阅读说明：本技术 合成气生成装置及生活垃圾高温气化生产合成气的方法 (Synthetic gas generating device and method for producing synthetic gas by high-temperature gasification of household garbage ) 是由 吴龙 吕志辉 康啸奇 张旭 于 2019-08-27 设计创作，主要内容包括：本发明公开了一种合成气生成装置及生活垃圾高温气化生产合成气的方法。合成气生成装置包括流化床气化炉及气固分离器；流化床气化炉用于生活垃圾的高温气化并生成合成气,流化床气化炉的顶部设有出气口,流化床气化炉的下部设有半焦氧化区,半焦氧化区的温度高于1300℃；气固分离器用于将合成气中的固体颗粒分离；气固分离器具有进气口及下料口,气固分离器的进气口与流化床气化炉的出气口相连通,气固分离器的下料口与半焦氧化区连通。本发明利用气固分离器将合成气中包括飞灰的固体颗粒分离出来,并输送至高温的半焦氧化区,从而将固体颗粒熔融软化并与炉渣粘合,实现对固体颗粒的固化,也实现了对飞灰的固化,避免了飞灰进入合成气内。(The invention discloses a synthesis gas generation device and a method for producing synthesis gas by high-temperature gasification of household garbage. The synthesis gas generating device comprises a fluidized bed gasification furnace and a gas-solid separator; the fluidized bed gasification furnace is used for high-temperature gasification of household garbage and generating synthesis gas, the top of the fluidized bed gasification furnace is provided with a gas outlet, the lower part of the fluidized bed gasification furnace is provided with a semicoke oxidation area, and the temperature of the semicoke oxidation area is higher than 1300 ℃; the gas-solid separator is used for separating solid particles in the synthesis gas; the gas-solid separator is provided with a gas inlet and a feed opening, the gas inlet of the gas-solid separator is communicated with the gas outlet of the fluidized bed gasification furnace, and the feed opening of the gas-solid separator is communicated with the semicoke oxidation zone. The invention separates solid particles including fly ash from the synthesis gas by using the gas-solid separator, and conveys the solid particles to the high-temperature semicoke oxidation area, thereby melting and softening the solid particles and bonding the solid particles with the slag, realizing the solidification of the solid particles, also realizing the solidification of the fly ash, and avoiding the fly ash from entering the synthesis gas.)

1. A synthetic gas generating device is used for high-temperature gasification of household garbage and generation of synthetic gas, and is characterized by comprising a fluidized bed gasification furnace and a gas-solid separator;

the fluidized bed gasification furnace is used for high-temperature gasification of the household garbage and generating synthesis gas, the top of the fluidized bed gasification furnace is provided with a gas outlet, the lower part of the fluidized bed gasification furnace is provided with a semicoke oxidation area, and the temperature of the semicoke oxidation area is higher than 1300 ℃;

the gas-solid separator is used for separating solid particles in the synthesis gas; the gas-solid separator is provided with a gas inlet and a feed opening, the gas inlet of the gas-solid separator is communicated with the gas outlet of the fluidized bed gasification furnace, and the feed opening of the gas-solid separator is communicated with the semicoke oxidation zone.

2. The syngas generation apparatus of claim 1, further comprising a gas distribution plate, a slag discharge pipe, and a first gas inlet pipe;

the gas distribution plate is arranged at the bottom of the semicoke oxidation zone, the gas distribution plate is in an inverted cone shape, and the large end of the gas distribution plate is connected with the side wall of the fluidized bed gasification furnace;

one end of the slag discharging pipe is connected with the small end of the gas distribution plate, and the other end of the slag discharging pipe extends downwards to the outer side of the bottom plate of the synthetic gas generating device;

the first air inlet pipe is arranged inside the slag discharging pipe, the axis of the first air inlet pipe coincides with the axis of the slag discharging pipe, the first air inlet pipe is used for introducing an oxidant and fuel gas, a nozzle is arranged at the end part of the first air inlet pipe, and the oxidant and the fuel gas are sprayed into the semicoke oxidation area through the nozzle to be combusted, so that the temperature of the semicoke oxidation area is higher than 1300 ℃.

3. The syngas generation apparatus of claim 2, wherein the gas-solid separator comprises a first stage gas-solid separator and a second stage gas-solid separator,

the total separation efficiency of the first-stage gas-solid separator ranges from 65 to 75 percent, dp50 is 100-200 microns, the gas inlet of the first-stage gas-solid separator is communicated with the gas outlet of the fluidized bed gasification furnace, and the gas outlet of the first-stage gas-solid separator is communicated with the gas inlet of the second-stage gas-solid separator; a feed opening of the first-stage gas-solid separator is communicated with a semicoke inlet of the fluidized bed gasification furnace through a first pipeline, and the semicoke inlet is arranged on the side wall of the fluidized bed gasification furnace;

the total separation efficiency of the second stage gas-solid separator is more than 99 percent, and dp50 is 10-20 microns; and the feed opening of the second-stage gas-solid separator is communicated with a fine powder inlet of the semicoke oxidation area through a second pipeline, the fine powder inlet is connected with the gas distribution plate, and the axis of the fine powder inlet is intersected with the axis of the gas distribution plate.

