CN110982559B - Uniform feeding type circulating fluidized bed reactor - Google Patents
Uniform feeding type circulating fluidized bed reactor Download PDFInfo
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- CN110982559B CN110982559B CN201911351296.0A CN201911351296A CN110982559B CN 110982559 B CN110982559 B CN 110982559B CN 201911351296 A CN201911351296 A CN 201911351296A CN 110982559 B CN110982559 B CN 110982559B
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- 238000006243 chemical reaction Methods 0.000 claims abstract description 53
- 238000009826 distribution Methods 0.000 claims abstract description 10
- 238000007599 discharging Methods 0.000 claims abstract description 6
- 239000000463 material Substances 0.000 claims description 12
- 238000009423 ventilation Methods 0.000 claims description 6
- 230000008901 benefit Effects 0.000 claims description 5
- 230000008676 import Effects 0.000 claims description 3
- 230000000149 penetrating effect Effects 0.000 claims description 3
- 230000001737 promoting effect Effects 0.000 claims description 2
- 239000002245 particle Substances 0.000 abstract description 23
- 239000007787 solid Substances 0.000 abstract description 6
- 238000002309 gasification Methods 0.000 description 10
- 239000008187 granular material Substances 0.000 description 8
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 7
- 239000003245 coal Substances 0.000 description 7
- 229910052799 carbon Inorganic materials 0.000 description 6
- 238000005516 engineering process Methods 0.000 description 5
- 238000005243 fluidization Methods 0.000 description 3
- 239000007789 gas Substances 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000002485 combustion reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000012071 phase Substances 0.000 description 2
- XURIQWBLYMJSLS-UHFFFAOYSA-N 1,4,7,10-tetrazacyclododecan-2-one Chemical compound O=C1CNCCNCCNCCN1 XURIQWBLYMJSLS-UHFFFAOYSA-N 0.000 description 1
- 239000002028 Biomass Substances 0.000 description 1
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000005266 casting Methods 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000003034 coal gas Substances 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000002737 fuel gas Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005272 metallurgy Methods 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000012216 screening Methods 0.000 description 1
- 239000007790 solid phase Substances 0.000 description 1
- 239000002910 solid waste Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000003786 synthesis reaction Methods 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
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Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
- B04C—APPARATUS USING FREE VORTEX FLOW, e.g. CYCLONES
- B04C9/00—Combinations with other devices, e.g. fans, expansion chambers, diffusors, water locks
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/093—Coal
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Organic Chemistry (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The invention relates to an even feeding type circulating fluidized bed reactor, which comprises a hearth, a guide cylinder, a cyclone separator, a companion bed, a discharge pipe, a downcomer and a return pipe, wherein the inside of the hearth is divided into an air inlet chamber and a reaction chamber by an air distribution plate; the guide shell is in a conical shape and is arranged at the lower end of the reaction chamber, the lower port of the guide shell is positioned right above the lifting air conveying pipe, the upper end inlet of the guide shell is connected with the input port of the cyclone separator through the discharging pipe, the lower end outlet of the cyclone separator is connected with the accompanying bed, the accompanying bed is connected with the descending pipe, the descending pipe is connected with one end of the return pipe, and the other end of the return pipe is connected with the lower end of the reaction chamber. According to the invention, the central pipe and the guide cylinder are additionally arranged in the hearth, so that solid particles on the inner section of the bed are more uniformly mixed, the gas-solid two-phase contact time is longer, and the stable operation can be realized.
Description
The technical field is as follows:
the invention relates to a uniform feeding type circulating fluidized bed reactor.
Background art:
the circulating fluidized bed technology is an efficient and clean technology, has wide application range, and can treat high-quality coal, inferior coal, solid waste, biomass and other fuels. Among them, coal gasification is one of the industrially important uses of circulating fluidized beds, mainly for the conversion of coal into H2CO and CH4And the like, and is widely used as fuel gas in the fields of metallurgy, synthesis and the like at present.
According to the state of solid motion in the bed, the coal gasification technology can be divided into three types, namely fixed bed gasification, entrained flow gasification and fluidized bed gasification. The fluidized bed has the advantages of low raw material cost, small environmental pollution, high gasification efficiency and the like, and the fluidized bed technology can treat coal blocks with wider particle size, does not need screening, can gasify the coal blocks by using air, and has low processing cost, strong applicability and high combustion efficiency, thereby being widely applied.
