CN210140561U - Gasification reaction device - Google Patents
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- CN210140561U CN210140561U CN201920458771.3U CN201920458771U CN210140561U CN 210140561 U CN210140561 U CN 210140561U CN 201920458771 U CN201920458771 U CN 201920458771U CN 210140561 U CN210140561 U CN 210140561U
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Abstract
The utility model provides a gasification reaction device, the device includes: the device comprises an inner cylinder, an outer cylinder, a gasification nozzle, a discharge pipe and a reaction mechanism; the gasification nozzle sequentially penetrates through the top wall of the outer barrel and the top wall of the inner barrel and is arranged in the inner barrel and used for conveying coal dust, first hydrogen and oxygen into the inner barrel to perform primary hydrogenation pyrolysis reaction; the reaction mechanism is arranged in the inner cylinder and is used for enabling semicoke generated by the primary hydrogenation thermal decomposition reaction and second hydrogen in the primary hydrogenation thermal decomposition reaction to carry out semicoke hydrogenation reaction; the discharge pipe sequentially penetrates through the bottom wall of the outer cylinder and the bottom wall of the inner cylinder, and part of the discharge pipe is arranged in the inner cylinder. The utility model discloses in, through setting up reaction mechanism in the inner tube, prolonged the dwell time of semicoke in the inner tube, guaranteed the abundant reaction of semicoke and second hydrogen, improved the conversion rate of semicoke and methane gas's productivity, and then improved the holistic efficiency of coal hydrogasification reaction, improved holistic economic nature.
Description
Technical Field
The utility model relates to a coal gasification technical field particularly, relates to a gasification reaction device.
Background
The coal hydro-gasification reaction refers to a process of producing gas such as methane, carbon monoxide and the like, oil products with high added values and semicoke by a series of chemical reactions of coal under the environment of excessive hydrogen and high temperature and medium pressure. The reaction process can be divided into a primary hydrogenation thermal decomposition reaction and a secondary reaction, and specifically, the secondary reaction comprises the reactions of gas-phase product hydrocracking, polymerization, solid semicoke hydrogenation and the like. Wherein, the gas phase reaction speed in the first hydrogenation thermal decomposition reaction and the second reaction is relatively high, and the solid semicoke hydrogenation reaction in the second reaction is a slow reaction and needs a long reaction time to obtain a high conversion rate.
However, most of the existing coal hydro-gasification reactors are air-bed reactors, which belong to a plug flow reactor, the retention time of the semicoke and the gas product in the primary hydrogenation thermal decomposition reaction is the same in the reaction zone, and only the full reaction of the gas product can be ensured, but for the semicoke, the reaction time is short, the incomplete reaction is brought out of the reaction zone, so that the conversion rate of the semicoke is low, and the overall economy of the system is affected.
SUMMERY OF THE UTILITY MODEL
In view of this, the utility model provides a gasification reaction device aims at solving the problem that semicoke in the present coal hydrogasification reaction can't fully react because of the reaction time is short and leads to the conversion rate to be low.
The utility model provides a gasification reaction device, the device includes: the device comprises an inner cylinder, an outer cylinder, a gasification nozzle, a discharge pipe and a reaction mechanism; the gasification nozzle sequentially penetrates through the top wall of the outer barrel and the top wall of the inner barrel and is arranged in the inner barrel and used for conveying coal dust, first hydrogen and oxygen into the inner barrel to perform primary hydrogenation pyrolysis reaction; the reaction mechanism is arranged in the inner cylinder and is used for enabling semicoke generated by the primary hydrogenation thermal decomposition reaction and second hydrogen in the primary hydrogenation thermal decomposition reaction to carry out semicoke hydrogenation reaction; the discharge pipe sequentially penetrates through the bottom wall of the outer cylinder and the bottom wall of the inner cylinder, and part of the discharge pipe is arranged in the inner cylinder.
Furthermore, in the gasification reaction device, a first reaction zone and a second reaction zone which are communicated with each other are sequentially arranged in the inner cylinder from the top to the bottom; the reaction mechanism is arranged in the second reaction zone and used for conveying circulating gas with preset pressure and preset temperature into the second reaction zone, and the circulating gas drives the semicoke to circularly move between the side and the center of the second reaction zone to form a circulating flow field.
Further, in the gasification reaction apparatus, the circulating gas includes: and the third hydrogen drives the semicoke to move to form a circulating flow field, and the third hydrogen and the semicoke perform a secondary reaction and semicoke hydrogenation reaction.
