CN216919141U - Static mixing arrangement of fine coal fast pyrolysis reaction - Google Patents

Abstract

The utility model provides a static mixing device for a pulverized coal fast pyrolysis reaction, which comprises a charcoal burning device, a reactor and a settler; the bottom outlet of the charcoal burner is connected with a vertical pipe of the charcoal burner; the outlet of the vertical pipe of the charcoal burner is provided with a thin pipeline group; the inlet end of the reactor is connected with a conveying gas pipeline, and the outlet of the thin pipeline group is arranged in the inlet end of the reactor and is positioned on one side of the conveying gas pipeline; a first cyclone separator is arranged in the settler, and the outlet end of the reactor extends into the settler and is connected with the first cyclone separator; the bottom outlet of the settler is connected with a settler inclined tube, and the outlet of the settler inclined tube is connected with the inlet of the charcoal burner. The device makes hot fine coke more evenly fall to the reactor through installing thin pipeline group additional, again with the even mixture of fine coal, makes being heated of fine coal bigger degree, has improved the utilization ratio of hot fine coke, and can make the difficult jam of feeding hybrid system in the reactor, and the fine coke whereabouts volume is controllable, easily carries, low cost.

Description

Static mixing arrangement of fine coal fast pyrolysis reaction

Technical Field

The utility model relates to the technical field of pulverized coal pyrolysis reaction, in particular to a static mixing device for rapid pulverized coal pyrolysis reaction.

Background

Under the condition of reaching a certain coal thermal decomposition temperature, the coal pyrolysis reaction mainly generates tar, coke breeze and oil gas, so that the research on the rapid pyrolysis reaction of the pulverized coal is beneficial to further development and utilization of coal resources in China.

The existing fast pyrolysis process of pulverized coal is a heat carrier which is used independently, so that heat loss in the reaction process is easily caused, and resource waste is also caused. Therefore, two different heat carrier process technologies are developed, the advantages of the two heat carriers can be combined, hot coke breeze is used as a solid heat carrier, coal gas is used as a gas heat carrier, the flow of the gas is utilized to drive the back mixing of the coke breeze and the pulverized coal, the mass transfer and heat transfer processes are accelerated, meanwhile, the high-temperature coke breeze is used, the high-efficiency heat transfer can be realized, and the coal pyrolysis reaction of the pulverized coal in a reactor is guaranteed.

However, some defects are still found in the subsequent reaction, for example, the coke breeze directly falls into the reaction tube through a thick tube after passing through the coke burner riser slide valve, so that the complete and uniform mixing of the falling high-temperature coke breeze and the pulverized coal cannot be ensured; the pyrolysis reaction of coal is insufficient, the yield of tar of reaction products is low, the solid content of oil gas is high, the utilization rate of pulverized coal is low, and the load of a fan for combustion oxygen supply is large.

SUMMERY OF THE UTILITY MODEL

In order to solve the technical problems, the utility model aims to provide a static mixing device for a fast pyrolysis reaction of pulverized coal, which solves the problem of uneven mixing of coke breeze and pulverized coal in a reactor.

In order to achieve the above object, the technical scheme of the utility model is as follows.

A static mixing device for fast pyrolysis reaction of pulverized coal comprises:

the bottom outlet of the charcoal burner is connected with a charcoal burner vertical pipe; the outlet of the vertical pipe of the charcoal burner is provided with a thin pipeline group;

the inlet end of the reactor is connected with a conveying gas pipeline, and the outlet of the fine pipeline group is arranged in the inlet end of the reactor and is positioned on one side of the conveying gas pipeline;

the device comprises a settler, a first cyclone separator is arranged in the settler, and the outlet end of the reactor extends into the settler and is connected with the first cyclone separator; the bottom outlet of the settler is connected with a settler inclined tube, and the outlet of the settler inclined tube is connected with the inlet of the charcoal burner.

Further, along the flowing direction of the conveying coal gas, the lengths of the parts of the thin pipe groups, which are positioned in the inlet end of the reactor, are sequentially reduced.

Furthermore, the cross section of the thin pipeline group is elliptical.

