condenser, 5 is the first pipeline, 6 is the second pipeline, 7 is the third pipeline, 8 is the Intake pipe, 9 is a liquid inlet pipe, 10 is an air outlet pipe, 11 is a liquid outlet pipe, 12 is a valve, 13 is a low-order pulverized coal, 14 is quartz wool, and 15 is a CO shift reaction catalyst. the

Detailed ways

The present invention is not limited by the following examples, and specific implementation methods can be determined according to the technical solutions of the present invention and actual conditions.

Embodiment 1, as shown in accompanying drawing 1, this low rank coal pyrolysis tar device comprises pump 1, preheater 2, fixed bed reactor 3 and condenser 4; The liquid inlet end and the gas outlet end, the liquid outlet end of the pump 1 and the liquid inlet end of the preheater 2 are fixedly connected together through the first pipeline 5, and the gas outlet end of the preheater 2 and the inlet end of the fixed bed reactor 3 pass through The second pipeline 6 is fixedly connected together, the gas outlet end of the fixed bed reactor 3 and the inlet end of the condenser 4 are fixedly connected together through the third pipeline 7, and the side and the bottom of the condenser 4 have a gas outlet and an outlet respectively. liquid end.

Embodiment 2, as shown in accompanying drawing 1, as the optimization of above-mentioned embodiment, on the inlet end of preheater 2 in embodiment 2, be fixedly connected with inlet pipe 8, on the liquid inlet end of pump 1, be fixedly connected with The liquid inlet pipe 9 is fixedly connected with the gas outlet pipe 10 on the gas outlet end of the condenser 4, is fixedly connected with the liquid outlet pipe 11 on the liquid outlet end of the condenser 4, and is fixedly installed with a thermometer on the fixed bed reactor 3, and the thermometer The temperature measuring end is located in the fixed bed reactor 3; or/and, valves 12 are fixedly installed on the inlet pipe 8, the liquid inlet pipe 9, the first pipeline 5, the gas outlet pipe 10 and the liquid outlet pipe 11 respectively. In this way, valve 12 is easily controlled.

Embodiment 3, as shown in accompanying drawing 1, the pyrolysis method of the low-rank coal pyrolysis tar that this uses low-rank coal pyrolysis tar device, carry out according to the following steps: the first step, the filling of fixed-bed reactor 3, Fill the lower layer of the fixed bed reactor 3 with low-rank pulverized coal 13, fill the middle layer of the fixed bed reactor 3 with quartz wool 14, and fill the upper layer of the fixed bed reactor 3 with a CO shift reaction catalyst 15, CO shift reaction catalyst The mass ratio of 15 and low-rank pulverized coal 13 is 1:2 to 1:10; in the second step, after heating the preheater 2 to 150°C to 300°C, feed the raw material gas containing CO into the preheater 2 and water, the water is quickly vaporized into water vapor in the preheater 2 and mixed evenly with the feed gas containing CO to form a reaction gas, and the mass percentage of CO in the feed gas in the reaction gas is 30% to 80%; the third step , the reaction gas in the preheater 2 enters the fixed bed reactor 3, and at a temperature of 450°C to 750°C, the reaction gas reacts with the low-order pulverized coal in the fixed bed reactor 3 under the action of the CO shift reaction catalyst 15 13 pyrolysis reaction for 30 minutes to 60 minutes, the mixed gas after the pyrolysis reaction enters the condenser 4 for condensation, and after condensation, the mixed liquid and residual gas of coal tar and water are obtained; the fourth step is to mix the coal tar and water The liquid is separated to obtain coal tar. The water in the second step can be laboratory distilled water, tap water supplied by the city, industrial water or industrial wastewater containing organic matter. Low-rank coal is lignite or long-flame coal with low degree of coalification or a combination of lignite and long-flame coal with low degree of coalification in China's coal classification.