4. The syngas generation apparatus of claim 3, wherein the solid particulates within the first conduit comprise semicoke; the solid particles in the second conduit comprise fly ash.

5. The syngas generation apparatus of claim 3, wherein the first conduit is provided with a return feeder for transporting solid particulates within the first conduit to the semi-coking oxidation zone.

6. The syngas generation apparatus of claim 3, wherein the second conduit is provided with a fly ash inlet and a blowing gas inlet;

the fly ash inlet is used for introducing fly ash;

and the blowing gas inlet is used for introducing airflow so as to drive the fly ash in the second pipeline to enter the semicoke oxidation area.

7. The syngas generation apparatus of claim 2, wherein the side wall of the fluidized-bed gasifier is further provided with an auxiliary solid fuel inlet for feeding solid fuel, including coke and/or semi coke, into the semi-coke oxidation zone.

8. The syngas generation apparatus of claim 2, wherein the fluidized-bed gasification furnace further has a high-temperature pyrolysis gasification zone, the high-temperature pyrolysis gasification zone being located at an upper portion of the fluidized-bed gasification furnace, and a temperature of the high-temperature pyrolysis gasification zone ranges from 950 ℃ to 1000 ℃.

9. The syngas generation apparatus of claim 8, wherein the sidewall of the pyrolysis gasification zone is provided with a waste feed inlet and a second inlet pipe for introducing oxygen and/or steam.

10. The syngas generation apparatus of claim 8, wherein the fluidized-bed gasifier further has a char gasification zone located between the char oxidation zone and the high-temperature pyrolysis gasification zone, the char gasification zone having a temperature in the range of 950 ℃ to 1000 ℃.

11. The syngas generation apparatus of claim 2, wherein the fluidized-bed gasification furnace further has a plenum located between the gas distribution plate and a bottom plate of the fluidized-bed gasification furnace.

12. The syngas generation apparatus of claim 11 wherein the side wall of the chamber is provided with a third gas inlet pipe for introducing steam and an auxiliary fuel gas.

13. A method for producing synthesis gas by high-temperature gasification of domestic garbage, which uses the synthesis gas generation device according to claim 1; the method for producing the synthesis gas by the high-temperature gasification of the household garbage is characterized by comprising the following steps:

s10: heating the temperature of the semicoke oxidation zone to above 1300 ℃;

s20: introducing solid particles separated by the gas-solid separator into a semicoke oxidation zone;

s30: the solid particles are sintered and solidified, and discharged out of the fluidized-bed gasification furnace.

14. The method of claim 13, wherein the gas-solid separator comprises a first stage gas-solid separator and a second stage gas-solid separator, the first stage gas-solid separator has a total separation efficiency in the range of 65-75%, and dp50 is 100-200 μm; the total separation efficiency of the second stage gas-solid separator is more than 99 percent, and dp50 is 10-20 microns;

and the S20 further comprises the steps of introducing the synthesis gas into the first-stage gas-solid separator, and introducing the synthesis gas purified by the first-stage gas-solid separator into the second-stage gas-solid separator.

15. The method for producing synthesis gas by high-temperature gasification of household garbage according to claim 14, wherein the fluidized-bed gasification furnace further comprises a high-temperature pyrolysis gasification zone, and the method for producing synthesis gas by high-temperature gasification of household garbage further comprises the following steps:

heating the top of the fluidized bed gasification furnace to 950-1000 ℃;

and pyrolyzing and gasifying tar in the synthesis gas in the fluidized bed gasification furnace.

Technical Field

The invention relates to the field of garbage treatment, in particular to a synthesis gas generation device and a method for producing synthesis gas by high-temperature gasification of household garbage.

Background

The household garbage mainly refers to solid waste generated in daily life or activities for providing services for daily life, and solid waste regarded as household garbage according to laws and administrative laws and regulations. The garbage collection and treatment system mainly comprises resident household garbage, municipal trade and commercial garbage, public place garbage, street cleaning garbage, enterprise and public institution garbage and the like.

For some domestic waste, for example: kitchen, paper, plastic, textile plastic, rubber and other organic solid wastes and the like can be treated by adopting a waste pyrolysis technology.

The garbage pyrolysis technology generally comprises the steps of conveying garbage to a fluidized bed, heating the temperature in the fluidized bed to 450 ℃ and 750 ℃, and decomposing organic matters in the garbage into two parts of solid and hot gas under the condition. For the solid fraction, there will generally be fly ash with smaller particle size. For the hot gas portion, tar is usually contained.

In summary, the present method for treating domestic garbage by pyrolysis has no good treatment method for the fly ash or tar produced by the pyrolysis.

Disclosure of Invention

The invention aims to overcome the defects of fly ash generated in the process of pyrolysis treatment of garbage in the prior art and provides a synthesis gas generation device and a method for producing synthesis gas by high-temperature gasification of household garbage.

