CN106867588B

CN106867588B - Distributor, distribution injection assembly, gasification furnace and synthesis gas production method and system

Info

Publication number: CN106867588B
Application number: CN201510923979.4A
Authority: CN
Inventors: 彭宝仔; 刘臻; 巩志坚; 张颖; 张锋华; 陈薇; 冯子洋; 方薪晖
Original assignee: Shenhua Group Corp Ltd; National Institute of Clean and Low Carbon Energy
Current assignee: China Energy Investment Corp Ltd; National Institute of Clean and Low Carbon Energy
Priority date: 2015-12-14
Filing date: 2015-12-14
Publication date: 2021-05-28
Anticipated expiration: 2035-12-14
Also published as: CN106867588A

Abstract

The invention discloses a distributor, a distribution injection assembly, a gasification furnace and a synthesis gas production method and a synthesis gas production system, wherein the distributor (1) comprises an outer main pipe (12) and an inner main pipe (11), the inner main pipe and the outer main pipe respectively comprise an inner feeding pipe (111), a plurality of inner distributing pipes (112), an outer feeding pipe (121) and a plurality of outer distributing pipes (122), and the inner distributing pipes extend into the corresponding outer distributing pipes to form a distributing sleeve unit. The gasification raw material and the gasification agent can be independently conveyed and uniformly distributed in the inner and outer conveying channels in the distributor in a fluidized state. The fluidized state in the material cavity can be maintained through back blowing air inlet, the bottom does not generate deposition and blockage is prevented. The inverted ェ -shaped design of the gasification furnace can increase the reaction time of the gasification raw materials, shorten the retention time of the gas, effectively improve the carbon conversion rate and reduce the investment cost of the gasification furnace. In the gasification process, fly ash in the crude synthesis gas with the same quality can be adsorbed and filtered by the gasification residues after chilling and drying, so that the filtering cost is reduced.

Description

Distributor, distribution injection assembly, gasification furnace and synthesis gas production method and system

Technical Field

The invention relates to the field of gasification of carbon-containing fuels, in particular to a multi-nozzle gasification furnace device and a gasification process thereof.

Background

The gasification principle of the carbon-containing fuel is that the carbon-containing fuel such as coal and the like is crushed, dried, conveyed and sprayed into a high-temperature gasification furnace through a nozzle, and then a combustion reaction is generated to produce the synthesis gas. Furthermore, more water vapor can be introduced into the gasification furnace to generate water gas reaction, so that the output of the synthesis gas is increased.

Researchers in the field pursue improvement of a conveying device, a material distribution mechanism, a gasification furnace device and related components thereof, a process flow and the like, prevention of material conveying blockage, uneven material distribution, insufficient gasification reaction and the like, improvement of carbon conversion rate, reduction of equipment and process cost, and durability of the equipment. For example, in patent document CN1903998B, a gasifier injector is disclosed, which comprises a two-stage slurry flow separator and an injector face plate incorporating a cooling system. The first stage separator separates the main slurry flow into a plurality of secondary slurry flows, each secondary slurry flow separates a single secondary slurry flow into a plurality of tertiary slurry flows through the second stage separator, and the tertiary slurry flows are injected into the gasification chamber of the gasification furnace in the form of high-pressure slurry flows through the slurry flow injection pipes. The gasification agent is then impinged upon each high pressure slurry stream at high pressure in the form of an annular shaped spray through a plurality of annular impingement holes integrated into the injector face plate.

However, the gasifier injector using the cone as a separator to divide the primary slurry flow into a plurality of secondary slurry flows has several problems:

1) in the process of conveying materials from top to bottom, due to the gravity of the materials and the influence of the side wall effect of pipeline conveying, the materials are generally difficult to ideally pass through the center of a conveying pipeline and intensively pass through one side of the pipeline, so that the separator of the cone loses the material distribution function, the materials only flow through one or more of the secondary mud flows, and the material distribution is extremely uneven;

2) a plurality of dead corners exist among the plurality of secondary mud flow channels, and the channels are easily blocked when the material concentration is high;

3) the arrangement of a plurality of three-stage mud flow channels can enhance the mixing effect between gas and solid, but C and H are opposite to the combustion reaction of C and a gasifying agent in the coal gasification process₂O, C and CO₂The gasification degree of (2) finally determines the carbon conversion rate, and H is the later stage of the reaction₂O and CO₂The extent to which these two reactions proceed at equilibrium is determined primarily by the length of the reaction time. The cylindrical gasification chamber can not increase the gasification chamber H₂O and CO₂The concentration of (b) also does not prolong the reaction time, thus seriously affecting the high or low carbon conversion rate.

In addition, patent document CN101892086A also discloses a coal water slurry gasification furnace for coal water slurry gasification, which includes a combustion chamber and a quench chamber, wherein the combustion chamber is an ellipsoid-like wide-diameter combustion chamber housing, at least two coal water slurry and oxygen three-flow-channel process nozzle chambers are symmetrically arranged at the wide diameter of the combustion chamber housing and slightly inclined downwards, at least two coal water slurry and oxygen three-flow-channel nozzles are slightly inclined downwards and detachably mounted in each coal water slurry and oxygen three-flow-channel process nozzle chamber, and the nozzle openings face the inside of the combustion chamber, a refractory brick is lined in the combustion chamber housing, at least two oxygen nozzle chambers are located at the circumference below each coal water slurry and oxygen three-flow-channel process nozzle chamber and inclined upwards, at least two oxygen nozzles are inclined upwards and detachably mounted in each oxygen nozzle chamber, and the nozzle openings face the inside of the combustion chamber.

The ellipsoidal wide-diameter combustion chamber has the main problems of high requirements on the processing and installation of the combustion chamber, limited gasification strength, too long reaction residence time and low gasification yield, and the gasified fly ash is easy to corrode the top and the refractory bricks are easy to corrode and fall off.

Disclosure of Invention

Aiming at the defects or shortcomings in the prior art, the invention provides a distributor, a distribution injection assembly, a gasification furnace provided with the distribution injection assembly, and a synthesis gas production method and system, so as to effectively solve the problems of uneven material distribution, material blockage, low carbon conversion rate, low gasification strength, high fly ash filtration cost and the like of a plurality of nozzles.

