CN108325295B - Method and device for separating fine particles in high-temperature gas by fluidized bed - Google Patents
Method and device for separating fine particles in high-temperature gas by fluidized bed Download PDFInfo
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- CN108325295B CN108325295B CN201710717667.7A CN201710717667A CN108325295B CN 108325295 B CN108325295 B CN 108325295B CN 201710717667 A CN201710717667 A CN 201710717667A CN 108325295 B CN108325295 B CN 108325295B
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/66—Regeneration of the filtering material or filter elements inside the filter
- B01D46/74—Regeneration of the filtering material or filter elements inside the filter by forces created by movement of the filter element
- B01D46/78—Regeneration of the filtering material or filter elements inside the filter by forces created by movement of the filter element involving centrifugal forces
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
- B01D46/30—Particle separators, e.g. dust precipitators, using loose filtering material
Abstract
The present disclosure relates to a method and a device for separating fine particulate matters in high-temperature gas by a fluidized bed, and provides a method for separating fine particulate matters in high-temperature gas by a fluidized bed, which comprises the following steps: (i) the high-temperature gas containing fine particles passes through a medium bed layer of the boiling bed under the pressure drive; (ii) after the medium bed layer continuously operates until the pressure difference rises to a certain value, high-temperature gas is blown in from the bottom of the medium bed layer by increasing the gas amount, and nitrogen can also be blown in to ensure that the bed layer is fluidized and boiled, so as to carry out regeneration operation; performing cyclone separation on a gas-solid two-phase mixture containing medium particles and fine particles; after the regeneration is completed, the medium particles return to the lower bed layer, and the gas carrying the fine particles is discharged; and (iii) after the medium bed layer is completely regenerated, switching the bed layer to a normal working state, continuously filtering the high-temperature gas, and sequentially circulating the steps (i) - (ii). Also discloses a device for separating fine particles in high-temperature gas by using the fluidized bed.
Description
Technical Field
The disclosure belongs to the field of waste gas treatment and environmental protection, and relates to a method for regenerating and separating fine particulate matters in high-temperature gas by using a fluidized bed, which is suitable for removing the fine particulate matters in the high-temperature gas. In particular, the present disclosure provides a method and apparatus for purifying high temperature gas in a bubbling bed.
Background
How to effectively remove dust and purify a large amount of high-temperature dust-containing gas generated in the production processes of petroleum, chemical industry, metallurgy, electric power and the like to ensure that the high-temperature dust-containing gas reaches the environmental emission standard or the purpose of recovering energy is a difficult problem which is urgently needed to be solved in China at present. For example, in the coal pyrolysis gasification process, a large amount of coal particles, fly ash and other substances are inevitably carried in the pyrolysis gas, which has adverse effects on the subsequent process, not only affects the quality of tar, but also can block equipment and pipelines in severe cases. Therefore, in order to ensure the high efficiency and safety of the tar liquefaction and collection process and the coal gas utilization process, the fine particulate matters in the pyrolysis gas must be effectively removed at high temperature.
Chinese patent application publication CN1050013267A discloses a method and a device for efficiently trapping ultrafine particles in high-temperature smoke dust. The method traps fine particle contaminants in high temperature gases by means of porous inorganic ceramic membrane separation elements. However, due to the influence of the characteristics of the inorganic ceramic material such as high brittleness and low elasticity, the inorganic membrane element has high manufacturing cost and low packing density, so that the manufacturing cost of the membrane element and the device is high. Meanwhile, the system needs to be assisted by a sound wave auxiliary ash cleaner and a compressed gas pulse back-blowing device, so that fine particles adsorbed on the wall of the inorganic membrane tube are separated from the wall of the inorganic membrane tube, and the manufacturing cost and the operating cost of the system are increased.
The Chinese patent application publication CN104001622A discloses a high-temperature electrostatic dust removal system capable of continuously operating at a high temperature of 300-800 ℃, which can effectively trap fine particles in the pyrolysis gas and realize that the operating resistance of the equipment is less than 600 Pa. However, the system is limited by the restriction of the specific resistance of fine particles, the gas components and other properties, and has the problems of electrode corrosion, and meanwhile, the electric dust collector has large equipment investment and high running cost.