Further, in the gasification reaction apparatus, the reaction mechanism includes: an overflow tube and a plurality of nozzles; wherein, the diameter of the inner cylinder corresponding to the first reaction zone is smaller than that corresponding to the second reaction zone; each nozzle is arranged at the bottom of the inner cylinder and used for inputting circular flow gas into the inner cylinder; the overflow pipe sets up in the inner tube, and the first end and the row of overflow pipe are linked together, and the second end of overflow pipe has the default distance for the free end and with the top in second reaction zone.
Further, in the gasification reaction apparatus, a ratio of a height of the overflow pipe to a height of the inner cylinder corresponding to the second reaction zone is greater than 2: 3, and the ratio of the diameter of the inner cylinder corresponding to the first reaction zone to the diameter of the overflow tube is greater than 2: 1.
further, in the gasification reaction apparatus, a ratio of a diameter of the inner cylinder corresponding to the second reaction zone to a diameter corresponding to the first reaction zone is greater than 2: 1.
further, in the gasification reaction apparatus, the inner cylinder includes, corresponding to the second reaction zone: the inner cylinder is provided with a preset included angle with the inner wall of the inner cylinder corresponding to the reducing section.
Further, in the gasification reaction device, the bottom of the inner cylinder is conical, the conical top end of the inner cylinder faces the bottom of the outer cylinder, and each nozzle is arranged close to the conical bottom end of the inner cylinder.
Further, in the gasification reaction apparatus, the reaction mechanism further includes: a shell and a gas pipe; the shell is arranged between the inner cylinder and the outer cylinder and covers the bottom of the inner cylinder, the outer walls of the shell and the inner cylinder are enclosed into a cavity, and each nozzle is arranged in the cavity; the shell is provided with a gas inlet, the gas pipe penetrates through the outer barrel and is connected with the gas inlet, and the gas pipe is used for conveying circulating gas into the cavity; the cavity is used for conveying the circulating air to each nozzle after the circulating air is uniformly distributed.
Further, in the gasification reaction apparatus, the ratio of the height to the diameter of the inner cylinder corresponding to the first reaction zone is more than 3: 1.
further, the gasification reaction apparatus further includes: a coil pipe; the coil pipe is wound on the outer wall of the inner cylinder and corresponds to the second reaction area, and the first end of the coil pipe penetrates through the outer cylinder and is arranged outside the outer cylinder and used for receiving fourth hydrogen so as to exchange heat between the fourth hydrogen and the inner cylinder at the second reaction area; the second end of the coil pipe penetrates through the outer barrel and is communicated with the gasification nozzle, and the coil pipe is used for conveying the heat-exchanged fourth hydrogen to the gasification nozzle.
The utility model discloses in, through setting up reaction mechanism in the inner tube, make the semicoke that once hydrogenation thermal decomposition reaction produced continue to carry out semicoke hydrogenation reaction with the second hydrogen, the dwell time of semicoke in the inner tube has been prolonged, the abundant reaction of semicoke and second hydrogen has been guaranteed, the conversion rate of semicoke and methane gas's productivity have been improved, the semicoke among the current coal hydrogasification reaction has been solved and has leaded to the problem that the conversion rate is low because of the short and unable abundant reaction of reaction time, and then the holistic efficiency of coal hydrogasification reaction has been improved, whole economic nature has been improved.
Drawings
Various other advantages and benefits will become apparent to those of ordinary skill in the art upon reading the following detailed description of the preferred embodiments. The drawings are only for purposes of illustrating the preferred embodiments and are not to be construed as limiting the invention. Also, like reference numerals are used to refer to like parts throughout the drawings. In the drawings:
FIG. 1 is a schematic structural diagram of a gasification reaction apparatus provided in an embodiment of the present invention;
fig. 2 is a schematic cross-sectional view taken along line a-a in fig. 1.
Detailed Description
Exemplary embodiments of the present disclosure will be described in more detail below with reference to the accompanying drawings. While exemplary embodiments of the present disclosure are shown in the drawings, it should be understood that the present disclosure may be embodied in various forms and should not be limited to the embodiments set forth herein. Rather, these embodiments are provided so that this disclosure will be thorough and complete, and will fully convey the scope of the disclosure to those skilled in the art. It should be noted that, in the present invention, the embodiments and features of the embodiments may be combined with each other without conflict. The present invention will be described in detail below with reference to the accompanying drawings in conjunction with embodiments.