In order to achieve the above object, according to a first aspect of the present invention, there is provided a distributor comprising an outer main pipe and an inner main pipe, wherein a material cavity of the outer main pipe and a material cavity of the inner main pipe are independent and isolated closed chambers, the inner main pipe comprises an inner feeding pipe and a plurality of inner distributing pipes respectively communicating with the material cavity of the inner main pipe, the outer main pipe comprises an outer feeding pipe and a plurality of outer distributing pipes both communicating with the material cavity of the outer main pipe, and each inner distributing pipe extends into the corresponding outer distributing pipe and extends outwards to form a distributing sleeve unit.

Preferably, a plurality of outer branch material pipes are the annular and equally spaced and arrange and stretch out from the diapire on the diapire of outer main pipe, and a plurality of interior branch material pipes also are the annular and equally spaced and arrange on the diapire of interior main pipe, and every interior branch material pipe is from the coaxial extension of the diapire of interior main pipe to in the outer branch material pipe that corresponds to form a plurality of branch material bushing units that the annular was arranged.

Preferably, the number of the inner distributing pipes is the same as that of the outer distributing pipes, and is not less than 3, and more preferably 3-24.

Preferably, the bottom end of the outer main tube and the bottom of the inner main tube are both cones or hemispheres having a lower apex.

Preferably, the distributor can also correspondingly comprise an inner blowback pipe and/or an outer blowback pipe, the outer blowback pipe is communicated with the material cavity of the outer main pipe at the low point at the bottom of the outer main pipe, and the inner blowback pipe communicated with the material cavity of the inner main pipe extends into the outer blowback pipe from the low point at the bottom of the inner main pipe and extends outwards.

Preferably, the distributor further comprises an inner main pipe gas distributor and/or an outer main pipe gas distributor, the inner main pipe gas distributor is arranged at the low point of the inner main pipe material cavity to disperse the back-blowing air inflow of the inner back-blowing pipe, and the outer main pipe gas distributor is arranged at the low point of the outer main pipe material cavity to disperse the back-blowing air inflow of the outer back-blowing pipe.

Preferably, the upper ports of the inner main pipe and the outer main pipe are closed, and the outer feeding pipe extends out from the circular pipe wall of the outer main pipe along the tangential direction so as to introduce feeding rotational flow into the material cavity of the outer main pipe; the inner feeding pipe extends into the outer feeding pipe from the circular pipe wall of the inner main pipe along the tangential direction and extends outwards so as to introduce feeding rotational flow into the inner main pipe cavity.

Preferably, in the inner branch pipe and the outer branch pipe which form the sleeve structure, the inner blowback pipe and the outer blowback pipe which form the sleeve structure, and the inner feed pipe and the outer feed pipe which form the sleeve structure, the extending end of the inner sleeve in the sleeve structure is flush with or extends out of the extending end of the outer sleeve.

According to the second aspect of the invention, the material distribution and injection assembly is further provided, and the material distribution and injection assembly comprises a nozzle arrangement panel, a plurality of nozzle units and the material distributor, wherein the nozzle units are of a sleeve structure and are butted with the corresponding material distribution sleeve units, and the plurality of nozzle units are arranged on the nozzle arrangement panel in a mutually spaced mode and penetrate through the nozzle arrangement panel.

Preferably, the nozzle arrangement panel is provided with a through threaded mounting hole, and the nozzle unit is screwed to the threaded mounting hole through a connecting thread provided on the outer tube wall.

Preferably, the plurality of nozzle units are arranged at equal intervals in a ring shape on the nozzle arrangement panel.

Preferably, the split material spray assembly further comprises a nozzle cooling system comprising a plurality of removable tees for inflow or outflow of a cooling medium and cooling pipe units disposed around each nozzle unit in the nozzle arrangement panel, the cooling pipe units of any two adjacent nozzle units being connected by removable tees therebetween.

Preferably, the nozzle arrangement panel is further provided with a plurality of water vapor inlets therethrough, and the plurality of water vapor inlets are arranged around the plurality of nozzle units.

According to a third aspect of the present invention, there is also provided a gasification furnace comprising a furnace body and the above-described divided material injection assembly, the nozzle arrangement panel of which is mounted on the top of the furnace body.

Preferably, the furnace body comprises a gasification section with a gasification chamber, a buffer section with a buffer cavity and a quenching section with a quenching chamber from top to bottom, the gasification chamber is communicated with the quenching chamber through the buffer cavity, and the nozzle arrangement panel is horizontally installed on the top cover of the gasification section, so that the gasification raw material and the gasifying agent can be sprayed towards the gasification chamber vertically and downwards through the nozzle unit.

Preferably, the bottom end of the gasification stage is formed as a throat structure which is connected obliquely downwards to the buffer stage.

Preferably, the gasification chamber and the buffer cavity are both cylindrical cavities, the height of the gasification chamber is not more than 1/3, preferably 1/6-1/3, the height of the buffer cavity is not more than 1/3, and the ratio of the inner diameter of the gasification chamber to the inner diameter of the buffer cavity is not less than 2, preferably 2-10.

Preferably, water-cooled walls are continuously arranged on the inner wall of the gasification chamber and the inner wall of the buffer cavity.

Preferably, a synthetic gas outlet is formed in the peripheral wall of the chilling chamber, the bottom of the chilling chamber is formed into a slag pool, and the ratio of the inner diameter of the chilling chamber to the inner diameter of the buffer cavity is 1.2-1.5.

Preferably, a chilling ring is arranged at the joint of the top of the chilling chamber and the buffer cavity, and the chilling ring is connected with a descending pipe extending into the slag pool.

Preferably, the reaction temperature of the gasification furnace is 1300 ℃ to 3000 ℃, preferably 1500 ℃ to 2800 ℃, more preferably 1900 ℃ to 2500 ℃.

According to a fourth aspect of the present invention, there is also provided a method of gasifying synthesis gas, the method comprising:

a gasification step: inputting a gasification raw material and a gasification agent into a gasification furnace, and carrying out gasification reaction on the gasification raw material in the gasification furnace under a gasification condition to generate crude synthesis gas and gasification residues; and

and (3) filtering the synthesis gas: drying the gasification residue to form a porous particulate material; contacting the raw syngas with a porous particulate material to filter fly ash in the raw syngas.

