阅读说明：本技术 一种低氮气耗量的干煤粉气化除灰系统 (Dry pulverized coal gasification ash removal system with low nitrogen consumption ) 是由 樊强 贾会林 许世森 任永强 陶继业 刘刚 李小宇 刘沅 陈智 王鹏杰 罗丽珍 于 2021-03-12 设计创作，主要内容包括：本发明公开了一种低氮气耗量的干煤粉气化除灰系统,包括合成气输入管道、第一阀门、旋风除尘器、第二阀门、陶瓷过滤器、第一减压管、第二减压管、第一气提罐、第二气提罐、第三减压管、第四减压管、第一飞灰加速器、输灰管道、第二飞灰加速器、热低压氮气管道及合成气输出管道,该系统通过设置减压管替代了传统的飞灰锁斗及其反吹系统,反吹氮气用量较小,投资成本和能耗较低。(The invention discloses a dry coal powder gasification ash removal system with low nitrogen consumption, which comprises a synthesis gas input pipeline, a first valve, a cyclone dust collector, a second valve, a ceramic filter, a first pressure reducing pipe, a second pressure reducing pipe, a first gas stripping tank, a second gas stripping tank, a third pressure reducing pipe, a fourth pressure reducing pipe, a first fly ash accelerator, an ash conveying pipeline, a second fly ash accelerator, a hot low-pressure nitrogen pipeline and a synthesis gas output pipeline.)

1. The dry coal powder gasification ash removal system with low nitrogen consumption is characterized by comprising a synthetic gas input pipeline, a first valve, a cyclone dust collector (1), a second valve, a ceramic filter (2), a first pressure reducing pipe (3), a second pressure reducing pipe (4), a first gas stripping tank (7), a second gas stripping tank (8), a third pressure reducing pipe (5), a fourth pressure reducing pipe (6), a first fly ash accelerator (14), an ash conveying pipeline, a second fly ash accelerator (15), a hot low-pressure nitrogen pipeline and a synthetic gas output pipeline;

the outlet of the synthesis gas input pipeline is divided into two paths, wherein one path is communicated with the inlet of the cyclone dust collector (1) through a first valve, the other path is communicated with the inlet of the ceramic filter (2) through a second valve, the outlet at the top of the cyclone dust collector (1) is communicated with the inlet of the ceramic filter (2), the outlet at the bottom of the cyclone dust collector (1) is communicated with the inlet of the first pressure reducing pipe (3) and the inlet of the second pressure reducing pipe (4), the outlet of the first pressure reducing pipe (3) is communicated with the inlet of the first air stripping tank (7), the outlet of the second pressure reducing pipe (4) is communicated with the inlet of the second air stripping tank (8), the outlet at the bottom of the ceramic filter (2) is communicated with the inlet of the third pressure reducing pipe (5) and the inlet of the fourth pressure reducing pipe (6), the outlet of the third pressure reducing pipe (5) is communicated with the inlet of the first air stripping tank (7), and the outlet of the fourth pressure reducing pipe (6) is communicated with the inlet of the second air stripping tank (8;

the outlet of the first stripping tank (7) is communicated with an ash conveying pipeline through a first fly ash accelerator (14), and the outlet of the second stripping tank (8) is communicated with the ash conveying pipeline through a second fly ash accelerator (15);

the hot low-pressure nitrogen pipeline is communicated with a first fly ash accelerator (14), a second fly ash accelerator (15), a back-blowing inlet on the side surface of the first gas stripping tank (7), a back-blowing inlet on the side surface of the second gas stripping tank (8), a back-blowing inlet at the bottom of the first gas stripping tank (7) and a back-blowing inlet at the bottom of the second gas stripping tank (8);

the top outlet of the first stripping tank (7) is communicated with the inlet of a first stripping filter (9), and the top outlet of the second stripping tank (8) is communicated with the inlet of a second stripping filter (10);

the top outlet of the ceramic filter (2) is communicated with a synthesis gas output pipeline.

2. The dry pulverized coal gasification ash removal system with low nitrogen consumption according to claim 1, characterized in that a hot low-pressure nitrogen pipeline passes through a first back-blowing nitrogen buffer tank (11) and a back-blowing inlet of the first stripping filter (9).

