CN212560114U - Coal catalytic gasification reactor - Google Patents

Abstract

The utility model relates to a coal catalytic gasification field provides a coal catalytic gasification reactor. The reactor comprises a gasification furnace and a synthetic gas inlet system, wherein the top of the gasification furnace is provided with a crude gas outlet, and a dense-phase bed layer is arranged in the gasification furnace; the synthetic gas inlet system comprises a primary synthetic gas inlet cavity and a synthetic gas return tube, the primary synthetic gas inlet cavity is arranged at the lower part of the dense-phase bed layer, one end of the synthetic gas return tube is communicated with the crude gas outlet, the other end of the synthetic gas return tube penetrates through the side wall of the gasification furnace and is communicated with the primary synthetic gas inlet cavity, and a plurality of first exhaust holes are formed in the peripheral wall of the primary synthetic gas inlet cavity, so that the synthetic gas can enter the lower part of the dense-phase bed layer in a substantially horizontal mode and then flows through the whole dense-phase bed layer from bottom to top, and then is fully mixed and contacted with solid-phase bed materials, and methanation exothermic reaction is fully generated under the action.

Description

Coal catalytic gasification reactor

Technical Field

The utility model relates to a coal catalytic gasification field, concretely relates to coal catalytic gasification reactor.

Background

The coal catalytic gasification technology is one of the most effective technological approaches for preparing natural gas from coal, and the technical principle is that under the action of a multifunctional catalyst, coal gasification, transformation and methanation are simultaneously carried out in a reactor by coal and a gasifying agent, so that endothermic reaction and exothermic reaction are effectively coupled, and the methane yield and the system energy efficiency are greatly improved.

In order to realize the coupling of the carbohydrate endothermic reaction and the methanation reaction of the synthesis gas, reduce the oxygen consumption and the coal consumption to the maximum extent and improve the primary methane content at the outlet of the gasification furnace, the synthesis gas (CO and H2) generated by the system needs to be circularly returned to the gasification furnace for continuously generating the methanation exothermic reaction after being subjected to subsequent purification and separation system separation, so that heat is provided for the carbohydrate endothermic reaction, and the carbon loss caused by oxygen-introducing combustion is further reduced. After entering the gasification furnace, the synthetic gas returning to the furnace is fully contacted and mixed with the solid-phase bed material, and methanation reaction is carried out under the action of a catalyst. The return position and the return structure of the synthetic gas relate to the proceeding degree of the reaction in the furnace, the improper return position can cause the problems of local high-temperature slagging or incomplete methanation reaction, and the like, and the improper return structure can cause the problems of uneven dispersion, short circuit, insufficient contact and mixing with a solid-phase catalyst and the like of the synthetic gas entering the furnace, so that the incomplete methanation reaction is caused, and the return of the returned gas is meaningless.

Therefore, aiming at the catalytic gasification process, the development of the catalytic gasification reactor and the synthesis gas furnace-entering system which have reasonable structures, can realize the uniform mixing and sufficient reaction of the synthesis gas entering the furnace and the solid-phase bed material is very important.

SUMMERY OF THE UTILITY MODEL

The utility model discloses it is unreasonable that current catalytic gasification reactor synthetic gas returns the structure setting, leads to the synthetic gas of returning to disperse inequality in the gasifier, with the insufficient technical problem of solid-phase bed material reaction.

In order to solve the technical problem, the utility model provides a coal catalytic gasification reactor, which comprises a gasification furnace and a synthetic gas inlet system, wherein the top of the gasification furnace is provided with a crude gas outlet, and a dense bed layer is arranged in the gasification furnace; the synthetic gas inlet system comprises a primary synthetic gas inlet cavity and a synthetic gas return furnace tube, the primary synthetic gas inlet cavity is arranged at the lower part of the dense-phase bed layer, one end of the synthetic gas return furnace tube is communicated with the crude gas outlet, the other end of the synthetic gas return furnace tube penetrates through the side wall of the gasification furnace and is communicated with the primary synthetic gas inlet cavity, and a plurality of first exhaust holes are formed in the peripheral wall of the primary synthetic gas inlet cavity.