Preferably, the gasification step further comprises chilling the gasification residue and the raw syngas in the gasifier, and discharging the chilled gasification residue and the raw syngas out of the gasifier.

When the crude synthesis gas is contacted with the porous particle material to filter the fly ash, the temperature of the porous particle material is controlled to be 105-200 ℃, and the particle size is controlled to be 0.1-15 mm.

Preferably, after the gasification residue is dried, the water-containing volume of the porous granular material is controlled to be not more than 50% of the total volume of the porous granular material, and preferably 0-30%.

Preferably, in the synthesis gas filtration step, the dried porous particulate material is fed to a moving bed and the raw synthesis gas is filtered through the porous particulate material in the moving bed.

Preferably, the method further comprises:

a step of synthesizing, purifying and filtering: the filtered raw syngas is washed to further remove fly ash.

Preferably, the gasification reaction is carried out in the above-described gasification furnace according to the present invention.

According to a fifth aspect of the present invention, there is also provided a system for gasification of synthesis gas, the system comprising:

a gasification raw material crushing, drying and transporting system for producing and transporting dry coal powder or coal water slurry;

the gasification furnace is communicated with the gasification raw material crushing, drying and conveying system, and dry coal powder or coal water slurry is subjected to gasification reaction in the presence of a gasification agent in the gasification furnace to generate crude synthesis gas and gasification residues;

the slag discharging system is communicated with the gasification furnace and is used for discharging the gasification residues out of the gasification furnace;

a drying unit communicating with the slag discharge system, in which at least part of the gasification residue is dried to form a porous granular material; and

and a filtering and ash removing system communicated with the drying unit and the gasification furnace, wherein the crude synthesis gas is contacted with the porous granular material to filter fly ash in the crude synthesis gas.

Preferably, the filtration ash removal system comprises a moving bed in which the raw synthesis gas is contacted with porous particulate material to filter the fly ash.

Preferably, the gasifier is the gasifier according to the invention described above.

According to the technical scheme, the distributor provided by the invention is provided with the inner and outer independent conveying channels, the gasified raw material and the gasifying agent can pass through the inner and outer conveying channels in a fluidized state and are distributed through the plurality of distributing sleeve units. The material cavity can be always kept in a fluidized state through back-blowing air inlet of a back-blowing pipe connected with the bottom of the material cavity, deposition is not generated at the bottom of the material cavity, and therefore blockage is prevented, and material distribution is efficient and uniform. At the top of the gasification furnace, a plurality of top-arranged nozzles which are annularly arranged and a butted distributor which is uniformly distributed can ensure that the spraying materials of all the nozzles are uniform, and the flat cylindrical gasification chamber and the bottom necking design thereof can increase the reaction time, shorten the retention time, effectively improve the carbon conversion rate and reduce the investment cost of the gasification furnace. In the gasification process, the fly ash in the homogeneous crude synthesis gas is adsorbed and filtered by the gasification residues after being chilled and dried in the gasification furnace, so that the filtration cost can be reduced, and the total investment cost of gasification equipment can be reduced.

Additional features and advantages of the invention will be set forth in the detailed description which follows.

Drawings

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

FIG. 1 is a comparison graph of radial mean velocity distribution of cross sections of a furnace body with a single nozzle and a plurality of nozzles under the same test conditions;

fig. 2 is a schematic structural view of a gasification furnace according to a preferred embodiment of the present invention;

FIG. 3 is a schematic view of the construction of a dispenser according to a preferred embodiment of the present invention;

FIG. 4 is a cross-sectional view of the distributor of FIG. 3 illustrating tangential feed to create a swirling flow;

FIG. 5 is a top view of a nozzle arrangement panel according to a preferred embodiment of the present invention;

fig. 6 is a schematic view of a gasification process of a gasification furnace according to a preferred embodiment of the present invention.

Description of the reference numerals

1 distributor 2 nozzle device

3 furnace body 4 junction pipe

5 gasification raw material crushing, drying and conveying system 6 deslagging system

7 moving bed 8 venturi washing equipment

11 inner main pipe 12 outer main pipe

21 nozzle arrangement panel 22 nozzle unit

31 gasification chamber 32 buffer chamber

33 quench chamber 34 syngas outlet

111 inner main pipe 112 inner material pipe

113 internal blowback pipe 114 internal main pipe gas distributor

121 outer feeding pipe and 122 outer distributing pipe

123 outer blowback pipe 124 outer main pipe gas distributor

211 steam inlet 221 cooling medium inlet

222 cooling medium outlet 223 nozzle unit fixing panel

224 detachable three-way pipe 311 water-cooled wall

331 quench ring 332 downcomer

333 slag pool 334 slag discharge hole

Height of H1 gasification Chamber H total height of furnace body

Detailed Description

The following detailed description of embodiments of the invention refers to the accompanying drawings. It should be understood that the detailed description and specific examples, while indicating the present invention, are given by way of illustration and explanation only, not limitation.

In the present invention, unless otherwise specified, use of the terms of orientation such as "upper, lower, top, bottom" or the like are generally used in the description of the orientation shown in the drawings or the positional relationship of the components with respect to each other in the vertical, or gravitational direction; "vertical direction" means the up-down direction of the drawing sheet; "inner and outer" generally refers to the inner and outer of the chamber relative to the chamber or the radially inner and outer relative to the center of the circle.

In addition, the applicant filed chinese patent application No.201510740660.8 on 14/11/2015, which is incorporated herein by reference in its entirety.

Referring to fig. 3, the present invention firstly provides a novel distributor, the distributor 1 includes an outer main pipe 12 and an inner main pipe 11, an outer main pipe material cavity in the outer main pipe 12 and an inner main pipe material cavity in the inner main pipe 11 are independent and isolated closed chambers, the inner main pipe 11 includes an inner feeding pipe 111 and a plurality of inner branch pipes 112 respectively communicating with the inner main pipe material cavity, the outer main pipe 12 includes an outer feeding pipe 121 and a plurality of outer branch pipes 122 both communicating with the outer main pipe material cavity, wherein each inner branch pipe 112 extends into a corresponding outer branch pipe 122 and extends outward to form a distribution sleeve unit.