3. The dry pulverized coal gasification ash removal system with low nitrogen consumption according to claim 1, characterized in that a hot low-pressure nitrogen pipeline is communicated with a blowback inlet of the second gas stripping filter (10) through a second blowback nitrogen buffer tank (12).

4. The dry pulverized coal gasification ash removal system with low nitrogen consumption according to claim 1, further comprising a hot high-pressure nitrogen pipeline and a hot high-pressure nitrogen buffer tank (13), wherein the hot high-pressure nitrogen pipeline is communicated with the back-blowing gas inlet of the ceramic filter (2) through the hot high-pressure nitrogen buffer tank (13).

5. The dry pulverized coal gasification ash removal system with low nitrogen consumption according to claim 1, wherein a hot low-pressure nitrogen pipeline is communicated with a back-blowing inlet on the side of the first stripping tank (7) and a back-blowing inlet on the side of the second stripping tank (8).

6. The dry pulverized coal gasification ash removal system with low nitrogen consumption according to claim 1, characterized in that a hot low-pressure nitrogen pipeline is communicated with a blowback inlet at the bottom of the first stripping tank (7) and a blowback inlet at the bottom of the second stripping tank (8).

7. The dry pulverized coal gasification ash removal system with low nitrogen consumption according to claim 1, characterized in that the outlet of the first pressure reducing pipe (3) is communicated with the inlet of the first stripping tank (7) through a third valve.

8. The dry pulverized coal gasification ash removal system with low nitrogen consumption according to claim 7, characterized in that the outlet of the second pressure reducing pipe (4) is connected to the inlet of the second stripping tank (8) via a fourth valve.

9. The dry pulverized coal gasification ash removal system with low nitrogen consumption according to claim 8, characterized in that the outlet of the third pressure reducing pipe (5) is communicated with the inlet of the first stripping tank (7) through a fifth valve.

10. The dry pulverized coal gasification ash removal system with low nitrogen consumption according to claim 9, characterized in that the outlet of the fourth pressure reducing pipe (6) is communicated with the inlet of the second stripping tank (8) via a sixth valve.

Technical Field

The invention belongs to the technical field of coal gasification, and relates to a dry coal powder gasification ash removal system with low nitrogen consumption.

Background

Coal gasification is an important process technology in the field of IGCC power generation and coal chemical industry, and synthesis gas generated by a coal gasification furnace cannot be directly utilized due to large ash content, and usually enters a subsequent system after being subjected to ash removal treatment and washing.

After the crude synthesis gas generated by the gasification furnace enters a cyclone separator of an ash removal system, the synthesis gas is separated from ash, and the separated ash is collected by a fly ash collecting tank and is discharged into a fly ash lock hopper at regular time. The fly ash lock hopper adopts variable pressure and intermittent operation. And the fly ash lock hopper is communicated with a fly ash filter to collect ash under a high pressure state, and when the ash collection timer reaches a preset time or a high material level appears, the fly ash lock hopper is cut off from upstream and downstream equipment, and the pressure is released through the exhaust filter. And after the pressure relief is finished, opening a valve at the bottom of the fly ash lock bucket, discharging the fly ash into a fly ash gas stripping tank, and carrying out gas stripping by using hot low-pressure nitrogen. Like this kind of conventional lock fill pressure release technology, investment cost is higher, and erects the frame height, and the quantity of blowback nitrogen gas is great. The temperature of the back-flushing nitrogen is generally 225 ℃ and 5.0MPa, so the energy consumption is higher.

Therefore, it is necessary to develop a dry pulverized coal gasification ash removal system with low energy consumption to solve the above problems.

Disclosure of Invention

The invention aims to overcome the defects of the prior art and provides a dry coal powder gasification ash removal system with low nitrogen consumption, which has the advantages of small back-flushing nitrogen consumption and low investment cost.