However, in the traditional fluidized bed gasification technology, the particles are not uniformly mixed, the retention time is short, and the carbon content of the ash is high due to insufficient reaction. Today, most fluidized bed gasification has a carbon conversion of only 65% to 85%, making it inefficient to use a portion of the carbon residue present in the ash. On one hand, the carbon conversion rate of the fluidized bed reactor is reduced, so that the coal gas yield and the system thermal efficiency are reduced; on the other hand, the carbon content in the ash is high, the combustion and gasification activity is low, and the direct application is not beneficial.
The invention content is as follows:
the invention aims at solving the problems in the prior art, namely the invention aims to provide a uniform feeding type circulating fluidized bed reactor, so that solid particles on the inner section of the bed are mixed more uniformly, and the contact time of gas phase and solid phase is longer.
In order to achieve the purpose, the invention adopts the technical scheme that: a uniform feeding type circulating fluidized bed reactor comprises a hearth, a guide cylinder, a cyclone separator, a companion bed, a discharge pipe, a downcomer and a return pipe, wherein the inside of the hearth is divided into an air inlet chamber and a reaction chamber which are communicated through an air distribution plate, a lifting air conveying pipe for conveying lifting air towards the interior of the reaction chamber is vertically arranged in the middle of the air inlet chamber in a penetrating manner, and a fluidizing air inlet is formed in the side wall of the air inlet chamber; the utility model discloses a reaction chamber, including draft tube, cyclone, companion bed, downcomer, reaction chamber, guide tube is the toper form and locates the lower extreme of reaction chamber, and the lower port of guide tube is located and promotes the wind conveyer pipe directly over, and the upper end import of guide tube is connected with cyclone's input port via the discharging pipe, cyclone's lower extreme exit linkage companion bed, companion bed and downcomer are connected, the downcomer is connected with the one end of returning charge pipe, the other end of returning charge pipe is connected with reaction chamber's lower extreme.
Further, the discharging pipe comprises a central pipe and a lifting pipe, the central pipe is vertically arranged on the upper side of the guide cylinder, the lower end of the central pipe is connected with the upper port of the guide cylinder, the upper end of the central pipe extends out of the reaction chamber and is connected with one end of the lifting pipe, and the other end of the lifting pipe is connected with the upper end inlet of the cyclone separator.
Further, the axes of the lifting air delivery pipe, the guide cylinder and the central pipe are coincident.
Further, the cross-sectional area of the lower end of the guide shell is larger than that of the central pipe.
Further, a plurality of ventilation holes that do benefit to gas along vertical passing are evenly distributed on the grid plate, the ventilation hole that lies in the middle part position on the upper end that promotes the wind conveyer pipe and the grid plate is connected.
Furthermore, the return pipe is in an inclined shape with a high upper end and a low lower end, the upper end of the return pipe is connected with the descending pipe, and the lower end of the return pipe is connected with the reaction chamber.
Furthermore, the lower end side wall of the reaction chamber is provided with a material returning hole used for being connected with a material returning pipe, and the material returning hole is positioned at the lower end side of the guide cylinder.
Furthermore, flow meters are arranged at the lower end of the lifting air conveying pipe and the position of the fluidized air conveying inlet.
Furthermore, the lower part of the cyclone separator is of a conical structure with a gradually reduced inner diameter, and an outlet at the lower end of the cyclone separator is connected with a vertical pipe which is connected with a companion bed.
Further, a first ball valve is mounted at the outlet of the lower end of the cyclone separator; and a second ball valve is arranged on the downcomer.
Compared with the prior art, the invention has the following effects: according to the invention, the guide cylinder is arranged in the reaction chamber of the hearth, and the fluidized air upwards passes through the gap between the guide cylinder and the side wall of the reaction chamber and forms countercurrent contact with the particles falling in the reaction chamber, so that the retention time of the particles in the reaction chamber is increased, the particles are more uniformly mixed, the materials can be fully oxidized, the full contact and reaction between the particles and a gasifying agent are realized, the gasification efficiency and the carbon conversion rate are improved, and the carbon content of ash residues in the hearth is reduced.
Description of the drawings:
FIG. 1 is a schematic configuration diagram of an embodiment of the present invention.