In the distributor, an inner main pipe 12 and an outer main pipe 11 form an inner conveying channel and an outer conveying channel, so that the gasified raw material, the gasifying agent and the like can be independently conveyed and are independently and uniformly distributed through a plurality of distributing sleeve units without mutual influence. The sleeve type distributor has novel and compact structure, and can match the sizes of the outer main pipe 12, the inner main pipe 11, the feeding pipe and the distributing pipe according to the shape, the weight and the like of conveyed materials, so that the conveyed materials are always in a fluidized state in a material cavity, and any material deposition or blockage and the like are not generated in a conveying channel as much as possible.

Specifically, the plurality of outer branched pipes 122 are preferably arranged on the bottom wall of the outer main pipe 12 at equal intervals in a ring shape and extend out from the bottom wall, the plurality of inner branched pipes 112 are also arranged on the bottom wall of the inner main pipe 11 at equal intervals in a ring shape, and each inner branched pipe 112 coaxially extends from the bottom wall of the inner main pipe 11 into the corresponding outer branched pipe 122. As shown in fig. 3, the number of the inner distributing pipes 112 and the number of the outer distributing pipes 122 are preferably the same, and particularly preferably 3 to 24 (determined according to the process requirement), so that a plurality of distributing sleeve units arranged annularly are formed, the structural symmetry is strong, and the distribution is uniform. When the assembly, can set up a plurality of branch material holes that the annular was arranged on the diapire, peg graft each branch material pipe and can realize the installation of branch material pipe on corresponding branch material hole.

Wherein, as shown in fig. 4, the outer feeding pipe 121 preferably extends tangentially from the circular pipe wall of the outer main pipe 12 to enable the feeding rotational flow to be introduced into the outer main pipe cavity; the inner feed pipe 111 extends tangentially from the circular wall of the inner main pipe 11 into the outer feed pipe 121 and projects outwards to enable the feed swirl to be introduced into the inner main pipe cavity. No matter the gasification raw material or the gasification agent is conveyed in a fluid form, and enters the material cavity along the tangential direction, the gasification raw material or the gasification agent surrounds along the inner wall of the material cavity to form feeding rotational flow, so that the gasification raw material or the gasification agent fully flows, the retention time is long, and the material distribution is convenient to be uniform.

The material flow falls in the material chamber due to its own weight, so that the bottom wall is preferably inclined downwards to facilitate the material flow entering each material distributing hole for distributing material. In the present embodiment, the bottom wall (or bottom) of the outer main tube 12 and the bottom wall (or bottom) of the inner main tube 11 are each preferably funnel-shaped, i.e., in the form of a conical wall (or cone) having a lower apex. Thus, the material flow sinking to the bottom of the material cavity can conveniently flow into the material distributing hole along the conical wall.

However, the stream with solid particles may be deposited at the lower apex (i.e., the lower point) of the conical wall. Therefore, in the present invention, if the materials conveyed in the inner and outer main pipes have solid particles, the distributor 1 may further comprise an inner blowback pipe 113 and/or an outer blowback pipe 123 of a sleeve structure, the outer blowback pipe 123 is communicated with the material chamber of the outer main pipe at a low point of the bottom wall of the outer main pipe 12, and the inner blowback pipe 113 communicated with the material chamber of the inner main pipe extends from the low point of the bottom wall of the inner main pipe 11 into the outer blowback pipe 123 and extends outward. The material flow deposited can be upwards raised through the back-blowing air inlet of the back-blowing pipe, so that the fluid in the material cavity is always in a fluidized state, the blockage is prevented, and the uniform distribution of the materials is ensured. Of course, it will be understood by those skilled in the art that if only the gasifying agent is fed into the inner main pipe or the outer main pipe, i.e. there is no clogging, there is no need to provide a corresponding blowback pipe.

More preferably, the distributor 1 further comprises an inner main pipe gas distributor 114 and/or an outer main pipe gas distributor 124, the inner main pipe gas distributor 114 is disposed at the low point of the inner main pipe material cavity to disperse the blowback gas of the inner blowback pipe 113, and the outer main pipe gas distributor 124 is disposed at the low point of the outer main pipe material cavity to disperse the blowback gas of the outer blowback pipe 113. The gas distributor can be a cavity shell with various air holes on the top arc surface of a simple structure, the gas inlet dispersion of the back flushing pipe can be more uniform by arranging the gas distributor, and the flow field in the material cavity cannot be excessively stirred.

Referring to fig. 3 and 4, the inner branch pipe 112 and the outer branch pipe 122, the inner blowback pipe 113 and the outer blowback pipe 123, and the inner feed pipe 111 and the outer feed pipe 121 are three sets of sleeves constituting a sleeve structure. In each group of sleeve structures, the extending end (namely the outer end) of the inner sleeve is flush with or extends out of the extending end of the outer sleeve, so that the butt joint operation of the outer end of the inner sleeve and the connecting pipe is facilitated, and the feeding and discharging of the inner sleeve can not be influenced by the outer sleeve.

On the basis of the sleeve type material distributing pipe, the invention also provides a material distributing and spraying assembly which comprises a nozzle device 2 and the material distributor 1. The nozzle device 2 includes a nozzle arrangement panel 21 and a plurality of nozzle units 22 mounted thereon, the nozzle units 22 are also of a sleeve structure and can be butted against corresponding distributing sleeve units through connecting short pipes 4 and the like, and the plurality of nozzle units 22 are arranged on the nozzle arrangement panel 21 at intervals and penetrating through each other. In this way, the feed streams from the plurality of feed sleeve units may be vertically injected into the gasifier through the respective nozzle units 22.

Similarly, when a plurality of distributing sleeve units are arranged in a ring shape, a plurality of nozzle units 22 abutting against the distributing sleeve units are also arranged on the nozzle arrangement panel 21 at equal intervals in a ring shape. The nozzle unit 22 is preferably vertically inserted on the nozzle arrangement panel 21. Among them, the nozzle unit 22 may be mounted on the nozzle arrangement panel 21 in various suitable manners. In the present embodiment, a screw connection method is preferably adopted, that is, a through threaded mounting hole is provided on the nozzle arrangement panel 21, and the nozzle unit 22 is screwed to the threaded mounting hole through a connecting thread provided on the outer pipe wall. The screw connection mode not only facilitates the disassembly and replacement, but also facilitates the arrangement and maintenance of the cooling pipe and the like.