In order to achieve the aim, the dry coal powder gasification ash removal system with low nitrogen consumption comprises a synthesis gas input pipeline, a first valve, a cyclone dust collector, a second valve, a ceramic filter, a first pressure reducing pipe, a second pressure reducing pipe, a first gas stripping tank, a second gas stripping tank, a third pressure reducing pipe, a fourth pressure reducing pipe, a first fly ash accelerator, an ash conveying pipeline, a second fly ash accelerator, a hot low-pressure nitrogen pipeline and a synthesis gas output pipeline;

the outlet of the synthesis gas input pipeline is divided into two paths, wherein one path is communicated with the inlet of the cyclone dust collector through a first valve, the other path is communicated with the inlet of the ceramic filter through a second valve, the outlet of the top of the cyclone dust collector is communicated with the inlet of the ceramic filter, the outlet of the bottom of the cyclone dust collector is communicated with the inlet of the first pressure reducing pipe and the inlet of the second pressure reducing pipe, the outlet of the first pressure reducing pipe is communicated with the inlet of the first gas stripping tank, the outlet of the second pressure reducing pipe is communicated with the inlet of the second gas stripping tank, the outlet of the bottom of the ceramic filter is communicated with the inlet of the third pressure reducing pipe and the inlet of the fourth pressure reducing pipe, the outlet of the third pressure reducing pipe is communicated with the inlet of the first gas stripping tank, and the outlet of the fourth pressure reducing pipe is communicated with the;

the outlet of the first gas stripping tank is communicated with the ash conveying pipeline through a first fly ash accelerator, and the outlet of the second gas stripping tank is communicated with the ash conveying pipeline through a second fly ash accelerator;

the hot low-pressure nitrogen pipeline is communicated with the first fly ash accelerator, the second fly ash accelerator, the back-blowing inlet on the side surface of the first gas stripping tank, the back-blowing inlet on the side surface of the second gas stripping tank, the back-blowing inlet at the bottom of the first gas stripping tank and the back-blowing inlet at the bottom of the second gas stripping tank;

the top outlet of the first stripping tank is communicated with the inlet of the first stripping filter, and the top outlet of the second stripping tank is communicated with the inlet of the second stripping filter;

the top outlet of the ceramic filter is communicated with a synthesis gas output pipeline.

The hot low-pressure nitrogen pipeline passes through the first back-blowing nitrogen buffer tank and the back-blowing inlet of the first stripping filter.

The hot low-pressure nitrogen pipeline is communicated with a back-blowing inlet of the second gas stripping filter through a second back-blowing nitrogen buffer tank.

The device also comprises a hot high-pressure nitrogen pipeline and a hot high-pressure nitrogen buffer tank, wherein the hot high-pressure nitrogen pipeline is communicated with the back-blowing inlet of the ceramic filter through the hot high-pressure nitrogen buffer tank.

The hot low-pressure nitrogen pipeline is communicated with a back-blowing inlet on the side surface of the first gas stripping tank and a back-blowing inlet on the side surface of the second gas stripping tank.

The hot low-pressure nitrogen pipeline is communicated with a back-blowing inlet at the bottom of the first gas stripping tank and a back-blowing inlet at the bottom of the second gas stripping tank.

The outlet of the first pressure reducing pipe is communicated with the inlet of the first stripping tank through a third valve.

The outlet of the second pressure reducing pipe is communicated with the inlet of the second stripping tank through a fourth valve.

The outlet of the third pressure reducing pipe is communicated with the inlet of the first stripping tank through a fifth valve.

The outlet of the fourth decompression pipe is communicated with the inlet of the second stripping tank through a sixth valve.

The invention has the following beneficial effects:

in addition, the invention replaces the traditional fly ash lock hopper system by the first pressure reducing pipe, the second pressure reducing pipe, the third pressure reducing pipe and the fourth pressure reducing pipe so as to reduce the cost, reduce the height of a fixed frame and reduce the consumption of back flushing nitrogen.

Drawings

The accompanying drawings, which are incorporated in and constitute a part of this specification, are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification, illustrate exemplary embodiments of the invention and together with the description serve to explain the invention and not to limit the invention. In the drawings:

FIG. 1 is a schematic structural diagram of the present invention.