The invention solves the technical problems through the following technical scheme:

a synthetic gas generating device is used for high-temperature gasification of household garbage and generation of synthetic gas and is characterized by comprising a fluidized bed gasification furnace and a gas-solid separator; the fluidized bed gasification furnace is used for high-temperature gasification of the household garbage and generating synthesis gas, the top of the fluidized bed gasification furnace is provided with a gas outlet, the lower part of the fluidized bed gasification furnace is provided with a semicoke oxidation area, and the temperature of the semicoke oxidation area is higher than 1300 ℃; the gas-solid separator is used for separating solid particles in the synthesis gas; the gas-solid separator is provided with a gas inlet and a feed opening, the gas inlet of the gas-solid separator is communicated with the gas outlet of the fluidized bed gasification furnace, and the feed opening of the gas-solid separator is communicated with the semicoke oxidation zone.

In the embodiment, by adopting the structure, the solid particles including the fly ash in the synthesis gas are separated by the gas-solid separator, the solid particles are conveyed to the semicoke oxidation area, and the solid particles are melted and softened and bonded with the slag by using the high temperature higher than 1300 ℃ in the semicoke oxidation area, so that the solid particles are solidified, the fly ash is solidified, and the fly ash is prevented from entering the synthesis gas; at the same time, the purification of the synthesis gas is also realized.

Preferably, the synthesis gas generation device further comprises a gas distribution plate, a slag discharge pipe and a first gas inlet pipe; the gas distribution plate is arranged at the bottom of the semicoke oxidation zone, the gas distribution plate is in an inverted cone shape, and the large end of the gas distribution plate is connected with the side wall of the fluidized bed gasification furnace; one end of the slag discharging pipe is connected with the small end of the gas distribution plate, and the other end of the slag discharging pipe extends downwards to the outer side of the bottom plate of the synthetic gas generating device; the first air inlet pipe is arranged inside the slag discharging pipe, the axis of the first air inlet pipe coincides with the axis of the slag discharging pipe, the first air inlet pipe is used for introducing an oxidant and fuel gas, a nozzle is arranged at the end part of the first air inlet pipe, and the oxidant and the fuel gas are sprayed into the semicoke oxidation area through the nozzle to be combusted, so that the temperature of the semicoke oxidation area is higher than 1300 ℃.

In this embodiment, through adopting above structure, through setting up first intake pipe, be favorable to stable, violent burning in the semicoke oxidation zone of fuel gas to the temperature that is favorable to the semicoke oxidation zone is higher than 1300 ℃.

Preferably, the gas-solid separator comprises a first stage gas-solid separator and a second stage gas-solid separator, the total separation efficiency of the first stage gas-solid separator is in the range of 65-75%, dp50 is 100-; a feed opening of the first-stage gas-solid separator is communicated with a semicoke inlet of the fluidized bed gasification furnace through a first pipeline, and the semicoke inlet is arranged on the side wall of the fluidized bed gasification furnace; the total separation efficiency of the second stage gas-solid separator is more than 99 percent, and dp50 is 10-20 microns; and the feed opening of the second-stage gas-solid separator is communicated with a fine powder inlet of the semicoke oxidation area through a second pipeline, the fine powder inlet is connected with the gas distribution plate, and the axis of the fine powder inlet is intersected with the axis of the gas distribution plate.

In this embodiment, by adopting the above structure, the separation of solid particles with a larger particle size is realized by the first stage gas-solid separator, and the separation of solid particles with a smaller particle size is realized by the second stage gas-solid separator, which is beneficial to improving the efficiency of separating solid particles in synthesis gas and reducing the production cost. In addition, the feed opening of the second-stage gas-solid separator is communicated with the fine powder inlet of the semicoke oxidation area through the second pipeline, and the axis of the fine powder inlet is intersected with the axis of the gas distribution plate, so that solid particles with smaller particle sizes can be effectively melted and softened and bonded with slag, and particularly, the effect on solid particles such as fly ash and the like is more obvious.

Preferably, the solid particles in the first conduit comprise semicoke; the solid particles in the second conduit comprise fly ash.

Preferably, a material returning device is arranged on the first pipeline and used for conveying the solid particles in the first pipeline to the semicoke oxidation area.

In this embodiment, through adopting above structure, utilize the returning charge ware, be favorable to the solid particle in the first pipeline to get into in the semicoke oxidation zone fast.

Preferably, the second pipeline is provided with a fly ash inlet and a blowing gas inlet; the fly ash inlet is used for introducing fly ash; and the blowing gas inlet is used for introducing airflow so as to drive the fly ash in the second pipeline to enter the semicoke oxidation area.

In this embodiment, by adopting the above structure, the present synthesis gas generation apparatus can process external fly ash by using the fly ash inlet, such as: the fly ash inlet is connected with the dust remover, so that the fly ash in the dust remover can be treated, and the application range of the device is widened. The blowing gas inlet is utilized, so that the flying ash can rapidly and efficiently enter a semicoke oxidation area, and the pipeline blockage is avoided.

Preferably, the side wall of the semi-coking oxidation zone is also provided with an auxiliary solid fuel inlet, the auxiliary solid fuel inlet is used for conveying solid fuel into the semi-coking oxidation zone, and the solid fuel comprises coke and/or semi coke.