Further, the thin tube group is internally provided with a plurality of channels, and each channel is communicated with the inlet end of the reactor.

Further, a precipitator gas collection chamber is arranged at the top of the precipitator, and an exhaust port of the first cyclone separator is connected with an inlet of the precipitator gas collection chamber; the discharge port of the first cyclone separator is provided with a first discharge pipe, and the outlet of the first discharge pipe is arranged on the upper side of the inclined pipe of the settler.

Furthermore, a settler inclined tube slide valve is arranged on the settler inclined tube.

Furthermore, a main air conveying pipe is connected to the inclined pipe of the settler, and one end of the main air conveying pipe is connected with a main fan.

Further, a charcoal burner gas collection chamber is arranged at the top of the charcoal burner, a second cyclone separator is arranged in the charcoal burner, and an exhaust port of the second cyclone separator is connected with an inlet of the charcoal burner gas collection chamber; a second discharge pipe is arranged at the discharge port of the second cyclone separator; and the outlet of the second discharging pipe is arranged on the upper side of the vertical pipe of the charcoal burner.

Further, a vertical pipe sliding valve of the charcoal burner is arranged on the vertical pipe of the charcoal burner.

Furthermore, the coke oven riser comprises a first part and a second part, and two sides of the coke oven riser slide valve are respectively connected with the first part and the second part; one end of the first part is connected with the charcoal burner; one end of the second part is connected with the reactor; the pressure of the first portion is greater than the pressure of the second portion.

The utility model has the beneficial effects that:

1. according to the utility model, the fine pipeline group is arranged at the outlet of the vertical pipe of the coke oven, so that the uniform distribution of the coke breeze is facilitated, the accumulation of the coke breeze is prevented, meanwhile, the uniform dispersion of the coke breeze is facilitated, the falling hot coke breeze is uniformly mixed with the feeding pulverized coal, the yield of tar and coal gas is improved, the pulverized coal is more effectively utilized, and the utilization rate of the heat of the coke breeze is increased.

2. The utility model adds a (DN) fine pipeline group in a pipeline from the lower part of a single-acting slide valve of a heat carrier of the coke burning device to the reactor, so that the coke breeze from the coke burning device falls to the reactor and is uniformly mixed with the pulverized coal, and the coal thermal decomposition reaction is generated in the reactor under the lifting action of the coal gas. The device can make coke breeze and fine coal homogeneous mixing, and reactor feeding hybrid system is difficult for blockking up, and reaction tar productivity is high, and the raw materials that do not take place to react are few, and coke breeze whereabouts volume is controllable, easily carries, is difficult for causing the pipe blockage, low cost.

Drawings

Fig. 1 is a schematic structural diagram of an embodiment of the present invention.

Fig. 2 is a schematic structural view of a portion a in fig. 1.

Fig. 3 is a schematic structural diagram of a thin tube bank in an embodiment of the present invention.

In the figure, 1, a gas collecting chamber of a charcoal burner; 2. a second cyclone separator; 201. a second discharge pipe; 3. a charcoal burning device; 4. a charcoal burner riser; 401. a first portion; 402. a second portion; 5. a charcoal burner riser spool valve; 6. a thin pipe group; 601. a channel; 7. a reactor; 8. a precipitator gas collection chamber; 9. a first cyclone separator; 901. a first discharging pipe; 10. a settler; 11. a settler chute slide valve; 12. a settler chute; 13. a conveying gas pipeline; 131. a first delivery conduit; 132. a second delivery conduit; 14. a main air delivery pipe; 15. a main blower.

Detailed Description

In order to make the objects, technical solutions and advantages of the present invention more apparent, the present invention is described in further detail below with reference to the accompanying drawings and embodiments. It should be understood that the specific embodiments described herein are merely illustrative of the utility model and are not intended to limit the utility model.

All other embodiments, which can be derived by a person skilled in the art from the embodiments given herein without making any creative effort, shall fall within the protection scope of the present invention.

Referring to fig. 1 to 3, a static mixer for fast pyrolysis of pulverized coal includes a char burner 3, a reactor 7, and a settler 10.