Wherein, 1 is a cyclone dust collector, 2 is a ceramic filter, 3 is a first decompression pipe, 4 is a second decompression pipe, 5 is a third decompression pipe, 6 is a fourth decompression pipe, 7 is a first stripping tank, 8 is a second stripping tank, 9 is a first stripping filter, 10 is a second stripping filter, 11 is a first back-blowing nitrogen buffer tank, 12 is a second back-blowing nitrogen buffer tank, 13 is a hot high-pressure nitrogen buffer tank, 14 is a first fly ash accelerator, and 15 is a second fly ash accelerator.

Detailed Description

The present invention will be described in detail below with reference to the embodiments with reference to the attached drawings. It should be noted that the embodiments and features of the embodiments in the present application may be combined with each other without conflict.

The following detailed description is exemplary in nature and is intended to provide further details of the invention. Unless otherwise defined, all technical terms used herein have the same meaning as commonly understood by one of ordinary skill in the art to which this application belongs. The terminology used herein is for the purpose of describing particular embodiments only and is not intended to be limiting of exemplary embodiments according to the invention.

Referring to fig. 1, the dry pulverized coal gasification ash removal system with low nitrogen consumption according to the present invention comprises a synthesis gas input pipeline, a first valve, a cyclone dust collector 1, a second valve, a ceramic filter 2, a first pressure reducing pipe 3, a second pressure reducing pipe 4, a first gas stripping tank 7, a second gas stripping tank 8, a third pressure reducing pipe 5, a fourth pressure reducing pipe 6, a first fly ash accelerator 14, an ash conveying pipeline, a second fly ash accelerator 15, a hot low-pressure nitrogen pipeline, and a synthesis gas output pipeline; the outlet of the synthesis gas input pipeline is divided into two paths, wherein one path is communicated with the inlet of the cyclone dust collector 1 through a first valve, the other path is communicated with the inlet of the ceramic filter 2 through a second valve, the outlet at the top of the cyclone dust collector 1 is communicated with the inlet of the ceramic filter 2, the outlet at the bottom of the cyclone dust collector 1 is communicated with the inlet of the first pressure reducing pipe 3 and the inlet of the second pressure reducing pipe 4, the outlet of the first pressure reducing pipe 3 is communicated with the inlet of the first gas stripping tank 7, the outlet of the second pressure reducing pipe 4 is communicated with the inlet of the second gas stripping tank 8, the outlet at the bottom of the ceramic filter 2 is communicated with the inlet of the third pressure reducing pipe 5 and the inlet of the fourth pressure reducing pipe 6, the outlet of the third pressure reducing pipe 5 is communicated with the inlet of the first gas stripping tank 7, and the outlet of the fourth pressure reducing pipe 6 is communicated with the inlet; the outlet of the first gas stripping tank 7 is communicated with an ash conveying pipeline through a first fly ash accelerator 14, and the outlet of the second gas stripping tank 8 is communicated with the ash conveying pipeline through a second fly ash accelerator 15; the hot low-pressure nitrogen pipeline is communicated with a first fly ash accelerator 14, a second fly ash accelerator 15, a back-blowing inlet on the side surface of the first gas stripping tank 7, a back-blowing inlet on the side surface of the second gas stripping tank 8, a back-blowing inlet at the bottom of the first gas stripping tank 7 and a back-blowing inlet at the bottom of the second gas stripping tank 8; the top outlet of the first stripping tank 7 is communicated with the inlet of a first stripping filter 9, and the top outlet of the second stripping tank 8 is communicated with the inlet of a second stripping filter 10; the top outlet of the ceramic filter 2 is communicated with a synthesis gas output pipeline.