In this embodiment, by adopting the above structure, the solid fuel is added by using the auxiliary solid fuel inlet, and especially when the calorific value of the garbage is low and cannot meet the reaction temperature of the fluidized bed gasification furnace, the solid fuel needs to be added by using the auxiliary solid fuel inlet.

Preferably, the fluidized bed gasification furnace further comprises a high temperature pyrolysis gasification region, the high temperature pyrolysis gasification region is located at the upper part of the fluidized bed gasification furnace, and the temperature of the high temperature pyrolysis gasification region ranges from 950 ℃ to 1000 ℃.

In the embodiment, by adopting the structure, the high-temperature pyrolysis gasification area is utilized, and the temperature range of the high-temperature pyrolysis gasification area is set to 950-1000 ℃, so that the pyrolysis of tar is facilitated, and the damage of the tar to the gas-solid separator is avoided.

Preferably, the side wall of the high-temperature pyrolysis gasification area is provided with a garbage feeding port and a second air inlet pipe, and the second air inlet pipe is used for introducing oxygen and/or steam.

In this embodiment, through adopting above structure, utilize the rubbish feed inlet, be favorable to controlling the entering speed of rubbish. By utilizing the second air inlet pipe, the amount of oxygen can be increased or reduced according to the actual needs of the high-temperature pyrolysis gasification area, and the control of the reaction of the high-temperature pyrolysis gasification area is facilitated.

Preferably, the garbage feeding hole is arranged below the second air inlet pipe; the quantity of rubbish feed inlet is a plurality of, the quantity of second intake pipe is a plurality of.

Preferably, the fluidized bed gasification furnace is further provided with a semicoke gasification zone, the semicoke gasification zone is positioned between the semicoke oxidation zone and the high-temperature pyrolysis gasification zone, and the temperature of the semicoke gasification zone ranges from 950 ℃ to 1000 ℃.

In this embodiment, through adopting above structure, be favorable to improving the pyrolysis gasification efficiency of tar.

Preferably, the fluidized bed gasification furnace further comprises a gas chamber, and the gas chamber is located between the gas distribution plate and a bottom plate of the fluidized bed gasification furnace.

Preferably, a third air inlet pipe is arranged on the side wall of the air chamber and is used for introducing steam and auxiliary fuel gas.

A method for producing synthesis gas by high-temperature gasification of household garbage uses the synthesis gas generation device; the method for producing the synthesis gas by the high-temperature gasification of the household garbage is characterized by comprising the following steps:

s10: heating the temperature of the semicoke oxidation zone to above 1300 ℃;

s20: introducing solid particles separated by the gas-solid separator into a semicoke oxidation zone;

s30: the solid particles are sintered and solidified, and discharged out of the fluidized-bed gasification furnace.

In the embodiment, by adopting the method, the solid particles including the fly ash in the synthesis gas are separated by the gas-solid separator by utilizing the high temperature higher than 1300 ℃ in the semicoke oxidation area, and the solid particles are conveyed to the semicoke oxidation area, so that the solid particles are melted and softened and bonded with the slag, the solidification of the fly ash is realized, and the fly ash is prevented from entering the synthesis gas; at the same time, the purification of the synthesis gas is also realized.

Preferably, the gas-solid separator comprises a first stage gas-solid separator and a second stage gas-solid separator, the total separation efficiency of the first stage gas-solid separator is in the range of 65-75%, and dp50 is 100-200 microns; the total separation efficiency of the second stage gas-solid separator is more than 99 percent, and dp50 is 10-20 microns; and the S20 further comprises the steps of introducing the synthesis gas into the first-stage gas-solid separator, and introducing the synthesis gas purified by the first-stage gas-solid separator into the second-stage gas-solid separator.

In this embodiment, by adopting the above method, the separation of the solid particles with a larger particle size is realized by the first stage gas-solid separator, and the separation of the solid particles with a smaller particle size is realized by the second stage gas-solid separator, which is beneficial to improving the efficiency of separating the solid particles in the synthesis gas and reducing the production cost.

Preferably, the fluidized bed gasification furnace is further provided with a high-temperature pyrolysis gasification area, and the method for producing the synthesis gas by high-temperature gasification of the household garbage further comprises the following steps:

heating the top of the fluidized bed gasification furnace to 950-1000 ℃;

and pyrolyzing and gasifying tar in the synthesis gas in the fluidized bed gasification furnace.

In the embodiment, by adopting the method, the temperature of the high-temperature pyrolysis gasification zone is set to be 950-1000 ℃, so that the pyrolysis of tar is realized, and the damage of tar to the gas-solid separator is avoided.

On the basis of the common knowledge in the field, the above preferred conditions can be combined randomly to obtain the preferred embodiments of the invention.

The positive progress effects of the invention are as follows:

the synthesis gas generation device of the invention separates solid particles including fly ash in synthesis gas by using the gas-solid separator, conveys the solid particles to the semicoke oxidation area, melts and softens the solid particles and bonds with slag by using the high temperature higher than 1300 ℃ in the semicoke oxidation area, thereby realizing the solidification of the solid particles, also realizing the solidification of the fly ash and avoiding the fly ash from entering the synthesis gas; at the same time, the purification of the synthesis gas is also realized. The synthesis gas generation device has simple structure and high efficiency, and realizes zero emission of fly ash.