Referring to fig. 1, fig. 1 is a schematic structural diagram of a gasification reaction apparatus according to an embodiment of the present invention. As shown in the figure, the gasification reaction device is used for carrying out coal hydro-gasification reaction, and comprises: an inner cylinder 1, an outer cylinder 2, a gasification nozzle 3, a discharge pipe and a reaction mechanism. Wherein, the inner cylinder 1 is arranged inside the outer cylinder 2, and the vertical axis of the inner cylinder 1 coincides with the vertical axis of the outer cylinder 2. The gasification nozzle 3 sequentially penetrates through the top wall of the outer barrel 2 and the top wall of the inner barrel 1 and is arranged in the inner barrel 1, the gasification nozzle 3 is used for conveying coal dust, first hydrogen and oxygen into the inner barrel 1, and the coal dust, the first hydrogen and the oxygen carry out primary hydrogenation thermal decomposition reaction in the inner barrel 1 to generate gas, oil and semicoke. Specifically, one end of the gasification nozzle 3 is disposed outside the outer cylinder 2, and the other end is disposed inside the inner cylinder 1.
The reaction mechanism is arranged in the inner cylinder 1 and is used for enabling semicoke generated by the primary hydrogenation thermal decomposition reaction and second hydrogen in the primary hydrogenation thermal decomposition reaction to carry out semicoke hydrogenation reaction. Wherein, the second hydrogen may be the excess first hydrogen delivered by the gasification nozzle 3, and may also include: excess first hydrogen gas and hydrogen gas produced in the primary hydrogenation thermal decomposition reaction. The semicoke and the second hydrogen are subjected to semicoke hydrogenation reaction to generate methane gas and the like.
The discharging pipe sequentially penetrates through the bottom wall of the outer cylinder 2 and the bottom wall of the inner cylinder 1 and is partially arranged in the inner cylinder 1, specifically, one end of the discharging pipe is arranged in the inner cylinder 1, the other end of the discharging pipe is arranged outside the outer cylinder 2, and the discharging pipe is used for receiving reaction products generated by a primary hydrogenation thermal decomposition reaction and a semicoke hydrogenation reaction and discharging the reaction products. Wherein the reaction product comprises: gas, oil, semicoke, and methane gas.
It can be seen that, in this embodiment, the reaction mechanism is arranged in the inner cylinder 1, so that the semicoke generated by the primary hydrogenation thermal decomposition reaction continues to perform the semicoke hydrogenation reaction with the second hydrogen, the retention time of the semicoke in the inner cylinder 1 is prolonged, the sufficient reaction of the semicoke and the second hydrogen is ensured, the conversion rate of the semicoke and the yield of methane gas are improved, the problem that the conversion rate is low due to the insufficient reaction of the semicoke in the existing coal hydro-gasification reaction because of short reaction time is solved, the overall efficiency of the coal hydro-gasification reaction is improved, and the overall economy is improved.
With continued reference to fig. 1, in the above embodiment, the inner cylinder 1 is provided with a first reaction zone 4 and a second reaction zone 5 in sequence from the top to the bottom (from the top to the bottom as shown in fig. 1), and the first reaction zone 4 is communicated with the second reaction zone 5. The first reaction zone 4 is located at the upper part of the inner cylinder 1, and the second reaction zone 5 is located at the lower part of the inner cylinder 1.
The reaction mechanism is arranged in the second reaction zone 5, so that the first hydrogenation thermal decomposition reaction is carried out in the first reaction zone 4, and the semicoke hydrogenation reaction of the semicoke and the second hydrogen is carried out in the second reaction zone 5. The reaction mechanism is used for conveying circulation gas with preset pressure and preset temperature into the second reaction zone 5, and the circulation gas drives the semicoke to circularly move between the side and the center of the second reaction zone 5 so as to form a circulation flow field. Specifically, circulating gas with a preset pressure is conveyed into the inner cylinder 1, the circulating gas moves under the action of pressure difference to drive the semicoke to move together, and the movement locus of the circulating gas moves from the side of the second reaction area to the center of the second reaction area and then moves from the center of the second reaction area to the side of the second reaction area, so that a circulating flow field in circulating motion is formed. Thus, the first reaction zone 4 is a plug flow reaction zone and the second reaction zone 5 is a loop reaction zone.
Because the temperature of the product in the first reaction zone 4 is high, after the circulating gas is mixed with the product in the first reaction zone 4, the preset temperature of the circulating gas can adjust the temperature of the second reaction zone 5 to ensure the reaction temperature of the semicoke hydrogenation reaction, thereby avoiding deep cracking of oil products generated by the primary hydrogenation thermal decomposition reaction in the first reaction zone 4. In specific implementation, both the preset pressure and the preset temperature can be determined according to actual conditions, and this embodiment does not limit this.
In specific implementation, the reaction temperature of the first reaction zone 4 is 900-.