The char burner 3 is mainly used for performing a combustion reaction on the coke breeze, and the burned coke breeze is used as one of reaction heat sources, namely a solid heat carrier. In this embodiment, a heater (not shown) is connected to the bottom of the char burner 3, and the heater heats and burns coke breeze in the char burner 3. The top of the charcoal burner 3 is provided with a charcoal burner gas collection chamber 1, and the top of the charcoal burner gas collection chamber 1 is provided with a high-temperature flue gas outlet; a second cyclone separator 2 is arranged in the charcoal burner 3, and an exhaust port of the second cyclone separator 2 is connected with an inlet of a gas collection chamber 1 of the charcoal burner. The high-temperature flue gas generated by burning the coke breeze can be separated through the second cyclone separator 2, so that the separated high-temperature flue gas enters the gas collection chamber 1 of the coke burner and enters a subsequent system. In this embodiment, the second cyclone separator 2 is a conventional cyclone separator, and the structure thereof will not be described herein. Of course, the bottom solid outlet of the second cyclone separator 2 is provided with an elbow nozzle, and the elbow nozzle is arranged to prevent high-temperature flue gas from entering the second cyclone separator 2.

The bottom outlet of the charcoal burner 3 is connected with a charcoal burner vertical pipe 4; the discharge port of the second cyclone 2 is provided with a second discharge pipe 201; the outlet of the second discharging pipe 201 is arranged on the upper side of the vertical pipe 4 of the coke burning device. Referring to fig. 2, a vertical pipe slide valve 5 of the charcoal burner is provided on the vertical pipe 4 of the charcoal burner. The char burner riser spool valve 5 is used primarily to regulate the amount of coke breeze that falls into the reactor 7. Specifically, the char former riser 4 comprises a first portion 401 and a second portion 402, and both sides of the char former riser spool 5 are connected with the first portion 401 and the second portion 402, respectively; one end of the first part 401 is connected with the charking device 3; one end of the second portion 402 is connected to the reactor 7; the pressure of the first portion 401 is greater than the pressure of the second portion 402. In this embodiment, the coke breeze in the char burner 3 passes through the char burner riser 4 and then passes through the char burner riser slide valve 5 and then enters the reactor 7, wherein a certain pressure difference is controlled before and after the char burner riser slide valve 5 to prevent the coal gas in the reactor 7 from entering the char burner 3.

In order to be more beneficial to the homogeneous distribution of the coke breeze, the outlet of the vertical pipe 4 of the coke burner is provided with a thin pipe group 6; the outlet of the fine tube bank 6 is arranged in the inlet end of the reactor 7. The length of the portion of the thin tube group 6 located inside the inlet end of the reactor 7 decreases in sequence in the direction of flow of the conveying gas. For example, as shown in fig. 2, when the top of the thin tube group is a plane, the bottom of the thin tube group 6 is an inclined plane, and the inlet end of the reactor 7 is set to the left, the lengths of the thin tube group 6 decrease from left to right, the length of the thin tube group 6 on the left side is the longest, and the left side has the transport gas. This prevents the conveying gas from blowing back into the narrow tube bank 6.

Referring to fig. 3, the cross section of the thin tube set 6 is elliptical. The thin tube bank 6 has a plurality of channels 601 therein, each channel 601 communicating with the inlet end of the reactor 7. The lengths of the channels 601 are not uniform and decrease in sequence along the flow direction of the conveying gas, so that the outlet of the thin tube set 6 presents an inclined plane facing the flow direction of the conveying gas in the reactor 7. In this embodiment, set up thin pipeline group 6 through the export at char-combusting device riser 4, more be favorable to the homogeneous phase distribution of coke breeze, prevent that the coke breeze from piling up, the even dispersion of coke breeze more is favorable to with fine coal misce bene simultaneously, has improved the productivity of tar and coal gas, and more effective utilization fine coal, increased the thermal utilization ratio of coke breeze.

In this embodiment, the diameter of the channel 601 is too small, so that the coke breeze is not easy to fall; if the pipe diameter is too large, coke breeze is easy to accumulate below the channel 601, and the mixing effect with pulverized coal is poor. Thus, the present embodiment selects the tube diameter of the fine tube bank 6 as DN15, and then calculates the riser tube diameter from the charbroiler riser spool valve 5 to the second section 402 of the reactor 7 by selecting the appropriate number of channels 601 of the fine tube bank 6.