The Chinese invention patent CN103341294B discloses a high-temperature gas filtering device and a filtering method thereof, which improve the filtering efficiency of a sintered metal or ceramic filter tube by a precoating filtering method and are suitable for the working condition of processing viscous dust, tar and water vapor in process gas. However, the method has the problems of complex process, large equipment investment and the like.
Chinese patent CN102716628B discloses a particulate dust removing filter and a dust removing filtering method, wherein the particulate dust removing filter uses solid particulate material as a filtering medium to purify high temperature dust-containing gas or remove dust, heavy tar and other components in pyrolysis gas. But the method has the problems of incomplete removal effect, large energy consumption, complex control and the like.
Therefore, in view of the above-mentioned drawbacks in the prior art, there is a need in the art to develop a method for separating fine particles from high-temperature gas, which can achieve the purpose of effectively removing fine particles from high-temperature gas.
Disclosure of Invention
The present disclosure provides a fluidized bed separation method for fine particles in high-temperature gas, which realizes the purpose of effectively removing the fine particles in the high-temperature gas. The method is simple and effective, the medium bed layer has a special sequencing mode, fine particles with the particle size of less than 2.5 mu m in high-temperature gas can be subjected to efficient gradient filtration, the application range is wide, and the investment and operation cost is low.
In one aspect, the present disclosure provides a method for separating fine particles from a high-temperature gas by using an ebullated bed, comprising the following steps:
(i) the high-temperature gas containing fine particles passes through a medium bed layer of the boiling bed under the pressure driving, wherein the medium particles with a particle size gradient or density gradient ordering mode carry out gradient filtration on the fine particles in the gas;
(ii) after the medium bed continuously operates until the pressure difference rises to a certain value, blowing high-temperature gas or nitrogen into the medium bed from the bottom of the medium bed by increasing the gas amount so as to ensure that the bed is fluidized by boiling to release fine particles intercepted or adsorbed in the medium bed; performing cyclone separation on a gas-solid two-phase mixture containing medium particles and fine particles so as to desorb and regenerate the medium particles; after the regeneration is completed, medium particles return to the lower bed layer, and are naturally settled and layered according to the particle size gradient or density gradient of the medium particles to form an initial sequencing form, and gas carrying fine particles is discharged; and
(iii) and (3) after the medium bed layer is completely regenerated, switching the bed layer to a normal working state, continuously filtering the high-temperature gas, and sequentially circulating the steps (i) - (ii).
In a preferred embodiment, the high-temperature gas is a dusty high-temperature gas at a temperature of 900 ℃ or less.
In another preferred embodiment, the media bed is composed of a plurality of different media particles with good high temperature resistance, corrosion resistance and thermal shock resistance, and the particle size of the media particles is in the range of 0.2 mm-5 mm.
In another preferred embodiment, a density gradient sorting mode is adopted, wherein the particles with large particle size and small density are gradually transited to the particles with small particle size and large density in the upper layer and the lower layer to form a sorting medium bed layer with a density gradient; after the medium particles are regenerated by boiling desorption, a density gradient sequencing medium bed layer is naturally formed due to density difference in the sedimentation process.
In another preferred embodiment, a particle size gradient sorting mode is adopted, wherein particles with small particle sizes are arranged on the upper layer and gradually transited to particles with large particle sizes on the lower layer to form a sorting medium bed layer with a particle size gradient; after the medium particles are regenerated by boiling desorption, a particle size gradient sequencing medium bed layer is naturally formed in the sedimentation process due to the particle size difference.
In another preferred embodiment, the media bed is subjected to a regeneration operation to completely fluidize, boil, and break up the media particles to release the fine particulates that are trapped or adsorbed in the media bed.
In another preferred embodiment, after the medium bed is completely fluidized and boiled and broken, the medium particles are enabled to rotate and revolve at a high speed in the medium bed under the action of a rotational flow field in the cyclone separator, and through the coupling action of the rotation and the revolution, the attachments on the surface of the medium bed and the attachments entering the pore channel are enabled to be desorbed at a high speed under the rotation and the revolution, so that the purpose of medium particle regeneration is achieved.
In another aspect, the present disclosure provides an apparatus for separating fine particles from a high-temperature gas by using an ebullated bed, the apparatus comprising:
a housing;
a media bed disposed within the housing for gradient filtering of the high temperature gas containing fine particulates, the gradient filtering including particle size gradient or density gradient filtering;
the cyclone separator is arranged at the top of the shell and is used for performing cyclone separation on a gas-solid two-phase mixture of medium particles and fine particles contained after the fluidized bed layer is boiled so as to desorb and regenerate the medium particles;
wherein the housing includes a high temperature gas inlet, a purge gas outlet, and a regeneration gas outlet.