When the device works, the synthetic gas output by the synthetic gas input pipeline is divided into two paths, wherein one path of the synthetic gas enters the cyclone dust collector 1 for dust removal, the other path of the synthetic gas enters the ceramic filter 2 for filtering through the second valve, the synthetic gas output by the cyclone dust collector 1 enters the ceramic filter 2, the dust output from the bottom of the cyclone dust collector 1 enters the first pressure reducing pipe 3 and the second pressure reducing pipe 4, the dust output by the ceramic filter 2 enters the third pressure reducing pipe 5 and the fourth pressure reducing pipe 6, the dust output by the first pressure reducing pipe 3 enters the first air stripping tank 7 through the third valve for air stripping, the dust output by the second pressure reducing pipe 4 enters the second air stripping tank 8 through the fourth valve for air stripping, the dust output by the third pressure reducing pipe 5 enters the first air stripping tank 7 through the fifth valve for air stripping, the dust output by the fourth pressure reducing pipe 6 enters the second air stripping tank 8 through the sixth valve for air stripping, the gas output by the first gas stripping tank 7 is discharged after being filtered by the first gas stripping filter 9, the gas output by the second gas stripping tank 8 is discharged after being filtered by the second gas stripping filter 10, the dust output by the first gas stripping tank 7 is output by the first fly ash accelerator 14, and the dust output by the second gas stripping tank 8 is output by the second fly ash accelerator 15.

Further, a hot low-pressure nitrogen pipeline passes through the first back-blowing nitrogen buffer tank 11 and the back-blowing inlet of the first stripping filter 9. The low-pressure nitrogen gas output by the hot low-pressure nitrogen gas pipeline passes through the first back-blowing nitrogen gas buffer tank 11 and then is input into the first stripping filter 9 to carry out back-blowing on the first stripping filter 9.

Further, the hot low-pressure nitrogen pipeline is communicated with a back-blowing inlet of the second gas stripping filter 10 through a second back-blowing nitrogen buffer tank 12, and low-pressure nitrogen output by the hot low-pressure nitrogen pipeline is input into the second gas stripping filter 10 through the second back-blowing nitrogen buffer tank 12 to back-blow the second gas stripping filter 10.

Further, still include hot high-pressure nitrogen gas pipeline and hot high-pressure nitrogen gas buffer tank 13, hot high-pressure nitrogen gas pipeline is linked together through hot high-pressure nitrogen gas buffer tank 13 and ceramic filter 2's blowback gas entry, and the high-pressure nitrogen gas of hot high-pressure nitrogen gas pipeline output carries out the blowback to ceramic filter 2 in the hot high-pressure nitrogen gas buffer tank 13 input ceramic filter 2.

Further, a hot low-pressure nitrogen pipeline is communicated with a back-blowing inlet on the side surface of the first gas stripping tank 7 and a back-blowing inlet on the side surface of the second gas stripping tank 8, and low-pressure nitrogen output by the hot low-pressure nitrogen pipeline is counted into the first gas stripping tank 7 and the second gas stripping tank 8 to carry out back-blowing on the first gas stripping tank 7 and the second gas stripping tank 8.

Furthermore, the hot low-pressure nitrogen pipeline is communicated with a back-blowing inlet at the bottom of the first gas stripping tank 7 and a back-blowing inlet at the bottom of the second gas stripping tank 8, and low-pressure nitrogen output by the hot low-pressure nitrogen pipeline enters the back-blowing inlet at the bottom of the first gas stripping tank 7 and the back-blowing inlet at the bottom of the second gas stripping tank 8 to perform back-blowing on the pipeline.

Further, the outlet of the first pressure reducing pipe 3 is communicated with the inlet of the first stripping tank 7 through a third valve; the outlet of the second pressure reducing pipe 4 is communicated with the inlet of the second stripping tank 8 through a fourth valve; the outlet of the third pressure reducing pipe 5 is communicated with the inlet of the first stripping tank 7 through a fifth valve; an outlet of the fourth decompression pipe 6 is communicated with an inlet of the second stripping tank 8 through a sixth valve, and dust is controlled to enter the first stripping tank 7 or the second stripping tank 8 by adjusting the third valve, the fourth valve, the fifth valve and the sixth valve, so that the first stripping tank 7 and the second stripping tank 8 can be used.

Finally, it should be noted that: the above embodiments are only for illustrating the technical solutions of the present invention and not for limiting the same, and although the present invention is described in detail with reference to the above embodiments, those of ordinary skill in the art should understand that: modifications and equivalents may be made to the embodiments of the invention without departing from the spirit and scope of the invention, which is to be covered by the claims.