In the figure: 1-lifting air conveying pipe, 2-fluidizing air inlet, 3-air distribution plate, 4-hearth, 5-guide cylinder, 6-central pipe, 7-lifting pipe, 8-cyclone separator, 9-first ball valve, 10-accompanying bed, 11-accompanying bed air inlet, 12-descending pipe, 13-second ball valve, 14-return pipe, 15-air inlet chamber, 16-reaction chamber and 17-return hole.
The specific implementation mode is as follows:
the present invention will be described in further detail with reference to the accompanying drawings and specific embodiments.
In the description of the present invention, it is to be understood that the terms "longitudinal", "lateral", "upper", "lower", "front", "rear", "left", "right", "vertical", "horizontal", "top", "bottom", "inner", "outer", and the like, indicate orientations or positional relationships based on those shown in the drawings, are merely for convenience of description of the present invention, and do not indicate or imply that the referenced devices or elements must have a particular orientation, be constructed and operated in a particular orientation, and thus, are not to be construed as limiting the present invention.
As shown in fig. 1, the uniform feeding type circulating fluidized bed reactor of the present invention comprises a furnace chamber 4, a draft tube 5, a cyclone separator 8, a companion bed 10, a discharge tube, a downcomer 12 and a return pipe 17, wherein the interior of the furnace chamber 4 is divided into an air inlet chamber 15 and a reaction chamber 16 which are communicated with each other by an air distribution plate 3 located at the lower end of the furnace chamber 4, a lift air conveying pipe 1 for conveying lift air into the reaction chamber 16 is vertically arranged in the middle of the air inlet chamber 15 in a penetrating manner, and a fluidizing air inlet 2 is arranged on the side wall of the air inlet chamber 15 for inputting fluidizing air; the draft tube 5 is in a conical shape and is arranged at the lower end of the reaction chamber 16, the lower port of the draft tube 5 is located right above the lifting air conveying pipe 1, the upper end inlet of the draft tube 5 is connected with the input port of the cyclone separator 8 through the discharge pipe, the lower end outlet of the cyclone separator 8 is connected with the accompanying bed 10, the accompanying bed 10 is connected with the descending pipe 12, the descending pipe 12 is connected with one end of the return pipe 14, and the other end of the return pipe 14 is connected with the lower end of the reaction chamber 16. When the device is used, particles are accumulated on the air distribution plate 3, fluidized air in the air inlet cavity 15 passes through the air distribution plate 3 and flows upwards, particles positioned on the outer side of the guide cylinder 5 are blown by the fluidized air and upwards pass through a gap (annular gap area) between the guide cylinder 5 and the side wall of the reaction cavity 16 and enter the upper part of the reaction cavity 16, and particles positioned under the guide cylinder 5 are blown upwards into the guide cylinder 5 by the fluidized air, and at the moment, the lifting air conveying pipe 1 conveys lifting air towards the guide cylinder 5, so that the lifting air can blow the particles in the guide cylinder 5 to enter the discharge pipe and finally enter the cyclone separator 8; the particles pass through the cyclone separator 8, the accompanying bed 10 and the down pipe 12 in sequence and then return to the lower end of the reaction chamber 16 from the return pipe 14, and the particles falling from the return pipe 14 are located at the edge of the wind distribution plate 3 (outside the guide cylinder 5), so that the particles can be blown upwards to the upper part of the reaction chamber 16 by the fluidizing wind. In the process, the fluidized wind passes through the gap between the guide shell 5 and the side wall of the reaction chamber 16 upwards and can form countercurrent contact with the particles in a falling state in the reaction chamber 16, so that the residence time of the particles in the reaction chamber 16 is prolonged, the mixing is more uniform, and the particles can be fully contacted and reacted.
In this embodiment, the discharging pipe includes center tube 6 and riser 7, center tube 3 is vertical to be set up at the upside of draft tube, and the lower extreme of center tube 6 is connected with the last port of draft tube 5, and the upper end of center tube 6 stretches out reaction chamber 16 and is connected with the one end of riser 7, the other end of riser 7 is connected with the upper end import of cyclone 8.
In this embodiment, the axes of the lifting wind delivery pipe 1, the guide cylinder 5 and the central pipe 6 are coincident, so that the lifting wind energy can quickly and efficiently lift particles to the cyclone separator.