To control the temperature of the nozzle units 22 and extend the useful life, the dispensing spray assembly may also include a nozzle cooling system. As shown in fig. 5, the nozzle cooling system includes a plurality of removable tees 224 for flowing a cooling medium in or out and cooling pipe units provided around each nozzle unit 22 in the nozzle arrangement panel 21, the cooling pipe units of any adjacent two nozzle units 22 being connected by the removable tees 224. Two ports of the detachable tee 224 are respectively connected with two adjacent cooling pipe units, and the other port can be used as a cooling medium inlet 221 or a cooling medium outlet 222. Preferably, the cooling medium inlets 221 and the cooling medium outlets 222 are circumferentially spaced apart to provide uniform and reasonable cooling medium flow for each cooling unit. Among them, the cooling pipe unit may be embedded in the nozzle arrangement panel 21 and wound outside the nozzle unit 22, fixed by the nozzle unit fixing panel 223 at the top of the nozzle arrangement panel 21, leaving only the cooling medium inlet 221 and the cooling medium outlet 222 to the outside.

In addition, a plurality of water vapor inlets 211 may be further penetratingly disposed on the nozzle arrangement panel 21, and the plurality of water vapor inlets 211 are arranged around the plurality of nozzle units 22. The steam inlet 211 is used to inject steam into the gasification furnace so as to realize the water gas reaction. The number of the water vapor inlets 211 provided on the nozzle arrangement panel 21 is set according to the panel size and the process requirements, and is preferably 3 to 72, for example.

In addition, the present invention also provides a gasification furnace as shown in fig. 2, which comprises a furnace body 3 and the above-mentioned divided material injection assembly, the nozzle arrangement panel 21 of which is installed on the top of the furnace body 3.

An overhead multi-nozzle configuration was used here, as gasification chill experiments showed: the overhead single-nozzle jet distance is longer, while the overhead multi-nozzle jet distance is relatively shorter; from the view of dispersion effect, the multi-nozzle dispersion effect is obviously better than that of a single nozzle. FIG. 1 shows the comparison of radial mean velocity distribution of cross-section of single nozzle and multi-nozzle under the same experimental conditions, and it can be seen from FIG. 1 that the velocity of the central jet in the furnace body of the single nozzle is nearly 70m/s, the velocity distribution in the radial position is in a sharp downward trend, and the velocity distribution of the overhead multi-nozzle is more gentle. From the high speed camera, a single nozzle and multi-nozzle flow field map (not shown) under the same conditions can be tracked, which shows that the concentration of particles on the furnace wall is higher and the area of high concentration is larger for the single nozzle, while the particle concentration is slightly higher for the multi-nozzle only near the nozzle, but far lower than the single nozzle concentration, and the area of high concentration for the multi-nozzle is far smaller than the single nozzle, and the top-mounted multi-nozzle will form two opposite swirls on both sides of the center in the gasifier, and the swirl size is smaller. Thus, there is a small amount of back-mixing at both sides of the furnace with multiple nozzles at the top, but there is essentially no back-mixing at the center of the furnace.

Therefore, the overhead multi-nozzle has the advantages of short injection distance, good dispersion effect and the phenomenon of back mixing of the flow field in the furnace at two sides. The results of the tests also demonstrate that the gasification space required for an overhead multi-nozzle is much smaller than for a single nozzle, reducing the space occupied by the gasification chamber. Of course, the present invention is not limited to the above-described overhead nozzle structure, and, for example, an overhead nozzle of a shell-and-tube coaxial jet structure, etc. may be employed; the distributor is not limited to the single-stage and single-sleeve structure, and can also be a multi-stage grading and multi-sleeve distributing structure and the like

The invention not only adopts the material-distributing injection assembly with the sleeve-type material-distributing pipe and the multiple overhead nozzles, but also optimizes the design of the furnace body structure. As shown in fig. 2, the furnace body 3 includes a gasification section having a gasification chamber 31, a buffer section having a buffer chamber 32, and a quench section having a quench chamber 33 from top to bottom, the gasification chamber 31 communicates with the quench chamber 33 through the buffer chamber 32, and a nozzle arrangement panel 21 is horizontally installed on a top cover of the gasification section so that gasification raw materials, a gasification agent, and steam can be injected vertically downward toward the gasification chamber 31 through a nozzle unit 22 and a steam inlet 211 so as to generate a gasification reaction. It is known to those skilled in the art that the carbon conversion can be effectively increased by introducing more steam through the steam inlet 211 to enhance the water gas reaction. The combustion reaction and the water gas reaction are completed in the gasification chamber 31, and the reaction products including the raw synthesis gas and the gasification residues reach the chilling chamber 33 through the buffer chamber 32 and are finally discharged from the synthesis gas outlet 34 and the slag discharge port 334 respectively. Of course, it can be understood by those skilled in the art that the water vapor can be supplemented through the water vapor inlet 211 to prevent the insufficient supply of the consumed water vapor, but the invention is not limited thereto, and the water vapor can be supplied to the gasification furnace together with the oxygen through the outer tube.

The design purpose of the buffer section is to consider that the gasification temperature is too high on one hand, and if a water-cooled wall is arranged in the buffer section, the temperature of the synthesis gas passing through the buffer section is reduced; secondly, the buffer section is communicated with the gasification chamber, so that the gasification reaction time can be properly increased.

In particular, the bottom end of the gasification section is formed as a throat structure which is connected obliquely downwards to the buffer section. The necking design of the gasification chamber reduces the space of the gasification chamber, can improve the gasification reaction temperature and can also lead CO to be generated₂、H₂O and partial unreacted carbon residue and other substances touch the bottom wall and then flow back to the gasification chamber 31 for continuous reaction, so that the secondary reactant CO can be effectively increased₂And H₂The concentration of O and the reaction residence time, thereby increasing the carbon conversion. Through the gasification furnace, the carbon conversion rate can reach more than 99 percent, the composition of the synthesis gas reaches more than 90 percent, and the specific oxygen consumption is about 290Nm³/1000Nm³(CO+H₂)。

Because the overhead multi-nozzle of the gasification chamber has the characteristics of good gas-solid mixing effect, short flame, high temperature and the like, compared with the gasification chamber of the existing gasification furnace, the height of the gasification chamber 31 can be shortened, the width of the gasification chamber 31 can be wider, so that a plurality of nozzles are better arranged, and the design of the necking structure is favorable for reacting gas and unreacted gasThe complete gasified feedstock is refluxed (back-mixed) to a high temperature flame to generate C and CO₂The secondary reaction of (2) improves the carbon conversion rate. The design of shortening the radial dimension of the buffer chamber 32 can shorten the gas retention time and reduce the size of the furnace body and the investment cost.