Drawings

Fig. 1 is a schematic configuration diagram of a synthesis gas generation apparatus according to embodiment 1 of the present invention.

FIG. 2 is a schematic structural view of a nozzle of a synthesis gas generation apparatus according to example 1 of the present invention.

FIG. 3 is a schematic diagram of the configuration of the first stage gas-solid separator of the synthesis gas generation apparatus of example 1 of the present invention.

FIG. 4 is another schematic configuration of the first stage gas-solid separator of the synthesis gas generation plant of example 1 of the present invention.

FIG. 5 is a schematic diagram of the second stage gas-solid separator of the synthesis gas generation plant of example 1 of the present invention.

FIG. 6 is another schematic diagram of the second stage gas-solid separator of the synthesis gas generation plant of example 1 of the present invention.

Fig. 7 is a schematic flow chart of a method for producing synthesis gas by high-temperature gasification of household garbage according to embodiment 2 of the present invention.

Description of reference numerals:

synthesis gas generation apparatus 100

Fluidized bed gasification furnace 1

First stage gas-solid separator 2

Second stage gas-solid separator 3

Third intake pipe 4

Auxiliary solid fuel inlet 5

Garbage inlet 6

A second air inlet pipe 7

Semicoke inlet 8

Gas distribution plate 9

Air cell 10

First intake pipe 11

Nozzle 12

Fine powder inlet 13

First pipe 14

Second pipe 15

Air outlet 16

Slag discharge pipe 21

Auxiliary fuel gas conduit 22

Oxygen steam line 23

Blowing air inlet 24

Fly ash inlet 25

Return feeder 26

Blasting pipe 27

Semi-coke oxidation zone 101

Semi-coke gasification zone 102

High temperature pyrolysis gasification zone 103

Supplementary fuel gas inlet 1201

Oxidant inlet 1202

First stage gas-solid separator gas inlet 201

First stage gas-solid separator cylinder 202

Gas outlet 203 of first stage gas-solid separator

First stage gas-solid separator feed opening 204

Second stage gas-solid separator gas inlet 301

Second stage gas-solid separator barrel 302

Gas outlet 303 of second-stage gas-solid separator

Second stage gas-solid separator feed opening 304

Detailed Description

The present invention will be more clearly and completely described below by way of examples and with reference to the accompanying drawings, but the present invention is not limited thereto.

Example 1

As shown in fig. 1 to 6, the present embodiment is a synthesis gas generation apparatus 100 for high temperature gasification of domestic garbage and generating synthesis gas, the synthesis gas generation apparatus 100 includes a fluidized bed gasification furnace 1 and a gas-solid separator; the fluidized bed gasification furnace 1 is used for high-temperature gasification of household garbage and generating synthesis gas, the top of the fluidized bed gasification furnace 1 is provided with a gas outlet 16, the lower part of the fluidized bed gasification furnace 1 is provided with a semicoke oxidation area 101, and the temperature of the semicoke oxidation area 101 is higher than 1300 ℃; the gas-solid separator is used for separating solid particles in the synthesis gas; the gas-solid separator is provided with a gas inlet and a feed opening, the gas inlet of the gas-solid separator is communicated with the gas outlet 16 of the fluidized bed gasification furnace 1, and the feed opening of the gas-solid separator is communicated with the semicoke oxidation zone 101. In the embodiment, by adopting the structure, the solid particles including the fly ash in the synthesis gas are separated by the gas-solid separator, the solid particles are conveyed to the semicoke oxidation area 101, and the solid particles are melted and softened and bonded with the slag by using the high temperature higher than 1300 ℃ in the semicoke oxidation area 101, so that the solid particles are solidified, the fly ash is solidified, and the fly ash is prevented from entering the synthesis gas; at the same time, the purification of the synthesis gas is also realized.

As an embodiment, the synthesis gas generation device 100 may further include a gas distribution plate 9, a slag discharge pipe 21, and a first gas inlet pipe 11; the gas distribution plate 9 is arranged at the bottom of the semicoke oxidation zone 101, the gas distribution plate 9 is in an inverted cone shape, and the large end of the gas distribution plate 9 is connected with the side wall of the fluidized bed gasification furnace 1; one end of the slag discharge pipe 21 is connected with the small end of the gas distribution plate 9, and the other end of the slag discharge pipe 21 extends downwards to the outer side of the bottom plate of the synthetic gas generating device 100; the first air inlet pipe 11 is arranged inside the deslagging pipe 21, the axis of the first air inlet pipe 11 is overlapped with the axis of the deslagging pipe 21, the first air inlet pipe 11 is used for introducing an oxidant and fuel gas, a nozzle 12 is arranged at the end part of the first air inlet pipe 11, and the oxidant and the fuel gas are sprayed into the semicoke oxidation zone 101 through the nozzle 12 to be combusted, so that the temperature of the semicoke oxidation zone 101 is higher than 1300 ℃. The first air inlet pipe 11 is arranged in the semi-coking oxidation zone 101, so that stable and violent combustion of the fuel gas in the semi-coking oxidation zone 101 is facilitated, and the temperature of the semi-coking oxidation zone 101 is higher than 1300 ℃.