Preferably, the circulating gas comprises: a third hydrogen gas. The third hydrogen drives the semicoke to move to form a circulating flow field, and the third hydrogen and the semicoke perform semicoke hydrogenation reaction. Like this, can make semicoke and second hydrogen and third hydrogen carry out the abundant reaction, guarantee the abundant reaction of semicoke, improve the conversion rate of semicoke greatly.
It can be seen that, in the embodiment, the reaction mechanism drives the semicoke to move to form the circulation flow field by the flow of the circulation gas, so that the semicoke circulates in the second reaction zone 5, the retention time of the semicoke in the inner cylinder 1 is greatly prolonged, the sufficient reaction of the semicoke and the second hydrogen is ensured, the conversion rate of the semicoke is improved, the preset temperature of the circulation gas can ensure the reaction temperature of the hydrogenation reaction of the semicoke, the secondary cracking of oil products generated by the primary hydrogenation thermal decomposition reaction is effectively reduced, and the preset pressure of the circulation gas can drive the semicoke to move to form the circulation flow field.
Referring to fig. 1 and 2, in the above embodiment, the reaction mechanism may include: an overflow pipe 7 and a plurality of nozzles 6. The diameter D1 of the inner cylinder 1 corresponding to the first reaction zone 4 is smaller than the diameter D3 of the inner cylinder 1 corresponding to the second reaction zone 5, so that the semi-coke is driven by the circulating gas to form a circulating flow field in the second reaction zone 5. Preferably, the ratio of the diameter D3 of the inner cylinder 1 corresponding to the second reaction zone 5 to the diameter D1 of the inner cylinder 1 corresponding to the first reaction zone 4 is greater than 2: 1, the circulation gas can change the flow direction in the second reaction area 5 better, and then a circulation flow field is formed.
More preferably, the inner cylinder 1 comprises, in correspondence with the second reaction zone 5: a reducer section 12 and a main body section 13. The reducer section 12 and the main body section 13 communicate with each other, and the reducer section 12 communicates with the first reaction zone 4. Since the diameter of the inner cylinder 1 corresponding to the first reaction zone 4 is smaller than the diameter of the inner cylinder 1 corresponding to the second reaction zone 5, the diameter-changing section 12 enables the inner wall of the inner cylinder 1 to smoothly transit from the first reaction zone 4 to the second reaction zone 5, and the diameter of the inner cylinder 1 corresponding to the main body section 13 is the diameter D3 of the inner cylinder 1 corresponding to the second reaction zone 5. The inner wall of the inner cylinder 1 corresponding to the reducing section 12 and the inner wall of the inner cylinder 1 corresponding to the main body section 13 form a preset included angle. Preferably, the included angle is 120 ℃ to 150 ℃.
More preferably, the inner cylinder 1 is an arc-shaped section corresponding to the reducer section 12, so that the whole inner cylinder 1 is smooth in the flow field, and circulation flow of circulation gas and semicoke in the circulation flow field is facilitated.
Each nozzle 6 is arranged at the bottom of the inner cylinder 1, and each nozzle 6 is used for inputting circulation gas into the inner cylinder 1, so that the circulation gas drives the semicoke to move along the top of the second reaction zone 5 at the side of the second reaction zone 5 and then move from the center of the second reaction zone 5 to the bottom of the second reaction zone 5, thereby forming a circulation flow field. Specifically, each nozzle 6 corresponds to the bottom of the second reaction zone 5, i.e. each nozzle 6 is disposed at the bottom of the main section 13 of the second reaction zone 5, and the circulation gas input from each nozzle 6 is conveyed from the bottom of the second reaction zone 5 to the second reaction zone 5. A plurality of openings are formed in the bottom wall of the inner cylinder 1, each nozzle 6 corresponds to each opening one by one, each nozzle 6 penetrates through each opening one by one, the outlet end of each nozzle 6 is arranged in the inner cylinder 1, and more specifically, each nozzle 6 is attached to the inner wall of the inner cylinder 1 in the inner cylinder 1. The inlet end of each nozzle 6 is connected with a connecting pipe, each connecting pipe penetrates through the outer barrel 2 and is arranged outside the outer barrel 2, each connecting pipe is used for receiving the annular flow gas and conveying the annular flow gas to the corresponding nozzle 6, and each nozzle 6 conveys the annular flow gas into the inner barrel 1.
Preferably, each nozzle 6 is uniformly distributed along the bottom wall of the inner cylinder 1 in a circumferential shape, so that the circulating air delivered by each nozzle 6 can uniformly enter the inner cylinder 1, and a circulating flow field is conveniently formed.