In the present embodiment, as shown in fig. 2, the gasification chamber 31 and the buffer chamber 32 are preferably cylindrical chambers, the height H1 of the gasification chamber 31 does not exceed 1/3, preferably 1/6 to 1/3, of the total height H of the furnace body 3, and the ratio of the inner diameter of the gasification chamber 31 to the inner diameter of the buffer chamber 32 is not less than 2, preferably 2 to 10 according to practical applications. The design of the inverted H-shaped furnace body reduces the furnace body volume and the investment cost of the gasification furnace. The arrangement of the overhead parallel multi-nozzle and the design of the inverted I-shaped furnace body also strengthen the mixing of gas and solid. In addition, a water-cooled wall 311 is continuously arranged on the inner wall of the gasification chamber 31 and the inner wall of the buffer cavity 32 to protect the inner wall of the furnace body.

In particular, a quench ring 331 is also mounted at the top of the quench chamber 33 at the junction with the buffer chamber 32, the quench ring 331 having a downcomer 332 connected thereto that extends toward the slag bath 333. The quench ring 331 is configured to facilitate subsequent processing (e.g., dust removal, desulfurization cleaning, etc.) of the quenched syngas. Among the reaction products reaching the chilling chamber 33 through the buffer chamber 32, the raw synthesis gas is chilled by the chilling ring 331, then the speed is reduced, the temperature is reduced, the raw synthesis gas enters the slag bath 333 water from the down pipe 332 so as to remove more fly ash, and finally the raw synthesis gas is discharged from the synthesis gas outlet 34 formed on the peripheral wall of the chilling chamber 33 and goes to the synthesis gas treatment unit. The resulting slag (i.e., gasification residue) may form a slag layer on the water cooled wall 311 to protect the water cooled wall 311, and excess slag typically falls along the water cooled wall 311 into a slag bath 333 at the bottom of the quench chamber 33 and is discharged from a slag tap 334.

The principle of the gasification process using the above-described gasification furnace of the present invention is shown in fig. 6, and the process includes a gasification reaction step including inputting one of a gasification raw material and a gasification agent through the outer feed pipe 121 of the distributor, inputting the other of the gasification raw material and the gasification agent through the inner feed pipe 111, and supplementing water vapor through the water vapor inlet 211 on the nozzle arrangement panel 21, so that the gasification raw material undergoes a gasification reaction under gasification conditions in the gasification furnace, producing a raw synthesis gas and gasification residues to be discharged to the outside.

Wherein the gasification reaction temperature in the gasification chamber 31 is preferably kept between 1300 ℃ and 3000 ℃, more preferably between 1500 ℃ and 2800 ℃, even 1900 ℃ and 2500 ℃ to smoothly complete the combustion reaction and the water gas shift reaction (CO + H)₂O→CO₂+H₂，C+H₂O→CO+H₂). Compared with the gasification furnace in the prior art, the gasification temperature of the gasification furnace can be increased to more than 2800 ℃, and the subsequent process parameters such as the outlet temperature of the synthesis gas and the temperature of gasification residues can be ensured to be slightly influenced as long as the water-cooled wall and the chilling heat exchange are enough; after the gasification temperature is increased, the gasification reaction is faster by combining the gas-solid mixing effect of the multi-nozzle arranged at the top, the residence time of the gasification chamber can be less than 0.5s or even shorter, and the residence time of the buffer section is also less than 0.5s or even shorter.

In particular, the gasification process may further comprise a syngas filtration step comprising:

drying the gasification residue produced in the gasification reaction step to form a porous particulate material; contacting the raw synthesis gas with a porous particulate material to filter fly ash in the raw synthesis gas;

and taking the porous granular material with the temperature of 105-200 ℃ and the grain diameter of 0.1-15 mm after drying as a filter medium, and filtering fly ash in the rough synthesis gas at about 300 ℃ after chilling through the dried porous granular material.

Wherein, the gasification residue is used as a filter medium to remove fly ash in the synthesis gas, so that the investment cost of the gasification process can be reduced to a great extent. Because the material components of the gasification residue and the fly ash are basically similar, and the porosity of the quenched gasification residue is higher, the fly ash is easy to adsorb and gasify the residue, and the ash removal effect is better. Wherein, the water-containing volume of the dried gasification residue is not more than 50 percent of the total volume, preferably 0-30 percent, so as to have better adsorption effect on the fly ash.

Specifically, the dried gasification residue may be fed to the moving bed 7, and the raw synthesis gas is filtered through the dried gasification residue (i.e., porous particulate material) in the moving bed 7. Then, the gasification process further comprises a synthesis gas purification step of washing the filtered raw synthesis gas at about 200 ℃ by venturi washing equipment 8, thereby obtaining a purified synthesis gas.

Referring to fig. 6, the system for producing synthesis gas by coal gasification using the above method comprises:

a gasification raw material crushing, drying and transporting system 5 for producing and transporting dry coal powder or coal water slurry;

the gasification furnace is communicated with the gasification raw material crushing, drying and conveying system 5, and dry coal powder or coal water slurry is subjected to gasification reaction in the gasification furnace in the presence of a gasification agent to generate crude synthesis gas and gasification residues;

Wherein the raw synthesis gas is preferably efficiently filtered in the moving bed 7.

Wherein, the total process comprises the following steps: after the gasification raw materials enter a furnace body 3 of a gasification furnace through a gasification raw material crushing, drying and conveying system 5, gasification reaction is carried out in a gasification chamber 31 with the temperature of 1500-2500 ℃, part of gasification residues are discharged from a slag discharging system 6 at the bottom of the furnace body, the other part of gasification residues are dried and then enter a moving bed ash removal system, and the gasified crude synthesis gas is subjected to ash removal through the moving bed ash removal system and then is purified through a Venturi washing device 8 and synthesis gas to form a clean synthesis gas product.