Embodiment 4, as shown in accompanying drawing 1, the pyrolysis method of the low-rank coal pyrolysis tar that this uses low-rank coal pyrolysis tar device, carries out according to the following steps: the first step, the filling of fixed-bed reactor 3, Fill the lower layer of the fixed bed reactor 3 with low-rank pulverized coal 13, fill the middle layer of the fixed bed reactor 3 with quartz wool 14, and fill the upper layer of the fixed bed reactor 3 with a CO shift reaction catalyst 15, CO shift reaction catalyst The mass ratio of 15 and low-rank pulverized coal 13 is 1:2 or 1:10; in the second step, after heating the preheater 2 to 150°C or 300°C, feed the feed gas containing CO into the preheater 2 and water, the water is quickly vaporized into water vapor in the preheater 2 and mixed evenly with the raw material gas containing CO to form a reaction gas, and the mass percentage of CO in the raw gas in the reaction gas is 30% or 80%; the third step , the reaction gas in the preheater 2 enters the fixed bed reactor 3, and at a temperature of 450°C or 750°C, the reaction gas reacts with the low-order pulverized coal in the fixed bed reactor 3 under the action of the CO shift reaction catalyst 15 13 pyrolysis reaction for 30 minutes or 60 minutes, the mixed gas after the pyrolysis reaction enters the condenser 4 for condensation, and after condensation, the mixed liquid and residual gas of coal tar and water are obtained; the fourth step is to mix the coal tar and water The liquid is separated to obtain coal tar. The water in the second step can be laboratory distilled water, tap water supplied by the city, industrial water or industrial wastewater containing organic matter. Low-rank coal is lignite or long-flame coal with low degree of coalification or a combination of lignite and long-flame coal with low degree of coalification in China's coal classification.

Example 5, as an optimization of the above example, the mass percentage of CO in the feed gas in Example 5 is 2% to 99%. In this way, the raw gas can be CO liquefied gas or industrial waste gas containing CO.

Embodiment 6, as an optimization of the above embodiments, the particle size of the CO shift reaction catalyst 15 in Embodiment 6 is 40 mesh to 60 mesh.

Example 7, as an optimization of the above example, the CO shift reaction catalyst 15 in Example 7 is the B205-1 catalyst or the B113-1 catalyst or the B208 catalyst. Embodiment 8, as the optimization of the above-mentioned embodiment, the heating rate of preheater 2 in embodiment 8 is 10 ℃/min to 20 ℃/min; The heating rate of fixed bed reactor 3 is 10 ℃/min to 20 ℃/min min. This is more conducive to the pyrolysis reaction.

Example 9, as an optimization of the above examples, in the fourth step in Example 9, the mixture of coal tar and water is separated according to the ASTM D95-83 method to obtain coal tar.

Example 10, as an optimization of the above examples, the particle size of the low-rank pulverized coal 13 in Example 10 is 60 mesh to 100 mesh.

Example 11, as an optimization of the above examples, the condensation temperature in the condenser 4 in Example 11 is -5°C to -20°C, and the condensing agent is saturated brine or ethylene glycol or 60% to 99% by mass Aqueous solution of ethylene glycol.

The low-rank coal used in the above examples can be Tiechanggou coal, Datong coal, Nantaizi coal, Hongmiao lignite, Dongsheng lignite, etc. The average process parameters of Tiechanggou coal and Datong coal are shown in Table 1.

It can be seen from Table 1 that the average mass percentages of water, ash and volatile matter in Nantaizi coal industry analysis are 8.24%, 11.74% and 40.40% respectively, and C, H, N, O* The average mass percentages of S and S were 77.74%, 4.72%, 1.23%, 15.89%, and 0.42%, respectively; %, 43.73%, and the average mass percentages of C, H, N, O*, and S in the elemental analysis of Tiechanggou coal were 77.02%, 4.82%, 1.01%, 15.75%, and 1.40%, respectively.

°C, the average tar yield and semi-coke yield of the present invention and low-rank coal pyrolysis under different atmospheres are shown in Table 2.

It can be seen from Table 2 that at 500°C, the Datong coal ₂ The average tar yield and semi-coke yield of pyrolysis under atmosphere were 10.3% and 75.0% respectively; ₂ The average tar yield and semi-coke yield of pyrolysis under atmosphere were 7.6% and 73.5% respectively; ₂ The average tar yield and semi-coke yield of pyrolysis under atmosphere were 8.4% and 64.7% respectively; ₂ The average tar yield and semi-coke yield of pyrolysis under atmosphere are 3% to 6%, 70% to 75%, respectively; ₂ The average tar yield and semi-coke yield of pyrolysis under atmosphere are 6% to 8%, 70% to 75% respectively; ₂ The average tar yield and semi-coke yield of pyrolysis under O atmosphere are respectively 11% to 15%, 60% to 65%; ₂ Pyrolysis tar yield under O atmosphere lower rank coal in H ₂ Atmosphere or N ₂ The yield of pyrolysis tar under the atmosphere is significantly improved, and the feed gas CO+H ₂ O has the advantage of lower price than pure hydrogen supplied by traditional coal pyrolysis, which also reduces production costs.

The above technical features constitute the embodiment of the present invention, which has strong adaptability and implementation effect, and non-essential technical features can be increased or decreased according to actual needs to meet the needs of different situations.