As shown in fig. 1 and 2, a schematic view of the first intake pipe 11 and the nozzle 12 is shown. The auxiliary fuel gas pipeline 22 is filled with auxiliary fuel gas, and the oxygen steam pipeline 23 is filled with oxygen steam. The supplementary fuel gas inlet 1201 is located in the centre of the nozzle 12 and the oxidant inlet 1202 is located outside the nozzle 12.

As a specific implementation mode, as shown in FIG. 1, the gas-solid separator may further include a first stage gas-solid separator 2 and a second stage gas-solid separator 3, the first stage gas-solid separator 2 is used for separating solid particles with larger particle size in the synthesis gas, the total separation efficiency of the first stage gas-solid separator 2 is in the range of 65-75%, dp50 is 100-200 microns, and dp50 is also called median particle size. The gas inlet of the first-stage gas-solid separator 2 is communicated with the gas outlet 16 of the fluidized bed gasification furnace 1, and the gas outlet 16 of the first-stage gas-solid separator 2 is communicated with the gas inlet of the second-stage gas-solid separator 3; a feed opening of the first-stage gas-solid separator 2 is communicated with a semicoke inlet of the fluidized bed gasification furnace 1 through a first pipeline 14, and the semicoke inlet is arranged on the side wall of the fluidized bed gasification furnace 1; the second stage gas-solid separator 3 is used for separating solid particles with smaller particle sizes in the synthesis gas, the total separation efficiency of the second stage gas-solid separator 3 is more than 99 percent, and dp50 is 10-20 microns; the feed opening of the second-stage gas-solid separator 3 is communicated with a fine powder inlet 13 of the semicoke oxidation zone 101 through a second pipeline 15, the fine powder inlet 13 is connected with a gas distribution plate 9, and the axis of the fine powder inlet 13 is intersected with the axis of the gas distribution plate 9. In the embodiment, the first-stage gas-solid separator 2 is used for separating solid particles with larger particle sizes, and the second-stage gas-solid separator 3 is used for separating solid particles with smaller particle sizes, so that the efficiency of separating the solid particles in the synthesis gas is improved, and the production cost is reduced. In addition, the feed opening of the second stage gas-solid separator 3 is communicated with the fine powder inlet 13 of the semicoke oxidation zone 101 through the second pipeline 15, and the axis of the fine powder inlet 13 is intersected with the axis of the gas distribution plate 9, so that solid particles with smaller particle size can be effectively melted and softened and bonded with slag, and particularly, the effect is more obvious on solid particles such as fly ash and the like.

As a specific embodiment, the first stage gas-solid separator 2 may be as shown in fig. 3 and 4, and the first stage gas-solid separator 2 may be an inertial separator. The inertia separator realizes gas-solid separation based on different gas-solid inertia. The synthesis gas containing solid particles firstly enters the air inlet 201 of the first stage gas-solid separator in the horizontal direction and then turns 90 degrees to enter the cylinder 202 of the first stage gas-solid separator downwards. The solid particles in the gas-solid separator downwards enter a feed opening 204 of the first stage gas-solid separator, and the rest purified synthesis gas ascends to enter a gas outlet 203 of the first stage gas-solid separator.

The second stage gas-solid separator 3 may be as shown in fig. 5 and 6, and the second stage gas-solid separator 3 may be selected to be a cyclone. The cyclone separator makes solid particles or liquid drops with larger inertial centrifugal force thrown to the outer wall surface by the rotary motion caused by tangential introduction of airflow, thereby realizing gas-solid separation. The cyclone separator of the embodiment has the advantages of simple structure, high operation elasticity, high efficiency, convenience in management and maintenance and low price. Is suitable for collecting dust with the diameter of more than 5-10 mu m. In this embodiment, the syngas containing solid particles enters the second stage gas-solid separator cylinder 302 from the second stage gas-solid separator inlet 301 along the tangential direction, the solid particles enter the second stage gas-solid separator discharge opening 304 along the inner wall of the second stage gas-solid separator cylinder 302 under the action of centrifugal force, and the purified syngas rises to enter the second stage gas-solid separator outlet 303.

As a preferred embodiment, the solid particles in the first conduit 14 may also include semicoke; the solid particles in the second conduit 15 may comprise fly ash.

In this embodiment, as shown in FIG. 1, a material returning device 26 is further disposed on the first pipe 14, and the material returning device 26 is used for conveying the solid particles in the first pipe 14 to the semi-coking oxidation zone 101. This embodiment utilizes a return feeder 26 to facilitate the rapid entry of solid particles in the first conduit 14 into the semi-coke oxidation zone 101. In other embodiments, the solid particles in the first conduit 14 can also be conveyed into the semicoke gasification zone 102, and the solid particles introduced into the semicoke gasification zone 102 can also achieve the effect of stabilizing the bed.