Optionally, a second-stage synthesis gas inlet cavity is sleeved outside the first-stage synthesis gas inlet cavity, and a plurality of second exhaust holes are formed in the peripheral wall of the second-stage synthesis gas inlet cavity.

Optionally, the first exhaust hole is inclined to the circumferential direction of the primary syngas inlet chamber.

Optionally, the second exhaust hole is inclined towards the circumferential direction of the secondary syngas intake cavity, and the inclination direction of the first exhaust hole is consistent with the inclination direction of the second exhaust hole.

Optionally, the space of the first exhaust hole extending outward is staggered with the second exhaust hole; and/or the presence of a gas in the gas,

the aperture of the second exhaust hole is larger than that of the first exhaust hole.

Optionally, the synthesis gas return furnace tube is provided with a buffer ball.

Optionally, the gasification furnace comprises a conical distribution plate, a bottom reducing section, a middle straight pipe section and a top necking section which are sequentially connected from bottom to top; the conical distribution plate is in a truncated cone shape with the diameter gradually increasing from bottom to top, a plurality of horizontal air inlets are formed in the peripheral wall of the conical distribution plate, and the horizontal air inlets are used for introducing gasification agents into the gasification furnace; a central jet pipe penetrates through an opening at the bottom of the conical distribution plate and is used for injecting a gasification agent into the gasification furnace, and an annular ash residue outlet is formed between the central jet pipe and the opening at the bottom of the conical distribution plate; the diameter of the bottom diameter-changing section is gradually increased from bottom to top; the dense-phase bed layer is arranged in the middle straight pipe section; the top end of the top necking section forms the crude gas outlet.

Optionally, the top end of the central jet pipe is higher than the ash outlet, and the horizontal air inlet is higher than the top end of the central jet pipe.

Optionally, the syngas returning tube is higher than the maximum jet height of the central jet tube.

Optionally, a set interval is provided between the bottom of the first-stage syngas inlet cavity and the bottom of the dense-phase bed, and the syngas return furnace tube penetrates into the gasification furnace along the bottom region of the dense-phase bed and is communicated with the first-stage syngas inlet cavity.

By last, the utility model provides a coal catalytic gasification reactor, the one-level synthetic gas chamber of admitting air through being provided with a plurality of first exhaust holes on the perisporium, make the synthetic gas can the level or be close the horizontal ground and enter into the lower part on dense bed, and then by lower supreme whole dense bed of flowing through, from this with solid phase bed material intensive mixing, the contact, fully take place methanation exothermic reaction under the catalytic action, avoid the synthetic gas adherence to go upward or direct short circuit goes upward to the export of coarse coal gas and lead to going into the stove dispersion inhomogeneous, methanation takes place incomplete technical problem.

Drawings

The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the present disclosure and together with the description, serve to explain the principles of the disclosure.

In order to more clearly illustrate the embodiments or technical solutions in the prior art of the present disclosure, the drawings used in the description of the embodiments or prior art will be briefly described below, and it is obvious for those skilled in the art that other drawings can be obtained according to the drawings without inventive exercise.

FIG. 1 is a schematic diagram of a coal catalytic gasification reactor according to an embodiment of the present invention;

FIG. 2 is a side view of a primary syngas intake chamber and a secondary syngas intake chamber of an embodiment of the present invention;

fig. 3 is a schematic cross-sectional view of a primary syngas intake chamber and a secondary syngas intake chamber of an embodiment of the invention.

Reference numerals:

10. a conical distribution plate; 11. an ash outlet; 12. a central jet pipe; 2. a bottom reducer section; 3. the junction between the middle straight pipe section and the bottom reducing section; 4. a middle straight pipe section; 41. a raw material coal inlet; 5. a top necked-down section; 51. a raw gas outlet; 6. returning the synthesis gas to a furnace tube; 61. a buffer ball; 71. a primary syngas intake chamber; 72. a secondary syngas intake chamber; 73. a first exhaust port; 74. a second vent hole.