In a preferred embodiment, the apparatus further comprises: the inlet distributor is used for enabling the inlet air to be uniformly distributed and simultaneously preventing the inlet air from directly scouring the medium bed layer; the filter screen is used for blocking medium particles during filtering and avoiding the loss of filter materials during operation; and the support plate is used for installing the filter screen and supporting the medium bed layer.
In another preferred embodiment, the height of the medium bed is 0.5 to 1.5 m.
Has the advantages that:
the invention has simple working principle, small investment of the developed device, low operation cost, wide application range and wide application range, can carry out high-efficiency gradient filtration on fine particles with the particle size of less than 2.5 mu m in high-temperature gas, and can be widely applied to the removal of the fine particles in the high-temperature gas in coal pyrolysis gasification, industrial coal-fired boilers, metallurgical industry and the like.
Drawings
The accompanying drawings are included to provide a further understanding of the invention, and are incorporated in and constitute a part of this specification to further illustrate the invention and not limit the invention.
FIG. 1 is a schematic diagram of a media bed density gradient sequencing ebullated bed separator configuration according to the present invention.
FIG. 2 is a schematic diagram of a media bed particle size gradient sequencing ebullated bed separator configuration according to the present invention.
FIG. 3 is a schematic diagram of the operating principle of a media bed density gradient sequencing ebullated bed separator according to the present invention.
FIG. 4 is a schematic diagram of the operating principle of a medium bed particle size gradient sequencing ebullated bed separator according to the present invention.
Figure 5 is a process flow diagram for a 180 million ton/year methanol to olefins regenerator effluent flue gas ebullated bed separator according to example 1 of the present application.
Detailed Description
After extensive and intensive research, the inventor of the application finds that the conventional method adopts cyclone dust removal or particle layer filtration for fine particles in high-temperature gas; in actual production, cyclone dust removal has the problems of low separation precision, low separation efficiency and the like, and the classification efficiency of fine dust particles filtered by a particle layer is low and the control is complex; therefore, the invention adopts the particle bed to filter and purify high-temperature gas, avoids the defects of quick pressure difference rise, easy blockage of a filter element and incomplete regeneration of the traditional particle bed filtering device, simultaneously has high separation efficiency compared with cyclone dust removal, and has lower equipment cost and energy consumption and more reliable operation compared with the traditional particle bed filtering device.
The technical concept of the invention is as follows:
the high-temperature gas containing fine particles passes through a medium bed layer with a particle size gradient or density gradient sequencing mode under the driving of pressure to carry out gradient filtration on the fine particles in the gas; continuously running until the operating pressure difference of the medium bed layer is increased to a certain value, increasing the gas amount from the bottom of the bed layer, and blowing in high-temperature gas or nitrogen gas to ensure that the bed layer is completely fluidized and in a boiling state; the fluidized medium particles pass through the cyclone separator, and the medium particles generate high-speed rotation and revolution under the action of a rotational flow field in the cyclone separator, and the aim of desorption and regeneration of the medium particles is fulfilled through the coupling action of the rotation and the revolution; after the regeneration is completed, the medium particles return to the lower bed layer, and are naturally settled and layered according to the particle size gradient or density gradient to form an initial sequencing form; gas is discharged from a top gas phase outlet; the medium particles are continuously used for high-temperature gas purification after being completely regenerated and settled.
In a first aspect of the present disclosure, there is provided a method for separating fine particles from a high temperature gas by an ebullated bed, the method comprising the steps of:
the high-temperature gas containing fine particles passes through the medium bed layer under the pressure driving, wherein the medium particles filter the fine particles in the gas;
after the device continuously operates for a certain time, the pressure difference is increased to a certain value, high-temperature gas or nitrogen is blown into the bottom of the bed layer, the regeneration operation is carried out, the medium bed layer is broken, fluidized and separated, and the fine particles intercepted or adsorbed in the medium bed layer are released; the gas-solid two-phase mixture containing medium particles and fine particles passes through a cyclone separator at the top of the equipment, the medium particles are recovered and returned to a bed layer at the lower part for sedimentation and stratification, and the gas carrying the fine particles is discharged from a gas phase outlet at the top;
and after the medium bed layer is completely regenerated, switching to a normal working state, continuously filtering the high-temperature gas, and sequentially circulating the processes.