In this embodiment, the cross-sectional area of the lower end of the guide shell 5 is larger than that of the central tube 6; the advantages of this structure are: firstly, the particles falling in the reaction chamber can be blocked to a certain extent, and secondly, the particles in the middle of the air distribution plate can be ensured to smoothly enter the central tube under the driving of the lifting air.
In the embodiment, in the actual production process, the guide shell 5 is processed into various tapers, wherein the taper is more than 0 degree and less than 90 degrees, and the corresponding taper can be selected as required; the diameter of the central tube 6 is also processed into various diameters, the diameters are selected according to requirements, and meanwhile the installation height of the central tube can be adjusted according to requirements.
In this embodiment, the equipartition is a plurality of in order to do benefit to the ventilation hole that fluidizing gas passed along vertical on the grid 3, the ventilation hole that lies in the middle part position on promoting wind conveyer pipe and the grid is connected.
In this embodiment, the return pipe 14 is inclined with a high upper end and a low lower end, the upper end of the return pipe 14 is connected to the downcomer 12, and the lower end of the return pipe 14 is connected to the reaction chamber 16.
In this embodiment, a material returning hole 17 for connecting with the material returning pipe 14 is formed in a side wall of a lower end of the reaction chamber 16, and the material returning hole 17 is located at a side of a lower end of the guide shell 5 and located at an upper side of the air distribution plate 3. Because the material returning hole is positioned at the side of the lower end of the guide cylinder, particles falling from the material returning pipe can be prevented from being lifted into the cyclone separator by the lifting air again.
In this embodiment, flowmeters are disposed at the lower end of the lifting air delivery pipe 1 and the fluidized air input port 2, so that the air input volume and the air input volume ratio can be controlled according to needs.
In this embodiment, the lower part of the cyclone separator 8 is in a conical structure with a gradually reduced inner diameter, and the outlet at the lower end of the cyclone separator 8 is connected with a vertical pipe which is connected with a companion bed.
In this embodiment, a first ball valve 9 is installed at the lower outlet of the cyclone separator 8; a second ball valve 13 is mounted on the downcomer 12.
In this embodiment, the bed trace 10 is provided with a bed trace wind input port 11.
Compare with traditional fluidized bed, the reaction chamber lower extreme of this embodiment in furnace sets up the draft tube of toper form and the center tube that is connected with the draft tube upper end, and the granule can only get into the reaction chamber upper end from the clearance (annular clearance district) between the lower extreme of draft tube and the reaction chamber lateral wall under the drive of fluidization wind to the order of getting into is: the granule that is located air distributor outward flange (draft tube outside) passes annular clearance district earlier, and remaining granule then gets into cyclone under the drive of lifting wind, pass through cyclone in proper order, the companion bed, the downcomer returns to in the reaction chamber behind downcomer and the return pipe, this part granule continues to pass annular clearance district upwards under the drive of fluidization wind, fluidization wind at this moment forms countercurrent contact with the granule that is in the whereabouts form in the reaction chamber, make the dwell time extension of granule in furnace, it is more even to mix, the granule can fully contact and react, consequently, good gas-solid contact has, the quick stirring ability of heat transfer efficiency and particle, can effectively solve granule mixing inequality in the traditional fluidized bed, gas-solid double-phase contact time is shorter, the insufficient problem of reaction.
If the invention discloses or relates to parts or structures which are fixedly connected to each other, the fixedly connected parts can be understood as follows, unless otherwise stated: a detachable fixed connection (for example using bolts or screws) is also understood as: non-detachable fixed connections (e.g. riveting, welding), but of course, fixed connections to each other may also be replaced by one-piece structures (e.g. manufactured integrally using a casting process) (unless it is obviously impossible to use an integral forming process).
In addition, terms used in any technical solutions disclosed in the present invention to indicate positional relationships or shapes include approximate, similar or approximate states or shapes unless otherwise stated.
Any part provided by the invention can be assembled by a plurality of independent components or can be manufactured by an integral forming process.
Finally, it should be noted that: the above examples are only intended to illustrate the technical solution of the present invention and not to limit it; although the present invention has been described in detail with reference to preferred embodiments, those skilled in the art will understand that: modifications to the specific embodiments of the invention or equivalent substitutions for parts of the technical features may be made; without departing from the spirit of the present invention, it is intended to cover all aspects of the invention as defined by the appended claims.