Since the circulation gas has a predetermined pressure, the circulation gas ejected from each nozzle 6 has a certain velocity so as to form a circulation flow field. In specific implementation, the speed of the annular gas sprayed by each nozzle 6 is more than 15 m/s.
The overflow pipe 7 is arranged in the inner barrel 1, the first end (the lower end shown in figure 1) of the overflow pipe 7 is communicated with the discharge pipe, the second end (the upper end shown in figure 1) of the overflow pipe 7 is a free end, and the second end of the overflow pipe 7 has a preset distance with the top of the second reaction area 5. The overflow pipe 7 is used for conveying part of reaction products conveyed to the second reaction zone 5 from the first reaction zone 4 and reaction products generated by the semicoke hydrogenation reaction in the second reaction zone 5 to a discharge pipe. Specifically, the overflow pipe 7 is suspended in the inner cylinder 1, the overflow pipe 7 is disposed in the second reaction zone 5, and a first end of the overflow pipe 7 corresponds to a bottom of the second reaction zone 5 and a second end of the overflow pipe 7 extends toward a top of the second reaction zone 5. In specific implementation, the preset distance may be determined according to actual conditions, and this embodiment does not limit this. Preferably, the overflow pipe 7 and the discharge pipe are both arranged coaxially with the inner cylinder 1. More preferably, the overflow pipe 7 and the discharge pipe are integrally formed to form a pipe, which is convenient for processing and manufacturing.
In specific implementation, the motion track of the semicoke driven by the circulating air is as follows: the circulating gas is input from the bottom of the second reaction zone 5, the circulating gas drives the semicoke to move along the side of the second reaction zone 5 to the top of the second reaction zone 5, then the flow direction is changed at the top of the second reaction zone 5, the semi-coke reaches the center of the second reaction zone 5 from the side of the second reaction zone 5, namely reaches the overflow pipe 7, and then moves to the bottom of the second reaction zone 5 along the top of the center of the second reaction zone 5, namely moves from the top of the second reaction zone 5 to the bottom of the second reaction zone 5 along the pipe wall of the overflow pipe 7. And the semicoke circularly moves according to the movement track, so that a circular flow field is formed.
It can be seen that, in this embodiment, by controlling the diameter of the inner cylinder 1 corresponding to the first reaction zone 4 and the diameter corresponding to the second reaction zone 5, the circular gas moves upward from the bottom of the inner cylinder 1 and is blocked by the reducer section between the first reaction zone 4 and the second reaction zone 5, the flowing direction of the circular gas is changed, and the circular gas moves downward along the overflow pipe, so as to form a circular flow field, and the circular gas is ejected at a high speed through each nozzle 6, so that the circular gas flows in the inner cylinder 1 to drive the movement of the carbocoal, and meanwhile, the arrangement of the overflow pipe 7 can discharge the reaction product in the circular flow field and the product of the primary hydrogenation thermal decomposition reaction in the first reaction zone 4, and the structure is simple and convenient to implement.
With continued reference to fig. 1 and 2, in the above embodiment, in order to control the circulation rate of the circulating flow field, the ratio of the height L of the overflow tube 7 to the height of the inner cylinder 1 corresponding to the second reaction zone 5 is greater than 2: 3 and the ratio of the diameter D1 of the inner cylinder 1 corresponding to the first reaction zone 4 to the diameter D2 of the overflow pipe 7 is greater than 2: 1. specifically, the first end of the overflow pipe 7 corresponds to the bottom wall of the inner cylinder 1, and the discharge pipe is disposed between the bottom wall of the inner cylinder 1 and the bottom wall of the outer cylinder 2 and partially disposed outside the outer cylinder 2. When the overflow pipe 7 is integrally formed with the discharge pipe, the height L of the overflow pipe 7 merely means the height of the overflow pipe disposed in the inner cylinder 1. Therefore, the formation and circulation amount of a circulation flow field can be effectively controlled, the retention time of the semicoke in the inner cylinder 1 is prolonged, the semicoke and hydrogen are subjected to full semicoke hydrogenation reaction, and the conversion rate of the semicoke is improved.
With continued reference to fig. 1 and 2, in each of the above embodiments, the bottom of the inner cylinder 1 is tapered, the tapered top end (the lower end shown in fig. 1) of the inner cylinder 1 faces the bottom of the outer cylinder 2, and each of the nozzles 6 is disposed near the tapered bottom end (the upper end shown in fig. 1) of the inner cylinder 1. Specifically, the inner cylinder 1 further includes, corresponding to the second reaction zone 5: and the conical section 14 is communicated with the main body section 13, the conical section 14 corresponds to the bottom of the second reaction zone 5, the conical top end of the conical section 14 faces the bottom of the outer barrel 2, the conical bottom end of the conical section 14 is communicated with the main body section 13, and each nozzle 6 is arranged on the conical section 14 and is close to the main body section 13.