In the disclosure, the ebullated bed purification can be used in series with a cyclone separation method, wherein a part of large particles in high-temperature gas are removed in advance by the cyclone separation method, and the solid content is primarily reduced and then further purified by an ebullated bed purification device.
Preferably, the method is applicable to dust-containing high-temperature gas below 900 ℃.
Preferably, the medium bed layer consists of a plurality of different medium particles with good high temperature resistance, corrosion resistance and thermal shock resistance, and the particle size is within the range of 0.2 mm-5 mm.
Preferably, the medium bed is arranged in such a way that the particles with large particle size and small density are arranged on the upper layer and gradually transited to the particles with small particle size and large density on the lower layer to form a gradient ordered medium bed. After boiling regeneration, the medium particles naturally form the gradient ordering medium bed layer due to density difference in the sedimentation process.
Preferably, the medium bed is arranged in another way that the particles with small particle size are arranged at the upper layer and gradually transited to the particles with large particle size at the lower layer to form the ordered medium bed with gradient. After boiling regeneration, the medium particles naturally form the gradient ordering medium bed layer in the sedimentation process due to the particle size difference.
In the present disclosure, the media bed with a certain ordering mode performs gradient filtration on fine particulate matters in high-temperature gas.
In the present disclosure, the regeneration of the media bed causes the media particles to be completely fluidized, to be broken down by boiling, and to release the fine particles intercepted or adsorbed in the bed.
In the disclosure, after the medium bed is regenerated and fluidized, under the action of a rotational flow field in the cyclone separator, medium particles are enabled to generate high-speed rotation and revolution in the medium bed, and through the coupling action of the rotation and the revolution, surface attachments and attachments entering a pore channel are enabled to be desorbed in an accelerated manner under the high-speed rotation and the revolution, so that the purpose of desorption and regeneration of the medium particles is achieved.
In a second aspect of the present invention, there is provided an apparatus for separating fine particles from a high temperature gas by ebullated bed, the apparatus comprising: a housing; the sequencing medium bed layer is used for filtering fine particles carried in high-temperature gas; the cyclone separator is used for separating, regenerating and recovering medium particles when the medium bed layer is fluidized, and simultaneously discharging regeneration gas carrying fine particles from the upper gas phase outlet; the shell comprises a high-temperature gas inlet, a purified gas outlet and a regeneration gas outlet.
Preferably, the apparatus further comprises: the support plate is used for installing the filter screen and supporting the medium bed layer; the filter screen is used for blocking medium particles during filtering and avoiding the loss of filter materials during operation; an inlet distributor for distributing the inlet air evenly while avoiding direct scouring of the inlet air against the media bed.
Preferably, the height of the medium bed layer is 0.5-1.5 m, and the lower part of the bed layer can be paved with sand with larger grain diameter to be used as a bearing layer for preventing medium particles from running and being damaged and simultaneously ensuring uniform flow distribution during regeneration.
In the disclosure, a cyclone separator is arranged at the top of a shell, after boiling and fluidization, mixed gas enters from the upper part and forms a rotational flow through an air inlet, medium particles with larger particle size return to a bed layer through a bottom solid-phase outlet, and fine particles with small particle size and nitrogen are discharged from a gas-phase outlet.
Preferably, the fluidized bed separation device for fine particles in high-temperature gas disclosed by the invention can be popularized to various heterogeneous separation occasions where fine particles are carried in high-temperature gas.
Reference is made to the accompanying drawings.
FIG. 1 is a schematic diagram of a media bed density gradient sequencing ebullated bed separator configuration according to the present invention. As shown in fig. 1, the equipment comprises a high-temperature gas inlet 1 and an inlet distributor 4, a regeneration gas outlet 2 and a cyclone separator 3 which are arranged at the top, and a purified gas outlet 7, a filter screen 5 and a support plate 6 which are arranged at the bottom, wherein the equipment shell comprises different particle filter materials, and the filter materials are arranged in an ordering mode of large particle size, small density to small particle size and large density from top to bottom and are used for carrying out gradient interception and adsorption on particles in gas when the device runs; a filter cap is arranged on the equipment supporting plate 6 and used for blocking the filter material and preventing the filter material from leaking and being damaged; the top of the equipment is provided with a cyclone separator 3 which is used for washing and desorbing the filter material when the device is regenerated and discharging the regenerated gas carrying the fine particles.