Detailed Description

In order that the above objects, features and advantages of the present disclosure may be more clearly understood, aspects of the present disclosure will be further described below. It should be noted that the embodiments and features of the embodiments of the present disclosure may be combined with each other without conflict.

In the following description, numerous specific details are set forth in order to provide a thorough understanding of the present disclosure, but the present disclosure may be practiced in other ways than those described herein; it is to be understood that the embodiments disclosed in the specification are only a few embodiments of the present disclosure, and not all embodiments.

As shown in fig. 1, the catalytic coal gasification reactor provided by the embodiment of the present invention comprises a gasification furnace and a synthesis gas inlet system, wherein the bottom of the gasification furnace is provided with a gasification agent inlet and an ash outlet 11, the top of the gasification furnace is provided with a crude gas outlet 51, and crude gas generated in the reactor is discharged through the crude gas outlet 51; a dense-phase bed layer is arranged in the gasification furnace, the dense-phase bed layer is generally arranged in the middle area of the gasification furnace, a raw material coal inlet 41 which is communicated to the upper part of the dense-phase bed layer is arranged on the gasification furnace, and pulverized coal particles which enter the raw material coal inlet 41 can be uniformly dispersed on the dense-phase bed layer.

Referring to fig. 1 and fig. 2, the syngas inlet system includes a first-stage syngas inlet chamber 71 and a syngas return tube 6, the first-stage syngas inlet chamber 71 is disposed at the lower portion of the dense-phase bed, and is preferably located at the center of the dense-phase bed, and is preferably in a vertically extending tubular structure, the circumferential wall of the first-stage syngas inlet chamber 71 is provided with a plurality of first exhaust holes 73, and the plurality of first exhaust holes 73 are preferably uniformly distributed on the sidewall of the first-stage syngas inlet chamber 71 in a multi-turn manner; one end of the synthetic gas returning furnace tube 6 is communicated with the crude gas outlet 51, the other end of the synthetic gas returning furnace tube passes through the side wall of the gasification furnace and is communicated with the primary synthetic gas inlet cavity 71, the synthetic gas returning furnace tube 6 is preferably connected to the top or the bottom of the primary synthetic gas inlet cavity 71, and when the primary synthetic gas inlet cavity 71 is of a tubular structure, one end of the primary synthetic gas inlet cavity is not plugged with the synthetic gas returning furnace tube 6. The synthesis gas return tube 6 is preferably further provided with a purification and separation system for filtering and separating the raw gas to obtain a relatively pure synthesis gas (CO and H2), and the purification and separation of the raw gas are well known in the art and will not be described herein.

The embodiment of the utility model provides a coal catalytic gasification reactor, one-level synthetic gas air inlet chamber 71 through being provided with a plurality of first exhaust holes 73 on the perisporium, make the synthetic gas can the level or be close the horizontal ground and enter into the lower part on dense bed, and then by lower supreme whole dense bed of flowing through, from this with solid phase bed material intensive mixing, the contact, fully take place exothermic methanation under the catalytic action, avoid the synthetic gas adherence to go upward or direct short circuit goes upward to coarse coal gas export 51 and lead to going into the stove dispersion inhomogeneous, methanation takes place incomplete technical problem.

Referring to fig. 2 and 3, in some embodiments, a secondary syngas inlet chamber 72 is sleeved outside the primary syngas inlet chamber 71, and a plurality of second exhaust holes 74 are formed in the peripheral wall of the secondary syngas inlet chamber 72. The secondary syngas inlet cavity 72 is preferably a vertically extending tubular structure, an annular chamber is formed between the secondary syngas inlet cavity 72 and the primary syngas inlet cavity 71, and the syngas discharged from the primary syngas inlet cavity 71 is buffered by the annular chamber and then introduced into the gasifier. In the process of entering and discharging the synthesis gas from the primary synthesis gas inlet cavity 71, because the flow direction of the gas flow changes, the exhaust pressure of each first exhaust hole 73 on the primary synthesis gas inlet cavity 71 is different, and if the synthesis gas is directly discharged into the gasification furnace, the distribution of the exhaust gas in all directions is uneven, thereby affecting the mixing effect with the solid-phase bed material. In the embodiment, the annular chamber formed by the primary syngas inlet chamber 71 and the secondary syngas inlet chamber 72 can perform rectification and pressure equalization on the syngas, so that the syngas discharged from the primary syngas inlet chamber 71 is buffered to a certain extent and then discharged into the gasifier, and the syngas can be dispersed more uniformly to the surrounding dense phase bed.