With continued reference to fig. 1 and 2, in each of the above embodiments, the reaction mechanism may further include: a housing 8 and a gas pipe 9. The shell 8 is arranged between the inner cylinder 1 and the outer cylinder 2, the shell 8 is covered at the bottom of the inner cylinder 1, and the shell 8 and the outer wall of the inner cylinder 1 are enclosed to form a cavity 11. Specifically, the housing 8 is disposed outside the bottom of the inner cylinder 1 and inside the outer cylinder 2, the housing 8 corresponding to the bottom of the second reaction zone 5. The housing 8 is a closed structure, and the housing 8 and the outer wall of the inner cylinder 1 enclose an annular cavity 11. More specifically, the housing 8 corresponds to the junction of the main section 13 and the tapered section 14 of the inner barrel 1, and is disposed at the bottom of the main section 13 and partially in the tapered section 14.
Each nozzle 6 is arranged in the cavity 11, that is, each nozzle 6 is arranged in the cavity 11 at the bottom of the inner cylinder 1.
The casing 8 is provided with a gas inlet, the gas pipe 9 penetrates through the outer barrel 2 and is connected with the gas inlet, and the gas pipe 9 is used for conveying circulating gas into the cavity 11. The cavity 11 is used for uniformly distributing circulating air and then conveying the circulating air to each nozzle 6. Specifically, a first end of the gas pipe 9 is disposed outside the outer cylinder 2, and a second end of the gas pipe 9 is disposed inside the outer cylinder 2 and connected to the gas inlet of the housing 8.
It can be seen that, in the embodiment, the circulation gas with the preset pressure is uniformly distributed in the cavity 11 surrounded by the outer walls of the shell 8 and the inner cylinder 1 by using the pressure difference, and then the uniformly distributed circulation gas is conveyed into the inner cylinder 1 through each nozzle 6, so that the semicoke can be effectively driven to move, and the circulation flow field can be conveniently formed.
Referring to fig. 1, in the above embodiments, the ratio of the height to the diameter of the inner cylinder 1 corresponding to the first reaction zone 4 is greater than 3: 1. therefore, the semi-coke can be output in a plug flow mode in the first reaction zone 4, and the semi-coke can be conveyed from the first reaction zone 4 to the second reaction zone 5 at a preset speed, so that a circulating flow field is formed under the driving of circulating gas.
With continued reference to fig. 1, in the above embodiments, the gasification reaction apparatus may further include: a coil 10. Wherein, the coil pipe 10 is arranged between the outer cylinder 2 and the inner cylinder 1, the coil pipe 10 is wound on the outer wall of the inner cylinder 1, and the coil pipe 10 corresponds to the second reaction zone 5. The first end of the coil 10 penetrates through the outer cylinder 2, the first end of the coil 10 is arranged outside the outer cylinder 2, and the first end of the coil 10 is used for receiving fourth hydrogen so that the fourth hydrogen exchanges heat with the inner cylinder 1 at the second reaction area 5. The second end of the coil 10 is inserted into the outer cylinder 2, the second end of the coil 10 is arranged outside the outer cylinder 2 and is communicated with the gasification nozzle 3, and the second end of the coil 10 is used for conveying the heat-exchanged fourth hydrogen to the gasification nozzle 3.
In practice, the first end of the coil 10 is near the bottom of the second reaction zone 5 and the second end of the coil 10 is near the top of the second reaction zone 5.
It can be seen that, in this embodiment, the coil pipe 10 exchanges heat with the fourth hydrogen and the inner cylinder 1 in the second reaction area 5, so that not only is the reaction temperature of the semicoke hydrogenation ensured, deep cracking of an oil product generated in the first reaction area 4 avoided, but also the fourth hydrogen can be heated, the heated fourth hydrogen is conveyed to the first reaction area 4 through the gasification nozzle 3, the reaction temperature of the primary hydrogenation thermal decomposition reaction in the first reaction area 4 is ensured, and the energy utilization rate is improved.