FIG. 2 is a schematic diagram of a media bed particle size gradient sequencing ebullated bed separator configuration according to the present invention. As shown in fig. 2, the equipment comprises a purified gas outlet 7, a regenerated gas outlet 2 and a cyclone separator 3 which are arranged at the top, and a high-temperature gas inlet 1, an inlet distributor 4, a filter screen 5 and a support plate 6 which are arranged at the bottom, wherein the equipment shell comprises one or more granular filter materials with different grain sizes and similar density, and the filter materials are arranged in an ordering mode from top to bottom according to the grain size from small to large and are used for carrying out gradient interception and adsorption on particulate matters in gas when the device runs; a filter cap is arranged on the equipment supporting plate 6 and used for blocking the filter material and preventing the filter material from leaking and being damaged; the top of the equipment is provided with a cyclone separator 3 which is used for washing and desorbing the filter material when the device is regenerated and discharging the regenerated gas carrying the fine particles.
FIG. 3 is a schematic diagram of the operating principle of a media bed density gradient sequencing ebullated bed separator according to the present invention. As shown in fig. 3, the workflow includes: gradient filtration 11, boiling fluidization 12, autorotation desorption 13, separation and sedimentation 14 and sequencing layering 15, wherein high-temperature gas containing fine particles enters the equipment from a gas inlet above the equipment and passes through a medium bed layer, and medium particles filter the fine particles in the gas; after the device continuously operates for a certain time, the pressure difference is increased to a certain value, high-temperature gas or nitrogen is blown into the bottom of the bed layer, the regeneration operation is carried out, the medium bed layer is broken, fluidized and separated, and the fine particles intercepted or adsorbed in the medium bed layer are released; the gas-solid two-phase mixture containing medium particles and fine particles passes through a cyclone separator at the top of the equipment, the medium particles are recovered and returned to a bed layer at the lower part for sedimentation and stratification, and the gas carrying the fine particles is discharged from a gas phase outlet at the top; and after the medium bed layer is completely regenerated, switching to a normal working state, continuously filtering the high-temperature gas, and sequentially circulating the processes.
FIG. 4 is a schematic diagram of the operating principle of a medium bed particle size gradient sequencing ebullated bed separator according to the present invention. As shown in fig. 4, the workflow includes: gradient filtration 11, boiling fluidization 12, autorotation desorption 13, separation and sedimentation 14 and sequencing layering 15, wherein high-temperature gas containing fine particles enters the equipment from a gas inlet below the equipment and passes through a medium bed layer, and the medium particles filter the fine particles in the gas; after the device continuously operates for a certain time, the pressure difference is increased to a certain value, high-temperature gas or nitrogen is blown in from the bottom of the bed layer by increasing the gas amount, and regeneration operation is carried out to break, fluidize and separate the medium bed layer and release the fine particles intercepted or adsorbed in the medium bed layer; the gas-solid two-phase mixture containing medium particles and fine particles passes through a cyclone separator at the top of the equipment, the medium particles are recovered and returned to a bed layer at the lower part for sedimentation and stratification, and the gas carrying the fine particles is discharged from a gas phase outlet at the top; and after the medium bed layer is completely regenerated, switching to a normal working state, continuously filtering the high-temperature gas, and sequentially circulating the processes.
Figure 5 is a process flow diagram for a 180 million ton/year methanol to olefins regenerator effluent flue gas ebullated bed separator according to example 1 of the present application. As shown in fig. 5, methanol is sent to a reactor 21 for treatment, the obtained reaction gas is discharged from the top, and the obtained product is sent to a regenerator 22 for reaction; unreacted methanol returns to the reactor 21 to be continuously treated, flue gas containing catalyst fine powder obtained by reaction firstly enters a pre-cyclone separator 23 to remove larger catalyst particles, the removed catalyst particles are sent to a particle storage tank 24, the flue gas subjected to pre-dust removal enters a fluidized bed separator group 25 through an air inlet valve 26, nitrogen is sent to the fluidized bed separator group 25 through a nitrogen inlet valve, a medium bed layer filters the flue gas, the fine particles in the removed gas are subjected to heat recovery through a waste heat boiler, purified gas is sent to a chimney through an air outlet valve 28 to be emptied, and the catalyst is recovered through a regenerated gas outlet valve 29; wherein, the boiling bed separator group comprises 6 separators working in parallel, 5 separators working in 1 mode, continuously operating until the pressure difference is increased to 500Pa, and alternately switching to regeneration operation; and after the regeneration is completed, switching to a normal working state to continue running.