Compared with the prior art, the gasification furnace and the gasification process thereof provided by the invention have at least the following beneficial technical effects:

a) the sleeve type distributor can separate the gasification agent and the gasification raw material into a plurality of channels, a feeding port adopts tangential rotational flow feeding, and the bottom of the sleeve type distributor is provided with distributed back-blowing holes so as to keep the material in a fluidized state all the time, thus not only ensuring the uniformity of material distribution, but also preventing the pipeline from being blocked;

b) the nozzles formed by each channel are independent, the upper part and the lower part of each nozzle are connected in an internal and external thread mode, the cooling water inlet and the cooling water outlet of each nozzle are connected by a detachable tee joint, and each nozzle is convenient to mount and dismount and simple to operate;

c) the top parallel multi-nozzle arrangement and the similar inverted H-shaped furnace body design strengthen the mixing between gas and solid, and the necking design of the furnace body gasification chamber reduces the space of the gasification chamber, thereby not only improving the gasification reaction temperature, but also leading CO to be capable of₂、H₂And substances such as O, part of unreacted residual carbon and the like flow back to the gasification chamber to continue to react, so that the reaction residence time and the reactant concentration are improved to a certain extent, and the carbon conversion rate is improved. In addition, the design of the inverted H-shaped furnace body reduces the volume of the gasification furnace body and the investment cost thereof.

d) And the gasification residue is used as a filter medium to remove fly ash in the synthesis gas, so that the investment cost of the gasification process is reduced to a great extent. Because the material components of the gasification residue and the fly ash are basically similar, and the porosity of the quenched residue is higher, the fly ash is easy to adsorb and gasify the residue, and the ash removal effect is better.

The preferred embodiments of the present invention have been described in detail with reference to the accompanying drawings, however, the present invention is not limited to the details of the above embodiments, and various simple modifications can be made to the technical solution of the present invention within the technical idea of the present invention, for example, the bottom wall shape of the outer main tube or the inner main tube in the sleeve type distributor is not limited to the conical shape having a lower vertex, and may be a hemisphere with a wall surface inclined downward, etc.; the connection mode between the material distributing sleeve unit and the nozzle unit is not limited to the sleeve butt joint mode shown in the figure, and the material distributing sleeve unit and the nozzle unit can be connected in a bypass mode; the top of the furnace body is not limited to be cylindrical, and can also be hemispherical and the like; these simple variants fall within the scope of protection of the present invention.

The various features described in the foregoing detailed description may be combined in any suitable manner without departing from the scope of the invention, and various combinations that are possible are not further described in order to avoid unnecessary repetition.

In addition, any combination of the various embodiments of the present invention is also possible, and the same should be considered as the disclosure of the present invention as long as it does not depart from the spirit of the present invention.

Claims

1. Carbonaceous fuel tripper, this tripper (1) are including outer person in charge (12) and interior main pipe (11), outer person in charge in outer person in charge (12) material chamber with interior person in charge in interior main pipe (11) material chamber be independent and isolated closed cavity each other, interior main pipe (11) are including the intercommunication respectively interior inlet pipe (111) and a plurality of interior branch material pipe (112) in the interior main pipe material chamber, outer person in charge (12) are including all the intercommunication outer inlet pipe (121) and a plurality of outer branch material pipe (122) in outer person in charge material chamber, wherein every interior branch material pipe (112) all stretch into corresponding outwards extend in outer branch material pipe (122) and form and divide material sleeve pipe unit.

2. The carbonaceous fuel distributor according to claim 1, wherein a plurality of the outer distributing pipes (122) are arranged on and extend from the bottom wall of the outer main pipe (12) in an annular equal interval, a plurality of the inner distributing pipes (112) are also arranged on the bottom wall of the inner main pipe (11) in an annular equal interval, and each inner distributing pipe (112) coaxially extends from the bottom wall of the inner main pipe (11) into the corresponding outer distributing pipe (122), so as to form a plurality of distributing sleeve units in an annular arrangement.

3. The carbonaceous fuel distributor according to claim 2, wherein the number of the inner and outer distributor pipes (112, 122) is the same and not less than 3.

4. The carbonaceous fuel distributor according to claim 2, wherein the bottom end of the outer main pipe (12) and the bottom of the inner main pipe (11) are both cones or hemispheres with a lower apex.

5. The carbonaceous fuel distributor according to claim 2, wherein the distributor (1) further comprises an inner blowback pipe (113) and/or an outer blowback pipe (123), the outer blowback pipe (123) communicates with the outer main pipe material cavity at a low point of the bottom of the outer main pipe (12), and the inner blowback pipe (113) communicating with the inner main pipe material cavity extends from the low point of the bottom of the inner main pipe (11) into the outer blowback pipe (123) and protrudes outward.

6. The carbonaceous fuel distributor according to claim 5, wherein the distributor (1) further comprises an inner main pipe gas distributor (114) and/or an outer main pipe gas distributor (124), the inner main pipe gas distributor (114) being disposed at a low point of the inner main pipe material chamber to distribute blowback gas of the inner blowback pipe (113), the outer main pipe gas distributor (124) being disposed at a low point of the outer main pipe material chamber to distribute blowback gas of the outer blowback pipe (113).

7. The carbonaceous fuel distributor according to any one of claims 5 to 6, wherein the upper ports of the inner main pipe (11) and the outer main pipe (12) are closed, and the outer feed pipe (121) tangentially extends from the circular pipe wall of the outer main pipe (12) to enable feeding swirl flow into the outer main pipe feed cavity; the inner feeding pipe (111) extends from the circular pipe wall of the inner main pipe (11) to the inside of the outer feeding pipe (121) along the tangential direction and extends outwards so as to introduce feeding rotational flow into the inner main pipe cavity.

8. The carbonaceous fuel dispenser according to claim 7, wherein the protruding end of the inner sleeve in the sleeve structure is flush with or protrudes beyond the protruding end of the outer sleeve in the inner branch pipe (112) and the outer branch pipe (122) constituting the sleeve structure, the inner blowback pipe (113) and the outer blowback pipe (123) constituting the sleeve structure, and the inner feed pipe (111) and the outer feed pipe (121) constituting the sleeve structure.