The specific operation of the gasification reaction apparatus is described with reference to fig. 1 and 2: the first hydrogen is heated to a certain temperature and then is conveyed to the gasification nozzle 3, oxygen and the first hydrogen are subjected to oxygen-deficient combustion, the temperature of the first hydrogen is raised to be more than 1100 ℃, and then the first hydrogen and the pulverized coal are mixed at the outlet of the gasification nozzle 3, and the pulverized coal is rapidly heated and heated. The reaction temperature of the first reaction zone 4 is controlled at 900-1000 ℃ by controlling the oxygen amount. In the first reaction zone 4, the coal powder and the first hydrogen gas are subjected to primary hydrogenation thermal decomposition reaction to generate gas, oil products and semicoke. Because the temperature of the first reaction zone 4 is higher, the high temperature can cause the excessive cracking of the reaction product, especially the cracking of oil products, and the yield of the oil products with high added values is reduced, so the retention time of the reaction product in the first reaction zone 4 is shorter, namely 3-10 seconds. Then, the gas, oil and semicoke generated by the primary hydrogenation thermal decomposition reaction enter the second reaction zone 5.
In the second reaction zone 5, circulating gas with preset pressure and preset temperature is conveyed into the cavity 11 through the gas conveying pipe 9, and the circulating gas is uniformly distributed in the cavity 11 and then is sprayed into the inner barrel 1 at a high speed through each nozzle 6. In the second reaction zone 5, the temperature of the second reaction zone 5 is controlled to be 700-. Meanwhile, the circulating gas flows in the inner cylinder 1 by depending on the speed sprayed by each nozzle 6, so that the gas, the oil and the semicoke are driven to move together, and a circulating flow field is formed. In the circulation process, semicoke and second hydrogen carry out semicoke hydrogenation reaction, and when the circulation gas comprises third hydrogen, semicoke not only carries out semicoke hydrogenation reaction with second hydrogen, also carries out semicoke hydrogenation reaction with third hydrogen, has guaranteed the abundant reaction of semicoke, and this semicoke hydrogenation reaction generates methane gas and other products.
In the process of conveying the reaction products in the first reaction zone 4 to the second reaction zone 5, as the diameter difference exists between the diameter of the inner cylinder 1 corresponding to the first reaction zone 4 and the diameter of the overflow pipe 7, most of the reaction products generated by the primary hydrogenation thermal decomposition reaction are carried by the circulating gas to enter the circulating flow field for circulation, and the other part of the reaction products enter the overflow pipe 7. In the second reaction zone 5, following performance of the semicoke is enhanced along with the progress of the semicoke hydrogenation reaction, the semicoke is carried into the overflow pipe 7 by gas, and other products of the semicoke hydrogenation reaction in the circulation flow field also enter the overflow pipe 7, namely the overflow pipe 7 conveys reaction products generated in the primary hydrogenation thermal decomposition reaction and the semicoke hydrogenation reaction to the discharge pipe and then conveys the reaction products out through the discharge pipe.
And the fourth hydrogen is conveyed into the coil pipe 10, the fourth hydrogen exchanges heat with the inner cylinder 1 corresponding to the second reaction zone 5 in the coil pipe 10, so that the temperature of the fourth hydrogen is increased, and the increased fourth hydrogen can be conveyed to the gasification nozzle 3 as the first hydrogen and further conveyed into the inner cylinder 1.
In summary, in the embodiment, the reaction mechanism is arranged in the inner cylinder 1, so that the semicoke generated by the primary hydrogenation thermal decomposition reaction continues to perform the semicoke hydrogenation reaction with the second hydrogen, the retention time of the semicoke in the inner cylinder 1 is prolonged, the sufficient reaction of the semicoke and the second hydrogen is ensured, the conversion rate of the semicoke and the yield of methane gas are improved, the overall efficiency of the coal hydro-gasification reaction is improved, and the overall economy is improved.
It will be apparent to those skilled in the art that various changes and modifications may be made without departing from the spirit and scope of the invention. Thus, if such modifications and variations of the present invention fall within the scope of the claims and their equivalents, the present invention is also intended to include such modifications and variations.
Claims (11)
1. A gasification reaction apparatus, comprising: the device comprises an inner cylinder (1), an outer cylinder (2), a gasification nozzle (3), a discharge pipe and a reaction mechanism; wherein the content of the first and second substances,
the inner cylinder (1) is arranged in the outer cylinder (2), and the gasification nozzle (3) sequentially penetrates through the top wall of the outer cylinder (2) and the top wall of the inner cylinder (1) and is arranged in the inner cylinder (1) and used for conveying coal dust, first hydrogen and oxygen into the inner cylinder (1) to perform primary hydrogenation pyrolysis reaction;
the reaction mechanism is arranged in the inner cylinder (1) and is used for enabling semicoke generated by the primary hydrogenation thermal decomposition reaction and second hydrogen in the primary hydrogenation thermal decomposition reaction to carry out semicoke hydrogenation reaction;
the discharge pipe sequentially penetrates through the bottom wall of the outer cylinder (2) and the bottom wall of the inner cylinder (1), and part of the discharge pipe is arranged in the inner cylinder (1).