The second pipeline 15 is also provided with a fly ash inlet 25 and a blowing gas inlet 24; the fly ash inlet 25 is used for introducing fly ash; the blowing gas inlet 24 is used for introducing air flow to drive the fly ash in the second pipeline 15 to enter the semicoke oxidation area 101. The second conduit 15 communicates with the semi-coke oxidation zone 101 via a blow line 27. The present embodiment utilizes the fly ash inlet 25, so that the present synthesis gas generation apparatus 100 can process the external fly ash, such as: the fly ash inlet 25 is connected with the dust remover, so that the fly ash in the dust remover can be treated, and the application range of the device is widened in the embodiment. The blowing gas inlet 24 is beneficial to the flying ash to rapidly and efficiently enter the semicoke oxidation area 101, and the pipeline is prevented from being blocked.

And the side wall of the semi-coking oxidation zone 101 is also provided with an auxiliary solid fuel inlet 5, and the auxiliary solid fuel inlet 5 is used for conveying solid fuel into the semi-coking oxidation zone 101, wherein the solid fuel comprises coke and/or semi-coke. In the embodiment, the auxiliary solid fuel inlet 5 is used to realize the addition of the solid fuel, and particularly when the calorific value of the garbage is low and cannot meet the reaction temperature of the fluidized bed gasification furnace 1, the auxiliary solid fuel inlet 5 is used to add the solid fuel more.

In a preferred embodiment, the fluidized-bed gasification furnace 1 further has a high-temperature pyrolysis gasification region 103, the high-temperature pyrolysis gasification region 103 is located at an upper portion of the fluidized-bed gasification furnace 1, and a temperature of the high-temperature pyrolysis gasification region 103 ranges from 950 ℃ to 1000 ℃. In the embodiment, the high-temperature pyrolysis gasification area 103 is utilized, and the temperature of the high-temperature pyrolysis gasification area 103 is set to be 950-1000 ℃, so that the pyrolysis of tar is facilitated, and the damage of tar to the gas-solid separator is avoided.

In this embodiment, as shown in fig. 1, a garbage feeding port 6 and a second air inlet pipe 7 are disposed on a side wall of the high-temperature pyrolysis gasification region 103, and the second air inlet pipe 7 is used for introducing oxygen and/or steam. This embodiment utilizes rubbish feed inlet 6, is favorable to controlling the entering speed of rubbish. By using the second air inlet pipe 7, the amount of oxygen can be increased or decreased according to the actual needs of the pyrolysis gasification zone 103, which is beneficial to controlling the reaction of the pyrolysis gasification zone 103.

Specifically, the garbage feeding hole 6 is arranged below the second air inlet pipe 7; the quantity of rubbish feed inlet 6 is a plurality of, and the quantity of second intake pipe 7 is a plurality of.

In a preferred embodiment, the fluidized-bed gasification furnace 1 further comprises a char gasification zone 102, the char gasification zone 102 is located between the char oxidation zone 101 and the high-temperature pyrolysis gasification zone 103, and the temperature of the char gasification zone 102 is in the range of 950 ℃ to 1000 ℃. This embodiment is favorable to improving the pyrolysis gasification efficiency of tar.

In the present embodiment, as shown in fig. 1, the fluidized-bed gasification furnace 1 further includes a gas chamber 10, and the gas chamber 10 is located between the gas distribution plate 9 and the bottom plate of the fluidized-bed gasification furnace 1. Specifically, a third air inlet pipe 4 is disposed on a side wall of the air chamber 10, and the third air inlet pipe 4 is used for introducing steam and auxiliary fuel gas.

As an embodiment, the reaction of the fluidized-bed gasification furnace 1The zone comprises a semicoke oxidation zone 101, a semicoke gasification zone 102 and a garbage high-temperature pyrolysis gasification zone 103 from bottom to top. The synthesis gas generated by the fluidized bed gasification furnace 1 mainly comprises H₂、CO、CH₄、CO₂And H₂And O. The household garbage is screened and crushed, enters the garbage high-temperature pyrolysis gasification area 103 through the garbage feeding hole 6 of the fluidized bed gasification furnace 1 and is subjected to severe chemical reaction with high-temperature gas generated at the lower part of the fluidized bed gasification furnace 1, the temperature of the gas outlet 16 at the top of the fluidized bed gasification furnace 1 is controlled by the oxygen inlet amount of the second gas inlet pipe 7, and the temperature of the synthetic gas at the outlet of the fluidized bed gasification furnace 1 is maintained between 950 ℃ and 1000 ℃. The unreacted large solid particles in the high-temperature pyrolysis gasification area 103 of the garbage enter the lower dense-phase section of the fluidized bed gasification furnace 1 to continue reacting under the action of gravity, and the finer solid particles enter the first-stage gas-solid separator 2 along with the high-temperature synthesis gas at the top gas outlet 16 of the fluidized bed gasification furnace 1. The solid particles trapped by the first stage gas-solid separator 2 enter the semicoke gasification zone 102 of the fluidized-bed gasification furnace 1 through the first pipe 14, the return feeder 26 and the semicoke inlet 8. The finer solid particles collected by the second stage gas-solid separator 3 and the fly ash collected by the dust collector downstream of the synthesis gas generation apparatus 100 enter the semicoke oxidation zone 101 of the fluidized-bed gasification furnace 1 through the second pipe 15, the blowing pipe 27 and the fine powder inlet 13, and are mixed with the oxygen gas and the fuel gas from the nozzle 12, so that a vigorous oxidation reaction occurs. The reaction temperature of the semi-coke oxidation zone 101 is above 1300 ℃. The fine powder and fly ash particles after the reaction are melted and softened and bonded with the slag, and are discharged out of the gasifier through a slag discharge pipe 21 together with the slag. When the calorific value of the garbage is low and cannot meet the reaction temperature of the fluidized bed gasification furnace 1, auxiliary solid fuel is needed. The auxiliary solid fuel enters the semi-coke gasification zone 102 of the lower dense-phase section of the fluidized bed gasification furnace 1 through the feed inlet, is fully mixed with the materials of the dense-phase section and generates violent chemical reaction, the reaction temperature of the semi-coke gasification zone 102 is controlled between 950 ℃ and 1000 ℃, and slag is generated after the reaction. The slag is discharged out of the fluidized-bed gasification furnace 1 through the slag discharge pipe 21. After entering the gas chamber 10, the steam and the auxiliary fuel gas enter the reaction area of the fluidized bed gasification furnace 1 through the distribution plate.