According to 2n ═ (D/ad), where n is the number of channels 601; d is the riser pipe diameter of the second section 402; a is coefficient, and 1.5-1.7 is taken; d is the tube diameter of the channel 601 in the thin tube group 6. If n is 50, a is 1.5, and D is 15mm, D is 2250 mm.

The reactor 7 is mainly used for uniformly mixing the high-temperature coke breeze and the pulverized coal, completing heat exchange and generating a rapid thermal decomposition reaction of the pulverized coal. The inlet end of the reactor 7 is connected with a conveying gas pipeline 13, and the outlet of the thin pipeline group 6 is arranged in the inlet end of the reactor 7 and is positioned at one side of the conveying gas pipeline 13. Wherein, the gas conveying pipeline 13 can convey gas, and then the hot coke breeze falling from the thin pipeline group 6 is blown to the middle part of the reactor 7 in time, and in the process, the high-temperature coke breeze is uniformly mixed with the pulverized coal to complete heat exchange, and the rapid thermal decomposition reaction of the pulverized coal occurs. In this embodiment, the gas delivery pipe 13 includes a first delivery pipe 131 and a second delivery pipe 132. The first transfer pipe 131 is used to supply preheated gas for transferring pulverized coal, and the second transfer pipe 132 is used to supply self-produced cold gas for transferring pulverized coke. The preheated coal gas and the self-produced cold coal gas are coal gas obtained by performing a series of subsequent separation, purification and purification on the self-produced separated oil gas in the embodiment, and are directly used for the pulverized coal fast pyrolysis reaction static mixing device in the embodiment after being pressurized. The temperature in the reactor 7 should reach the temperature of the coal pyrolysis reaction, and the coal pyrolysis reaction mainly generates tar, coke breeze and oil gas. This application utilizes the coal gas of self-production can form cyclic utilization, in reduction in production cost, can also promote the homogeneous mixing of powdered coke and fine coal to make the difficult jam of reactor feeding hybrid system, reaction tar productivity is high, and the raw materials that do not take place the reaction are few.

Referring to fig. 1 again, the settler 10 is mainly used for separating oil gas carried by coke breeze generated by reaction. A first cyclone separator 9 is arranged in the settler 10, and the outlet end of the reactor 7 extends into the settler 10 and is connected with the inlet of the side wall of the first cyclone separator 9. In this embodiment, the first cyclone 9 is a conventional cyclone, and the structure thereof will not be described herein.

The top of the settler 10 is provided with a settler gas collection chamber 8, and an exhaust port of the first cyclone separator 9 is connected with an inlet of the settler gas collection chamber 8; the discharge opening of the first cyclone 9 is provided with a first discharge pipe 901, and the outlet of the first discharge pipe 901 is arranged on the upper side of the settler chute 12. The bottom outlet of the settler 10 is connected with a settler inclined tube 12, and the outlet of the settler inclined tube 12 is connected with the inlet of the charcoal burner 3.

After oil gas carried by the coke breeze generated by the reactor 7 is separated by the first cyclone separator 9, the coke breeze falls back to the precipitator 10 and falls into the charcoal burner 3 through the precipitator inclined tube 12, and the separated oil gas enters a subsequent purification system. The fine coke produced by the reactor 7 carries oil gas, and when entering the first cyclone separator 9, a certain linear velocity is required to be kept, so that a good separation effect can be ensured, and the oil gas is prevented from carrying the fine coke and entering a subsequent system.

The coke breeze falls into the coke burning device 3 through the settler inclined tube 12, and the settler inclined tube 12 is provided with a settler inclined tube slide valve 11. A certain pressure difference is controlled before and after the inclined tube slide valve 11 of the settler to prevent main air of the charcoal burner 3 from entering the settler 10. For example, the settler chute 12 comprises a front section and a rear section, and both sides of the settler chute slide valve 11 are connected with the front section and the rear section, respectively; the front section is connected with the charcoal burning device 3, and the rear section is connected with the settler 10; the pressure of the front section is lower than that of the rear section, thereby preventing the main air of the char-combusting device 3 from entering the settler 10.