Examples
The invention is further illustrated below with reference to specific examples. It is to be understood, however, that these examples are illustrative only and are not to be construed as limiting the scope of the present invention. Test methods in which specific conditions are not specified in the following examples are generally carried out under conventional conditions or under conditions recommended by the manufacturer. All percentages and parts are by weight unless otherwise indicated.
Example 1:
in a process of preparing olefin from methanol at a rate of 180 ten thousand tons per year, according to the method of the invention, a bubbling bed is adopted to filter and purify the fume discharged by a regenerator containing a solid catalyst, so as to remove residual waste catalyst particles, and the specific operation process and effect are described as follows:
1. material Properties and associated parameters
The discharged flue gas of the regenerator for preparing the olefin from the methanol is a gas-solid two-phase mixture, the gas contains solid catalyst particles, the gas is a continuous phase, and the solid catalyst is a disperse phase medium. The treatment capacity of discharged flue gas is 62500Nm3The operating temperature is 260-680 ℃, and the content of the catalyst is 60-400 mg/Nm3The average particle size was 2.5. mu.m.
2. Fluidized bed device
The device has a diameter of 2.5m and a height of about 6m, and a cyclone separator is arranged at the top of the device and is used for recovering medium particles during regeneration and discharging regeneration gas outwards. The medium particles used by the device are three kinds of quartz sand with the particle diameters of 0.5-1 mm, 1-2 mm and 2-3 mm, the particle diameters are graded and sequenced, the height of a bed layer is about 1500mm, and the single-unit treatment capacity is 12500Nm3And 6 stations are connected in parallel, wherein 5 stations run, 1 station is standby, and the regeneration states are switched in turn.
3. Carrying out the process
As shown in fig. 5, the method according to the present invention is implemented as follows:
the processing object is the discharged flue gas of the methanol-to-olefin regenerator, and the regeneration gas is nitrogen.
(1) Flue gas containing catalyst fines from a methanol to olefins regenerator is first passed to a pre-cyclone to remove larger catalyst particles. The pre-dedusted flue gas passes through a fluidized bed separator group, wherein a medium bed layer filters the flue gas, and fine particles in the removed gas are exhausted through a chimney after heat is recovered by a waste heat boiler;
(2) the fluidized bed separator group comprises 6 separators which work in parallel, 5 separators which work in 1 mode are continuously operated until the pressure difference is increased to 500Pa, and the separators are alternately switched to regeneration operation;
(3) and after the regeneration is completed, switching to a normal working state to continue running.
4. Effects of the implementation
(1) Separation effect
The solid content of the regenerated flue gas is 400mg/Nm after passing through the fluidized bed separator3Down to 10mg/Nm3The particle removal rate reaches 97.5 percent.
The regeneration is carried out once every 10h, the separation efficiency of the regenerated medium particles is about more than 99% of the initial operation condition, and the separation efficiency is still kept at 95% under the long-term operation condition. The separation efficiency of 0.5 μm particles is 60-90%, and the separation efficiency of 1.0 μm particles is 80-95%.
(2) Regeneration effect
The medium particles can be effectively regenerated, the catalyst residual rate on the surfaces of the medium particles is below 5%, and the pore attachment residual rate is below 15%.
The above-mentioned embodiments are merely preferred embodiments of the present invention, and are not intended to limit the scope of the present invention. That is, all equivalent changes and modifications made according to the contents of the claims of the present invention should be considered to be within the technical scope of the present invention.
All documents referred to herein are incorporated by reference into this application as if each were individually incorporated by reference. Furthermore, it should be understood that various changes and modifications of the present invention can be made by those skilled in the art after reading the above teachings of the present invention, and these equivalents also fall within the scope of the present invention as defined by the appended claims.