Claims (10)
1. The utility model provides an even feeding formula circulating fluidized bed reactor, includes furnace, cyclone, companion's bed and return pipe, its characterized in that: the furnace is characterized by also comprising a guide cylinder, a discharge pipe and a downcomer, wherein the interior of the furnace is divided into an air inlet chamber and a reaction chamber which are communicated through an air distribution plate, a lifting air conveying pipe for conveying lifting air towards the reaction chamber is vertically arranged in the middle of the air inlet chamber in a penetrating manner, and a fluidized air inlet is formed in the side wall of the air inlet chamber; the utility model discloses a reaction chamber, including draft tube, cyclone, companion bed, downcomer, reaction chamber, guide tube is the toper form and locates the lower extreme of reaction chamber, and the lower port of guide tube is located and promotes the wind conveyer pipe directly over, and the upper end import of guide tube is connected with cyclone's input port via the discharging pipe, cyclone's lower extreme exit linkage companion bed, companion bed and downcomer are connected, the downcomer is connected with the one end of returning charge pipe, the other end of returning charge pipe is connected with reaction chamber's lower extreme.
2. A homogeneous feed circulating fluidized bed reactor as set forth in claim 1 wherein: the discharging pipe comprises a central pipe and a lifting pipe, the central pipe is vertically arranged on the upper side of the guide cylinder, the lower end of the central pipe is connected with the upper port of the guide cylinder, the upper end of the central pipe extends out of the reaction chamber and is connected with one end of the lifting pipe, and the other end of the lifting pipe is connected with the upper end inlet of the cyclone separator.
3. A homogeneous feed circulating fluidized bed reactor according to claim 2, wherein: the axes of the lifting air conveying pipe, the guide cylinder and the central pipe are coincided.
4. A homogeneous feed circulating fluidized bed reactor according to claim 2, wherein: the cross-sectional area of the lower end of the guide shell is larger than that of the central pipe.
5. A homogeneous feed circulating fluidized bed reactor as set forth in claim 1 wherein: the last equipartition of grid plate is a plurality of in order to do benefit to the ventilation hole that gas passed along vertical, the ventilation hole that lies in the middle part position on promoting wind conveyer pipe and the grid plate is connected.
6. A homogeneous feed circulating fluidized bed reactor as set forth in claim 1 wherein: the upper end of the return pipe is connected with the descending pipe, and the lower end of the return pipe is connected with the reaction chamber.
7. A homogeneous feed circulating fluidized bed reactor according to claim 1 or 6, wherein: and a material returning hole used for being connected with a material returning pipe is formed in the side wall of the lower end of the reaction chamber, and the material returning hole is located on the side of the lower end of the guide cylinder.
8. A homogeneous feed circulating fluidized bed reactor as set forth in claim 1 wherein: and flowmeters are arranged at the lower end of the lifting air conveying pipe and the position of the fluidized air conveying inlet.
9. A homogeneous feed circulating fluidized bed reactor as set forth in claim 1 wherein: the lower part of the cyclone separator is of a conical structure with a gradually reduced inner diameter, and an outlet at the lower end of the cyclone separator is connected with a vertical pipe which is connected with a companion bed.
10. A homogeneous feed circulating fluidized bed reactor as set forth in claim 1 wherein: a first ball valve is arranged at the outlet of the lower end of the cyclone separator; and a second ball valve is arranged on the downcomer.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201911351296.0A CN110982559B (en) | 2019-12-25 | 2019-12-25 | Uniform feeding type circulating fluidized bed reactor |
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| CN201911351296.0A CN110982559B (en) | 2019-12-25 | 2019-12-25 | Uniform feeding type circulating fluidized bed reactor |
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| CN105056855B (en) * | 2015-07-30 | 2017-06-06 | 重庆大学 | Circulating chlorination device with bottom feeding and discharging functions |
| JP6888313B2 (en) * | 2017-02-07 | 2021-06-16 | 株式会社Ihi | Cement manufacturing system |
| CN106947544A (en) * | 2017-04-14 | 2017-07-14 | 中美新能源技术研发（山西）有限公司 | A kind of gasification and pyrolysis integral type top spray reactors of GPG IV and process units and technique |
| CN107841346A (en) * | 2017-11-01 | 2018-03-27 | 浙江大学 | Coal air part heat of gasification electricity fuel-gas multiple production device and method |
| CN109012513B (en) * | 2018-08-16 | 2020-11-03 | 中国石油大学(北京) | Methanol-to-olefin reactor |
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