Further preferably, the settler inclined tube 12 is connected with a main air conveying pipe 14, and one end of the main air conveying pipe 14 is connected with a main fan 15. After being pressurized by the main fan 15, the air enters the coke burning device 3 through the main air conveying pipe 14, on one hand, coke breeze in the inclined pipe 12 of the settler can be uniformly scattered into the coke burning device 3, on the other hand, as the coke breeze is burnt in the coke burning device 3, the main reaction is an oxidation reaction, and therefore, the air can also provide oxygen required by the oxidation reaction of the coke burning device 3 through the main air conveying pipe 14. High-temperature flue gas generated by burning the coke breeze needs a certain linear velocity to enter the second cyclone separator, so that the separation effect of the second cyclone separator is ensured, and the oil gas carrying the coke breeze is prevented from entering a subsequent system and blocking the subsequent system. And the burnt coke breeze falls into a fine pipeline group 6 of a carbon burner vertical pipe 4 from the carbon burner 3 through a carbon burner vertical pipe slide valve 5, and the coke breeze falls into a reactor 7 from the fine pipeline group 6.

The method is implemented according to the following steps:

step one, feeding the coke breeze generated in a reactor 7 into a coke burning device 3 through a settler inclined tube 12, and introducing main air through a main air blower 15 to burn the coke breeze, wherein the temperature of the coke burning device 3 is about 700 ℃, and the pressure is about 0.2 MPa;

step two, sending pulverized coal to a reactor 7 through self-produced coal gas, simultaneously, enabling high-temperature coke breeze in a coke oven 3 to fall to the reactor 7 through a coke oven vertical pipe 4, a coke oven vertical pipe slide valve 5 and a fine pipeline group 6, mixing the two, generating a coal thermal decomposition reaction in the reactor 7 under the lifting action of the coal gas, separating the reacted coke breeze and oil gas through a first cyclone separator 9 of a settler 10, and enabling the separated oil gas to enter a subsequent system; wherein, the heat source of the reaction: firstly, the burnt coke breeze in the charcoal burner is used as a solid heat carrier; secondly, the coal gas is used as a gas heat carrier, the advantages of the two heat carriers are combined by using two different heat carrier process technologies, the flow of the gas is utilized to drive the back mixing of the coke breeze and the pulverized coal, the mass transfer and heat transfer processes are accelerated, the high-temperature coke breeze can realize high-efficiency heat transfer, and the coal pyrolysis reaction of the pulverized coal in the reactor 7 is ensured. Certainly, the self-produced coal gas can also be used as a conveying and lifting medium, and the milled pulverized coal and the self-produced coal gas are mixed and then enter the lifting tubular reactor under the lifting action of the coal gas and are mixed with the hot pulverized coke from the vertical pipe 4 of the coke burner to generate the rapid thermal decomposition reaction of the coal.

Thirdly, the coke breeze separated by the second cyclone separator 9 passes through a settler inclined tube 12 and a settler inclined tube slide valve 11 and falls into the charcoal burner 3 under the action of conveying gas, and is used as a coal thermal decomposition heat source after combustion reaction;

fourthly, high-temperature flue gas generated by burning the coke breeze in the coke burner 3 enters a subsequent system after passing through the second cyclone separator 2 for further separation and application; the gas obtained by separating and purifying the oil gas separated by the first cyclone separator 9 is used as the conveying gas for reaction to circulate.

In this embodiment, the ratio of the hot coke breeze to the pulverized coal should be far greater than that of the pulverized coal, because the heat source is mainly provided by the coke breeze, the temperature of the pulverized coal subjected to the low-temperature pyrolysis reaction is most suitable for 500-650 ℃, and the low-rank coal is mostly subjected to low-temperature pyrolysis to obtain high-yield tar and coal gas, the temperature of the reactor 7 is controlled to be about 500-550 ℃, the pressure of the reactor 7 is controlled to be lower than that of the char burner 3, the reaction product in the reactor 7 enters the settler 10 for separation, and the pressure of the settler 10 is basically the same as that of the reactor 7. In this embodiment, the device makes hot fine coke powder fall to reactor 7 more evenly through install thin pipeline group 6 additional between the pipeline at carbonado riser spool valve 5 to reactor 7, again with the even mixture of fine coal, make being heated of fine coal bigger degree, improved hot fine coke powder's utilization ratio, the fine coal that does not take place the reaction is few, reaction tar productivity is high, and can make the difficult jam of feeding hybrid system in the reactor 7, the fine coke falling volume is controllable, easily carries, low cost.