In a further embodiment, as shown in FIG. 3, the first exhaust holes 73 are inclined towards the circumferential direction of the primary syngas inlet chamber 71, such that the syngas discharged from the first exhaust holes 73 forms a swirling flow in the annular chamber, thereby improving the homogenization buffer effect of the syngas pressure.

In still further embodiments, the second outlet holes 74 are inclined to the circumferential direction of the secondary syngas intake chamber 72, and the direction of inclination of the second outlet holes 74 coincides with the direction of inclination of the first outlet holes 73. Therefore, on one hand, the cyclone synthesis gas formed in the annular chamber can enter the second exhaust holes 74 more smoothly, and on the other hand, the synthesis gas can enter the dense-phase bed layer in a cyclone spraying mode, so that the synthesis gas is distributed more uniformly in the circumferential direction.

In still further embodiments, as shown in fig. 2 and 3, the space where the first venting holes 73 extend outward is offset from the second venting holes 74, i.e., the space where the first venting holes 73 extend outward in the venting direction does not overlap any of the second venting holes 74; specifically, taking the first exhaust holes 73 and the second exhaust holes 74 as examples, both of which extend radially outward, the distribution positions of the plurality of first exhaust holes 73 and the distribution positions of the plurality of second exhaust holes 74 are staggered in the axial direction and the circumferential direction. Therefore, the synthesis gas is discharged from the first exhaust hole 73 and then does not directly enter the second exhaust hole 74, the airflow path of the synthesis gas from the first exhaust hole 73 to the second exhaust hole 74 is prolonged, and the pressure equalization and rectification effects of the annular chamber on the synthesis gas are improved. The diameter of the second exhaust hole 74 is preferably larger than the diameter of the first exhaust hole 73, so that the exhaust pressure can be reduced and the synthesis gas can be smoothly and smoothly discharged from the second exhaust hole 74.

As shown in FIG. 1, in some embodiments, the syngas returning furnace tube 6 is provided with a buffering ball 61, the buffering ball 61 is preferably disposed on a portion of the syngas returning furnace tube 6 located outside the gasification furnace and adjacent to the sidewall of the gasification furnace, and the buffering ball 61 is a spherical pipe section with a larger diameter formed on the syngas returning furnace tube 6 for rectifying the syngas. When the synthesis gas enters the buffer ball 61, the flow rate is reduced, and the turbulent flow generated in the upstream transmission process of the synthesis gas is greatly eliminated, so that the synthesis gas can be more smoothly led to the downstream primary synthesis gas inlet cavity 71, and the pressure distribution of the synthesis gas in the primary synthesis gas inlet cavity 71 is improved.

In some embodiments, the gasification furnace comprises a conical distribution plate 10, a bottom reducing section 2, a middle straight pipe section 4 and a top necking section 5 which are sequentially connected from bottom to top; the conical distribution plate 10 is a truncated cone with the diameter gradually increasing from bottom to top, the cone angle can be 60-90 degrees, the outer side of the conical distribution plate is a metal wall surface, wear-resistant and high-temperature-resistant castable is poured inside the conical distribution plate, a plurality of horizontal air inlets are formed in the peripheral wall of the conical distribution plate 10, and the horizontal air inlets are used for introducing gasification agents into the gasification furnace; the diameter of the bottom reducing section 2 is gradually increased from bottom to top, the reducing angle can be 3-6 degrees (included angle with the vertical direction), smooth transition is preferably adopted at the joint of the bottom reducing section 2 and the conical distribution plate 10, so that part of the gasifying agent can smoothly adhere to the side wall of the bottom reducing section 2 and enter the edge area of the middle straight pipe section 4, and therefore, no dead zone is generated at the edge of the dense phase bed layer by the gasifying agent, and good fluidization effect in the middle straight pipe section 4 is ensured; the middle straight pipe section 4 is a vertically extending straight tubular structure, and the dense phase bed layer is arranged in the middle straight pipe section 4. Wherein, the top end of the middle straight pipe section 4 can be directly connected with the top necking section 5, and a reducing area and an expanding section with larger diameter can also be added; the diameter of the top necking section 5 is gradually reduced from bottom to top, and a crude gas outlet 51 is formed at the top end of the top necking section 5.