Claims (8)
1. A method for separating fine particles in high-temperature gas by using an ebullated bed comprises the following steps:
(i) high-temperature gas containing fine particles passes through a medium bed layer of the fluidized bed under the driving of pressure, wherein the medium bed layer adopts a particle size gradient sorting mode, and particles with small particle sizes are gradually transited to particles with large particle sizes in an upper layer and in a lower layer; the medium particles with a particle size gradient sorting mode carry out gradient filtration on fine particles in the gas;
(ii) after the medium bed continuously operates until the pressure difference is increased to a certain value, blowing the high-temperature gas or nitrogen by increasing the gas amount from the bottom of the medium bed to make the bed boiling and fluidizing so as to release the fine particles intercepted or adsorbed in the medium bed; performing cyclone separation on a gas-solid two-phase mixture containing medium particles and fine particles by using a cyclone separator arranged at the top in a boiling bed shell so as to desorb and regenerate the medium particles; after the regeneration is completed, medium particles return to the lower bed layer, and are naturally settled and layered according to the particle size gradient of the medium particles to form an initial sequencing form, and gas carrying fine particles is discharged; and
(iii) after the medium bed layer is completely regenerated, switching the bed layer to a normal working state, continuously filtering the high-temperature gas, and sequentially circulating the steps (i) - (ii),
wherein the ebullated bed shell comprises a purge gas outlet and a regeneration gas outlet disposed at the top, and a high temperature gas inlet disposed at the bottom.
2. The method of claim 1, wherein: the high-temperature gas is dust-containing high-temperature gas below 900 ℃.
3. The method of claim 1, wherein: the medium bed layer is composed of various medium particles with good high temperature resistance, corrosion resistance and thermal shock resistance, and the particle size of the medium bed layer is within the range of 0.2 mm-5 mm.
4. The method of claim 1, wherein: when the medium bed layer is regenerated, medium particles are completely fluidized, boiled and broken to release the fine particles intercepted or adsorbed in the medium bed layer.
5. The method of claim 4, wherein: after the medium bed layer is completely fluidized, boiled and broken, medium particles are enabled to generate high-speed rotation and revolution in the medium bed layer under the action of a rotational flow field in the cyclone separator, and through the coupling action of the rotation and the revolution, surface attachments and attachments entering a pore passage are enabled to be desorbed in an accelerated manner under the high-speed rotation and the revolution, so that the purpose of medium particle regeneration is achieved.
6. An ebullated bed separation apparatus for fine particulates in a hot gas for use in the method of claim 1, the apparatus comprising:
a housing; the medium bed layer is arranged in the shell and is used for carrying out gradient filtration on high-temperature gas containing fine particles, wherein the medium bed layer adopts a particle size gradient sorting mode, and particles with small particle sizes are arranged on the upper layer and gradually transited to particles with large particle sizes on the lower layer; the cyclone separator (3) is arranged at the top of the shell and is used for carrying out cyclone separation on a gas-solid two-phase mixture of medium particles and fine particles contained after the fluidized bed layer is boiled so as to desorb and regenerate the medium particles; wherein the housing comprises a high temperature gas inlet (1), a purge gas outlet (7) and a regeneration gas outlet (2).
7. The apparatus of claim 6, wherein: the device also includes: the inlet distributor (4) is used for enabling the inlet air to be uniformly distributed and simultaneously preventing the inlet air from directly scouring the medium bed layer; the filter screen (5) is used for blocking medium particles during filtering and avoiding the filter material from running and being damaged during operation; and the support plate (6) is used for installing the filter screen and supporting the medium bed layer.
8. The apparatus of claim 6, wherein: the height of the medium bed layer is 0.5-1.5 m.
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| WO2022105773A1 (en) * | 2020-11-17 | 2022-05-27 | 北京滤分环保技术有限责任公司 | Strong magnet particle accelerated material cleaning method and application thereof |
| CN114751482A (en) * | 2022-04-27 | 2022-07-15 | 华东理工大学 | Method and device for adsorption denitrification of domestic sewage tail water |
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| US6440198B1 (en) * | 2000-11-09 | 2002-08-27 | Siemens Westinghouse Power Corporation | Cost effective moving granular bed filters for particulates and contaminants removal |
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| CN1470310A (en) * | 2003-06-18 | 2004-01-28 | 宁波大学 | Granular bed filter dust-collector and method thereof |
| CN1647847A (en) * | 2004-11-22 | 2005-08-03 | 宁波大学 | Granular bed gas purifying device and its method |
| CN102716622A (en) * | 2012-07-06 | 2012-10-10 | 哈尔滨工业大学（威海） | Integrated bag-type dust removal and fluidized adsorption device |
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