The present invention is not limited to the above preferred embodiments, and any modifications, equivalent substitutions and improvements made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (10)

1. The utility model provides a static mixing arrangement of fast pyrolysis reaction of fine coal which characterized in that includes:

the bottom outlet of the charcoal burner (3) is connected with a charcoal burner vertical pipe (4); a fine pipeline group (6) is arranged at the outlet of the vertical pipe (4) of the charcoal burner;

the inlet end of the reactor (7) is connected with a conveying gas pipeline (13), and the outlet of the fine pipeline group (6) is arranged in the inlet end of the reactor (7) and is positioned on one side of the conveying gas pipeline (13);

the device comprises a settler (10), wherein a first cyclone separator (9) is arranged in the settler (10), and the outlet end of the reactor (7) extends into the settler (10) and is connected with the first cyclone separator (9); the bottom outlet of the settler (10) is connected with a settler inclined tube (12), and the outlet of the settler inclined tube (12) is connected with the inlet of the charcoal burner (3).

2. The pulverized coal fast pyrolysis reaction static mixing device according to claim 1, characterized in that the length of the portion of the fine pipe group (6) located in the inlet end of the reactor (7) decreases in sequence in the flow direction of the conveying gas.

3. The pulverized coal fast pyrolysis reaction static mixing device according to claim 1, wherein the cross section of the fine duct group (6) is elliptical.

4. The pulverized coal fast pyrolysis reaction static mixing device according to claim 1, characterized in that a plurality of channels (601) are provided in the fine duct group (6), and each channel (601) is communicated with an inlet end of the reactor (7).

5. The static mixing device for the pulverized coal fast pyrolysis reaction as claimed in claim 1, wherein a settler gas collection chamber (8) is arranged at the top of the settler (10), and the exhaust port of the first cyclone separator (9) is connected with the inlet of the settler gas collection chamber (8); a first discharging pipe (901) is arranged at a discharging port of the first cyclone separator (9), and an outlet of the first discharging pipe (901) is arranged on the upper side of the settler inclined pipe (12).

6. The pulverized coal fast pyrolysis reaction static mixing device according to claim 1, wherein a settler chute slide valve (11) is provided on the settler chute (12).

7. The pulverized coal fast pyrolysis reaction static mixing device according to claim 1, wherein a main air conveying pipe (14) is connected to the settler inclined pipe (12), and one end of the main air conveying pipe (14) is connected to a main fan (15).

8. The static mixing device for the pulverized coal fast pyrolysis reaction as claimed in claim 1, wherein a gas collection chamber (1) of the char burner (3) is arranged at the top of the char burner (3), a second cyclone separator (2) is arranged in the char burner (3), and an exhaust port of the second cyclone separator (2) is connected with an inlet of the gas collection chamber (1) of the char burner; a second discharge pipe (201) is arranged at the discharge outlet of the second cyclone separator (2); the outlet of the second discharging pipe (201) is arranged on the upper side of the vertical pipe (4) of the charcoal burner.

9. The pulverized coal fast pyrolysis reaction static mixing device according to claim 1, characterized in that a vertical pipe sliding valve (5) of the char burner is arranged on the vertical pipe (4) of the char burner.

10. The pulverized coal fast pyrolysis reaction static mixing device according to claim 9, wherein the char former stand pipe (4) comprises a first part (401) and a second part (402), and both sides of the char former stand pipe slide valve (5) are respectively connected with the first part (401) and the second part (402); one end of the first part (401) is connected with the charcoal burner (3); one end of the second part (402) is connected to the reactor (7); the pressure of the first portion (401) is greater than the pressure of the second portion (402).

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