                                                 

Claims (30)

1. the method for pyrolysis of a low-rank coal pyrolytic tar, it is characterized in that carrying out in the steps below: the first step, the filling of fixed-bed reactor, lower floor at fixed-bed reactor loads low order coal dust, silica wool is loaded in middle level at fixed-bed reactor, CO catalyst for water-gas shift reaction is loaded on upper strata at fixed-bed reactor, and the mass ratio of CO catalyst for water-gas shift reaction and low order coal dust is 1:2 to 1:10; Second step, preheater is heated to after 150 DEG C to 300 DEG C, in preheater, pass into the raw material G&W that contains CO, water is vaporizated into rapidly steam and is mixed into reaction gas with the unstripped gas that contains CO in preheater, and the mass percentage content of the CO in unstripped gas in reaction gas is 30% to 80%; The 3rd step, reaction gas in preheater enters in fixed-bed reactor, be at 450 DEG C to 750 DEG C in temperature, reaction gas under the effect of CO catalyst for water-gas shift reaction with fixed-bed reactor in low order coal dust pyrolytic reaction 30 minutes to 60 minutes, gas mixture after pyrolytic reaction enters in condenser and carries out condensation, obtains mixed solution, the residual gas of coal tar and water after condensation; The 4th step, separates the mixed solution of coal tar and water to obtain coal tar; Wherein:

Low order pyrolysis of coal tar device comprises pump, preheater, fixed-bed reactor and condenser; On preheater, there are respectively inlet end, liquid feeding end and outlet side, the outlet end of pump and the liquid feeding end of preheater are fixed together by the first pipeline, the outlet side of preheater and the inlet end of fixed-bed reactor are fixed together by the second pipeline, the outlet side of fixed-bed reactor and the inlet end of condenser are fixed together by the 3rd pipeline, have respectively outlet side and outlet end in sidepiece and the bottom of condenser.

2. the method for pyrolysis of low-rank coal pyrolytic tar according to claim 1, it is characterized in that being fixedly connected with inlet pipe on the inlet end of preheater, on the liquid feeding end of pump, be fixedly connected with liquid-inlet pipe, on the outlet side of condenser, be fixedly connected with escape pipe, on the outlet end of condenser, be fixedly connected with drain pipe, on fixed-bed reactor, be installed with thermometer, the thermometric end of thermometer is positioned at fixed-bed reactor; Or/and, on inlet pipe, liquid-inlet pipe, the first pipeline, escape pipe and drain pipe, be installed with respectively valve.

3. the method for pyrolysis of low-rank coal pyrolytic tar according to claim 1 and 2, the quality percentage composition that it is characterized in that CO in unstripped gas is 2% to 99%.

4. according to claim 1 or 2 or the method for pyrolysis of described low-rank coal pyrolytic tar, the particle diameter that it is characterized in that CO catalyst for water-gas shift reaction is 40 order to 60 orders.

5. according to the method for pyrolysis of claim 3 or described low-rank coal pyrolytic tar, the particle diameter that it is characterized in that CO catalyst for water-gas shift reaction is 40 order to 60 orders.

6. according to the method for pyrolysis of the low-rank coal pyrolytic tar described in claim 1 or 2 or 5, it is characterized in that CO catalyst for water-gas shift reaction is B205-1 catalyzer or B113-1 catalyzer or B208 catalyzer.

7. the method for pyrolysis of low-rank coal pyrolytic tar according to claim 3, is characterized in that CO catalyst for water-gas shift reaction is B205-1 catalyzer or B113-1 catalyzer or B208 catalyzer.

8. the method for pyrolysis of low-rank coal pyrolytic tar according to claim 4, is characterized in that CO catalyst for water-gas shift reaction is B205-1 catalyzer or B113-1 catalyzer or B208 catalyzer.

9. according to the method for pyrolysis of the low-rank coal pyrolytic tar described in claim 1 or 2 or 5 or 7 or 8, the heating rate that it is characterized in that preheater is 10 DEG C/min to 20 DEG C/min; The heating rate of fixed-bed reactor is 10 DEG C/min to 20 DEG C/min.

10. the method for pyrolysis of low-rank coal pyrolytic tar according to claim 3, the heating rate that it is characterized in that preheater is 10 DEG C/min to 20 DEG C/min; The heating rate of fixed-bed reactor is 10 DEG C/min to 20 DEG C/min.

The method for pyrolysis of 11. low-rank coal pyrolytic tars according to claim 4, the heating rate that it is characterized in that preheater is 10 DEG C/min to 20 DEG C/min; The heating rate of fixed-bed reactor is 10 DEG C/min to 20 DEG C/min.