In other embodiments, the syngas generating apparatus 100 may further be provided with a plurality of temperature detection ports for detecting the temperature of the locations of the semicoke oxidation zone 101, the semicoke gasification zone 102, the high-temperature pyrolysis gasification zone 103, the gas chamber 10, the gas-solid separator, and the like, and a pressure difference detection port for detecting the height of the dense phase section of the fluidized-bed gasification furnace 1. In addition, pressure detection ports can be arranged at the bottom of the fluidized bed gasification furnace 1, the gas outlet 16 of the fluidized bed gasification furnace 1, the outlet of the gas-solid separator and other material pipelines. Through the detection means, when the characteristics of the treated household garbage fluctuate, the auxiliary fuel quantity, the oxygen and the steam charging quantity can be adjusted in time, and the stable operation of the fluidized bed gasification furnace is ensured.

Example 2

As shown in fig. 7, the present embodiment is a method for producing synthesis gas by high-temperature gasification of domestic garbage, the method for producing synthesis gas by high-temperature gasification of domestic garbage uses a synthesis gas production apparatus 100 as in embodiment 1, the synthesis gas production apparatus 100 refers to fig. 1-6, and the method for producing synthesis gas by high-temperature gasification of domestic garbage includes the following steps:

s10: heating the temperature of the semicoke oxidation zone 101 to above 1300 ℃;

s20: solid particles separated by the gas-solid separator are led into a semicoke oxidation zone 101;

s30: the solid particles are sintered and solidified, and discharged out of the fluidized-bed gasification furnace 1.

In the embodiment, the high temperature higher than 1300 ℃ in the semicoke oxidation area 101 is utilized, the solid particles comprising the fly ash in the synthesis gas are separated by utilizing the gas-solid separator, and the solid particles are conveyed to the semicoke oxidation area 101, so that the solid particles are melted and softened and bonded with the slag, the solidification of the fly ash is realized, and the fly ash is prevented from entering the synthesis gas; at the same time, the purification of the synthesis gas is also realized.

In a preferred embodiment, the gas-solid separator comprises a first stage gas-solid separator 2 and a second stage gas-solid separator 3, the total separation efficiency of the first stage gas-solid separator 2 is in the range of 65-75%, and the dp50 is 100 and 200 microns; the total separation efficiency of the second-stage gas-solid separator 3 is more than 99 percent, and the dp50 is 10-20 microns; step S20 further includes introducing the synthesis gas into the first stage gas-solid separator 2, and then introducing the synthesis gas purified by the first stage gas-solid separator 2 into the second stage gas-solid separator 3. In the embodiment, the first-stage gas-solid separator 2 is used for separating solid particles with larger particle sizes, and the second-stage gas-solid separator 3 is used for separating solid particles with smaller particle sizes, so that the efficiency of separating the solid particles in the synthesis gas is improved, and the production cost is reduced.

In other embodiments, the fluidized bed gasification furnace 1 may further have a high temperature pyrolysis gasification zone 103, and the method for producing synthesis gas by high temperature gasification of domestic garbage further includes the following steps:

heating the top of the fluidized bed gasification furnace 1 to 950-1000 ℃;

tar in the synthesis gas is pyrolyzed and gasified in the fluidized-bed gasification furnace 1.

In the embodiment, the temperature of the high-temperature pyrolysis gasification zone 103 is set to be 950-1000 ℃, so that the pyrolysis of tar is realized, and the damage of tar to the gas-solid separator is avoided.

While specific embodiments of the invention have been described above, it will be appreciated by those skilled in the art that this is by way of example only, and that the scope of the invention is defined by the appended claims. Various changes and modifications to these embodiments may be made by those skilled in the art without departing from the spirit and scope of the invention, and these changes and modifications are within the scope of the invention.