9. A dispensing jet assembly comprising a nozzle arrangement panel (21), a plurality of nozzle units (22) and a dispenser (1) according to any one of claims 1 to 8, the nozzle units (22) being of a sleeve structure and abutting against the corresponding dispensing sleeve units, the plurality of nozzle units (22) being spaced from each other and disposed through the nozzle arrangement panel (21).

10. A feed splitter and spray assembly as claimed in claim 9, wherein the nozzle arrangement panel (21) is provided with a threaded mounting hole therethrough to which the nozzle unit (22) is screwed by means of a connecting thread provided on the outer pipe wall.

11. A feed divider spray assembly according to claim 9 wherein a plurality of said nozzle units (22) are arranged in an annular equally spaced arrangement on said nozzle arrangement panel (21).

12. A feed distribution spray assembly as claimed in claim 11 further comprising a nozzle cooling system including a plurality of removable tees (224) for the inflow or outflow of a cooling medium and cooling tube units disposed about each of said nozzle units (22) in said nozzle arrangement panel (21), said cooling tube units of any two adjacent nozzle units (22) being connected by said removable tees (224).

13. A feed divider spray assembly according to any of claims 9 to 12 wherein said nozzle arrangement panel (21) further has a plurality of water vapor inlets (211) disposed therethrough, said plurality of water vapor inlets (211) being arranged around a plurality of said nozzle units (22).

14. Gasifier, comprising a furnace body (3) and a split-material injection assembly according to any one of claims 9 to 13, the nozzle arrangement panel (21) of which is mounted on top of the furnace body (3).

15. A gasifier according to claim 14, wherein the furnace body (3) comprises a gasification section with a gasification chamber (31), a buffer section with a buffer chamber (32) and a quench section with a quench chamber (33) from top to bottom, the gasification chamber (31) communicating with the quench chamber (33) through the buffer chamber (32), the nozzle arrangement panel (21) being horizontally mounted on a roof of the gasification section such that gasification feedstock and gasification agent can be injected vertically downwards towards the gasification chamber (31) through the nozzle unit (22).

16. The gasification furnace of claim 15, wherein a bottom end of the gasification stage is formed as a throat structure connected obliquely downward to the buffer stage.

17. The gasification furnace according to claim 16, wherein the gasification chamber (31) and the buffer chamber (32) are both cylindrical chambers, the height of the gasification chamber (31) does not exceed 1/3 of the total height of the furnace body (3), the height of the buffer chamber (32) does not exceed 1/3 of the total height of the furnace body (3), and the ratio of the inner diameter of the gasification chamber (31) to the inner diameter of the buffer chamber (32) is not less than 2.

18. A gasifier according to claim 17, wherein the height of the gasification chamber (31) is 1/6-1/3 of the total height of the furnace body (3); the ratio of the inner diameter of the gasification chamber (31) to the inner diameter of the buffer chamber (32) is 2 to 10.

19. A gasifier according to claim 16, wherein water walls (311) are arranged in succession on the inner walls of said gasification chamber (31) and of said buffer chamber (32).

20. A gasifier according to claim 15, wherein a syngas outlet (34) is formed on a peripheral wall of the quench chamber (33), a bottom of the quench chamber (33) is formed as a slag bath (333), and a ratio of an inner diameter of the quench chamber (33) to an inner diameter of the buffer chamber is 1.2-1.5.

21. A gasifier according to claim 20, wherein a quench ring (331) is installed at the connection of the top of said quench chamber (33) and said buffer chamber (32), and a downcomer (332) extending into said slag bath (333) is connected to said quench ring (331).

22. The gasification furnace according to claim 14, wherein the reaction temperature of the gasification furnace is 1300 ℃ to 3000 ℃.

23. The gasifier of claim 22, wherein the reaction temperature of the gasifier is 1500 ℃ to 2800 ℃.

24. The gasifier of claim 23, wherein the reaction temperature of the gasifier is 1900 ℃ to 2500 ℃.

25. A method for gasification of synthesis gas using the gasifier of any one of claims 14 to 24, the method comprising:

a gasification step: inputting a gasification raw material and a gasification agent into a gasification furnace, and enabling the gasification raw material to generate gasification reaction in the gasification furnace under gasification conditions and generate crude synthesis gas and gasification residues; and

and (3) filtering the synthesis gas: drying the gasification residue to form a porous particulate material; contacting the raw syngas and the porous particulate material to filter fly ash in the raw syngas.

26. The method of claim 25, wherein the gasifying step further comprises chilling the gasification residue and the raw syngas within the gasifier and discharging the chilled gasification residue and raw syngas out of the gasifier.

27. The method according to claim 25, wherein the temperature of the porous particulate material is controlled to be 105 to 200 ℃ and the particle size is controlled to be 0.1 to 15mm when the raw synthesis gas and the porous particulate material are contacted to filter fly ash.

28. The method of claim 25, wherein the aqueous volume of the porous particulate material is controlled to be no more than 50% of the total volume of the porous particulate material after the gasification residue is dried.

29. The method as claimed in claim 28, wherein the water-containing volume of the porous particulate material is controlled to be not more than 0-30% of the total volume of the porous particulate material after the gasification residue is dried.

30. A method according to claim 25, wherein, in the synthesis gas filtration step, the dried porous particulate material is fed to a moving bed (7) and the raw synthesis gas is filtered through the porous particulate material in the moving bed (7).

31. The method of claim 25, further comprising:

a step of synthesizing, purifying and filtering: washing the filtered raw synthesis gas to further remove fly ash.

32. A system for gasification of synthesis gas using the gasifier of any one of claims 14 to 24, comprising:

a gasification raw material crushing, drying and transporting system (5) for producing and transporting dry coal powder or coal water slurry;

the gasification furnace is communicated with the gasification raw material crushing, drying and transporting system (5), and in the gasification furnace, the dry coal powder or the coal water slurry is subjected to gasification reaction in the presence of a gasification agent to generate crude synthesis gas and gasification residues;

a drying unit communicating with the slag discharge system, in which at least a part of the gasification residue is dried to be formed into a porous particulate material; and

and a filtering and ash removing system communicated with the drying unit and the gasification furnace, wherein the crude synthesis gas and the porous particle material are contacted to filter fly ash in the crude synthesis gas.

33. The system according to claim 32, wherein the filtration ash removal system comprises a moving bed (7), the raw synthesis gas being contacted with the porous particulate material in the moving bed (7) for filtering fly ash.