The method for pyrolysis of 12. low-rank coal pyrolytic tars according to claim 6, the heating rate that it is characterized in that preheater is 10 DEG C/min to 20 DEG C/min; The heating rate of fixed-bed reactor is 10 DEG C/min to 20 DEG C/min.

13. according to the method for pyrolysis of the low-rank coal pyrolytic tar described in claim 1 or 2 or 5 or 7 or 8 or 10 or 11 or 12, it is characterized in that the 4th step, and the mixed solution of coal tar and water is separated and obtains coal tar according to ASTM D95-83 method.

The method for pyrolysis of 14. low-rank coal pyrolytic tars according to claim 3, is characterized in that the 4th step, and the mixed solution of coal tar and water is separated and obtains coal tar according to ASTM D95-83 method.

The method for pyrolysis of 15. low-rank coal pyrolytic tars according to claim 4, is characterized in that the 4th step, and the mixed solution of coal tar and water is separated and obtains coal tar according to ASTM D95-83 method.

The method for pyrolysis of 16. low-rank coal pyrolytic tars according to claim 6, is characterized in that the 4th step, and the mixed solution of coal tar and water is separated and obtains coal tar according to ASTM D95-83 method.

The method for pyrolysis of 17. low-rank coal pyrolytic tars according to claim 9, is characterized in that the 4th step, and the mixed solution of coal tar and water is separated and obtains coal tar according to ASTM D95-83 method.

18. according to the method for pyrolysis of the low-rank coal pyrolytic tar described in claim 1 or 2 or 5 or 7 or 8 or 10 or 11 or 12 or 14 or 15 or 16 or 17, and the particle diameter that it is characterized in that low order coal dust is 60 order to 100 orders.

The method for pyrolysis of 19. low-rank coal pyrolytic tars according to claim 3, the particle diameter that it is characterized in that low order coal dust is 60 order to 100 orders.

The method for pyrolysis of 20. low-rank coal pyrolytic tars according to claim 4, the particle diameter that it is characterized in that low order coal dust is 60 order to 100 orders.

The method for pyrolysis of 21. low-rank coal pyrolytic tars according to claim 6, the particle diameter that it is characterized in that low order coal dust is 60 order to 100 orders.

The method for pyrolysis of 22. low-rank coal pyrolytic tars according to claim 9, the particle diameter that it is characterized in that low order coal dust is 60 order to 100 orders.

The method for pyrolysis of 23. low-rank coal pyrolytic tars according to claim 13, the particle diameter that it is characterized in that low order coal dust is 60 order to 100 orders.

24. according to the method for pyrolysis of the low-rank coal pyrolytic tar described in claim 1 or 2 or 5 or 7 or 8 or 10 or 11 or 12 or 14 or 15 or 16 or 17 or 19 or 20 or 21 or 22 or 23, it is characterized in that the condensing temperature in condenser is-5 DEG C to-20 DEG C, condensing agent is that saturated brine or ethylene glycol or mass percent are 60% to 99% aqueous glycol solution.

The method for pyrolysis of 25. low-rank coal pyrolytic tars according to claim 3, is characterized in that the condensing temperature in condenser is-5 DEG C to-20 DEG C, and condensing agent is that saturated brine or ethylene glycol or mass percent are 60% to 99% aqueous glycol solution.

The method for pyrolysis of 26. low-rank coal pyrolytic tars according to claim 4, is characterized in that the condensing temperature in condenser is-5 DEG C to-20 DEG C, and condensing agent is that saturated brine or ethylene glycol or mass percent are 60% to 99% aqueous glycol solution.

The method for pyrolysis of 27. low-rank coal pyrolytic tars according to claim 6, is characterized in that the condensing temperature in condenser is-5 DEG C to-20 DEG C, and condensing agent is that saturated brine or ethylene glycol or mass percent are 60% to 99% aqueous glycol solution.

The method for pyrolysis of 28. low-rank coal pyrolytic tars according to claim 9, is characterized in that the condensing temperature in condenser is-5 DEG C to-20 DEG C, and condensing agent is that saturated brine or ethylene glycol or mass percent are 60% to 99% aqueous glycol solution.

The method for pyrolysis of 29. low-rank coal pyrolytic tars according to claim 13, is characterized in that the condensing temperature in condenser is-5 DEG C to-20 DEG C, and condensing agent is that saturated brine or ethylene glycol or mass percent are 60% to 99% aqueous glycol solution.

The method for pyrolysis of 30. low-rank coal pyrolytic tars according to claim 18, is characterized in that the condensing temperature in condenser is-5 DEG C to-20 DEG C, and condensing agent is that saturated brine or ethylene glycol or mass percent are 60% to 99% aqueous glycol solution.