Wherein, the bottom opening of the conical distribution plate 10 is penetrated with a central jet pipe 12, the central jet pipe 12 is used for injecting a gasification agent into the gasification furnace, and the central jet pipe 12 and the horizontal air inlet jointly form the gasification agent inlet. An annular ash outlet 11 is formed between the central jet pipe 12 and the bottom opening of the conical distribution plate 10, and the top end of the central jet pipe 12 is higher than the ash outlet 11. The high-speed jet flow ejected by the central jet flow pipe 12 can strengthen the gas-solid contact between the gasification agent and the solid material in the dense-phase bed layer on one hand, and can form a negative pressure zone around the jet flow on the other hand, so that the coal dust particles carried in the falling ash are sucked and separated out and blown back to the dense-phase bed layer, and the ash particles with larger inertia continuously fall to the vicinity of the ash outlet 11 at the lower part.

In a further embodiment, the horizontal air inlet holes are higher than the top end of the central jet pipe 12. Therefore, on one hand, a certain ash buffer area can be formed, and the ash is prevented from forming an air seal on the pipe orifice of the central jet pipe 12 and causing adverse effects on the ash discharging of the ash outlet 11; on the other hand, the gasification agent entering from the horizontal air inlet hole can not interfere the air inlet of the central jet pipe 12, so that the negative pressure area formed by the high-speed jet of the gasification agent can be strengthened, more particle powder is sucked into the negative pressure area, and the gas-solid contact and slag-powder separation effects are strengthened.

In some embodiments, the syngas return tubes 6 are higher than the maximum jet height of the central jet tube 12, which is about 0.5-1m, to avoid erosive wear of the syngas return tubes 6 by the gasification agent jet ejected from the central jet tube 12.

Furthermore, a set interval is arranged between the bottom of the first-stage synthesis gas inlet cavity 71 and the bottom of the dense-phase bed layer, and the synthesis gas return furnace tube 6 penetrates into the gasification furnace along the bottom area of the dense-phase bed layer and is communicated with the first-stage synthesis gas inlet cavity 71, namely, the synthesis gas return furnace tube 6 penetrates into the gasification furnace from the joint 3 between the middle straight tube section 4 and the bottom reducer section 2, penetrates into the central position of the gasification furnace, extends upwards and is communicated with the first-stage synthesis gas inlet cavity 71. Because the gasifying agent contains oxygen, if the oxygen is directly contacted with the synthesis gas, detonation can occur, and the heat released by combustion forms local high temperature, so that the bed material is melted and slagged. In the embodiment, by setting the interval, the oxygen in the gasifying agent can be consumed by reaction when the gasifying agent passes through the interval, and then the gasifying agent is contacted with the synthesis gas above the gasifying agent, so that the phenomena of detonation and slagging are avoided.

It is noted that, in this document, relational terms such as "first" and "second," and the like, may be used solely to distinguish one entity or action from another entity or action without necessarily requiring or implying any actual such relationship or order between such entities or actions. Also, the terms "comprises," "comprising," or any other variation thereof, are intended to cover a non-exclusive inclusion, such that a process, method, article, or apparatus that comprises a list of elements does not include only those elements but may include other elements not expressly listed or inherent to such process, method, article, or apparatus. Without further limitation, an element defined by the phrase "comprising an … …" does not exclude the presence of other identical elements in a process, method, article, or apparatus that comprises the element.