2. The gasification reaction apparatus according to claim 1,
a first reaction zone (4) and a second reaction zone (5) which are communicated with each other are sequentially arranged in the inner cylinder (1) from the top to the bottom;
the reaction mechanism is arranged in the second reaction area (5) and used for conveying circulating gas with preset pressure and preset temperature into the second reaction area (5), and the circulating gas drives the semicoke to circularly move between the side and the center of the second reaction area (5) to form a circulating flow field.
3. The gasification reaction apparatus of claim 2, wherein the circulation gas comprises: and the third hydrogen drives the semicoke to move to form the circulating flow field, and the third hydrogen and the semicoke perform semicoke hydrogenation reaction.
4. A gasification reaction apparatus according to claim 2 or 3 wherein the reaction mechanism comprises: an overflow pipe (7) and a plurality of nozzles (6); wherein the content of the first and second substances,
the diameter of the inner cylinder (1) corresponding to the first reaction zone (4) is smaller than the diameter corresponding to the second reaction zone (5);
each nozzle (6) is arranged at the bottom of the inner cylinder (1) and is used for inputting the circulating gas into the inner cylinder (1);
overflow pipe (7) set up in inner tube (1), the first end of overflow pipe (7) with it is linked together to arrange the material pipe, the second end of overflow pipe (7) be the free end and with the top of second reaction zone (5) has the distance of predetermineeing.
5. A gasification reaction device according to claim 4, wherein the ratio of the height of the overflow pipe (7) to the height of the inner drum (1) corresponding to the second reaction zone (5) is greater than 2: 3 and the ratio of the diameter of the inner cylinder (1) corresponding to the first reaction zone (4) to the diameter of the overflow pipe (7) is greater than 2: 1.
6. a gasification reaction apparatus according to claim 4 wherein the ratio of the diameter of the inner barrel (1) corresponding to the second reaction zone (5) to the diameter corresponding to the first reaction zone (4) is greater than 2: 1.
7. a gasification reaction device in accordance with claim 4, wherein the inner tube (1) comprises, in correspondence with the second reaction zone (5): the variable-diameter section (12) and the main body section (13) are communicated with each other, the variable-diameter section (12) is communicated with the first reaction zone (4), and a preset included angle is formed between the inner wall of the inner cylinder (1) corresponding to the variable-diameter section (12) and the inner wall of the inner cylinder (1) corresponding to the main body section (13).
8. A gasification reaction apparatus according to claim 4, wherein the bottom of the inner tube (1) is tapered, the top of the inner tube (1) is directed to the bottom of the outer tube (2), and each of the nozzles (6) is disposed near the bottom of the inner tube (1).
9. The gasification reaction apparatus of claim 4 wherein the reaction mechanism further comprises: a shell (8) and a gas pipe (9); wherein the content of the first and second substances,
the shell (8) is arranged between the inner cylinder (1) and the outer cylinder (2) and covers the bottom of the inner cylinder (1), a cavity (11) is formed by enclosing the outer walls of the shell (8) and the inner cylinder (1), and each nozzle (6) is arranged in the cavity (11);
the shell (8) is provided with a gas inlet, the gas pipe (9) penetrates through the outer barrel (2) and is connected with the gas inlet, and the gas pipe (9) is used for conveying the circulating gas into the cavity (11);
the cavity (11) is used for enabling the circulating air to be uniformly distributed and then conveyed to the nozzles (6).
10. A gasification reaction apparatus according to claim 2 wherein the inner barrel (1) has a height to diameter ratio corresponding to the first reaction zone (4) of greater than 3: 1.
11. the gasification reaction apparatus of claim 2, further comprising: a coil (10); wherein the content of the first and second substances,
the coil pipe (10) is wound on the outer wall of the inner cylinder (1) and corresponds to the second reaction zone (5), and a first end of the coil pipe (10) penetrates through the outer cylinder (2) and is arranged outside the outer cylinder (2) and used for receiving fourth hydrogen so as to exchange heat between the fourth hydrogen and the inner cylinder (1) at the second reaction zone (5);
the second end of the coil pipe (10) penetrates through the outer cylinder (2) and is communicated with the gasification nozzle (3) for conveying the heat-exchanged fourth hydrogen to the gasification nozzle (3).
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| CN112251260A (en) * | 2020-11-05 | 2021-01-22 | 北京一亚高科能源科技有限公司 | Overhead feeding TFB gasification furnace |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN112251260A (en) * | 2020-11-05 | 2021-01-22 | 北京一亚高科能源科技有限公司 | Overhead feeding TFB gasification furnace |
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