The foregoing are merely exemplary embodiments of the present disclosure, which enable those skilled in the art to understand or practice the present disclosure. Various modifications to these embodiments will be readily apparent to those skilled in the art, and the generic principles defined herein may be applied to other embodiments without departing from the spirit or scope of the disclosure. Thus, the present disclosure is not intended to be limited to the embodiments shown herein but is to be accorded the widest scope consistent with the principles and novel features disclosed herein.

Claims (10)

1. A coal catalytic gasification reactor is characterized by comprising a gasification furnace and a synthetic gas inlet system, wherein the top of the gasification furnace is provided with a crude gas outlet (51), and a dense bed layer is arranged in the gasification furnace; the synthetic gas entering system comprises a first-stage synthetic gas inlet cavity (71) and a synthetic gas return tube (6), the first-stage synthetic gas inlet cavity (71) is arranged at the lower part of the dense-phase bed layer, one end of the synthetic gas return tube (6) is communicated with the crude gas outlet (51), the other end of the synthetic gas return tube penetrates through the side wall of the gasification furnace and is communicated with the first-stage synthetic gas inlet cavity (71), and a plurality of first exhaust holes (73) are formed in the peripheral wall of the first-stage synthetic gas inlet cavity (71).

2. A coal catalytic gasification reactor according to claim 1, wherein the primary syngas inlet chamber (71) is externally sleeved with a secondary syngas inlet chamber (72), and the peripheral wall of the secondary syngas inlet chamber (72) is provided with a plurality of second exhaust holes (74).

3. A coal catalytic gasification reactor according to claim 2, characterized in that the first exhaust hole (73) is inclined to the circumferential direction of the primary syngas inlet chamber (71).

4. A coal catalytic gasification reactor according to claim 3, characterized in that the second exhaust hole (74) is inclined towards the circumference of the secondary syngas inlet chamber (72), and the inclination direction of the first exhaust hole (73) coincides with the inclination direction of the second exhaust hole (74).

5. A coal catalytic gasification reactor according to claim 2, characterized in that the outwardly extending space of the first exhaust aperture (73) is staggered from the second exhaust aperture (74); and/or the presence of a gas in the gas,

the aperture of the second exhaust hole (74) is larger than that of the first exhaust hole (73).

6. The coal catalytic gasification reactor according to claim 1, wherein the synthesis gas return tube (6) is provided with buffer balls (61).

7. The coal catalytic gasification reactor according to claim 1, wherein the gasification furnace comprises a conical distribution plate (10), a bottom reducing section (2), a middle straight pipe section (4) and a top necking section (5) which are sequentially connected from bottom to top; a plurality of horizontal air inlets are formed in the peripheral wall of the conical distribution plate (10), and are used for introducing gasification agents into the gasification furnace; a central jet pipe (12) penetrates through the bottom opening of the conical distribution plate (10), the central jet pipe (12) is used for injecting a gasification agent into the gasification furnace, and an annular ash outlet (11) is formed between the central jet pipe (12) and the bottom opening of the conical distribution plate (10); the diameter of the bottom diameter-variable section (2) is gradually increased from bottom to top; the dense-phase bed layer is arranged in the middle straight pipe section (4); the top end of the top necking section (5) forms the crude gas outlet (51).

8. A coal catalytic gasification reactor according to claim 7, characterized in that the top end of the central jet pipe (12) is higher than the ash outlet (11) and the horizontal air inlet holes are higher than the top end of the central jet pipe (12).

9. The coal catalytic gasification reactor according to claim 7, wherein the syngas recuperator tube (6) is higher than the maximum jet height of the central jet tube (12).

10. The coal catalytic gasification reactor according to any of claims 1 to 9, characterized in that the primary syngas inlet chamber (71) has a set spacing between its bottom and the bottom of the dense bed, and the syngas return tubes (6) penetrate into the gasification furnace along the bottom region of the dense bed and communicate with the primary syngas inlet chamber (71).

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