CN113041759B - Bottom flow gas-solid separation method and device for multitube cyclone separator - Google Patents
Bottom flow gas-solid separation method and device for multitube cyclone separator Download PDFInfo
- Publication number
- CN113041759B CN113041759B CN201911375108.8A CN201911375108A CN113041759B CN 113041759 B CN113041759 B CN 113041759B CN 201911375108 A CN201911375108 A CN 201911375108A CN 113041759 B CN113041759 B CN 113041759B
- Authority
- CN
- China
- Prior art keywords
- gas
- dust
- filter
- receiving bin
- cyclone separator
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- 238000000926 separation method Methods 0.000 title claims abstract description 80
- 239000007787 solid Substances 0.000 title claims abstract description 38
- 239000000428 dust Substances 0.000 claims abstract description 213
- 239000002245 particle Substances 0.000 claims abstract description 115
- 230000001105 regulatory effect Effects 0.000 claims abstract description 43
- 239000000463 material Substances 0.000 claims abstract description 22
- 238000000034 method Methods 0.000 claims description 23
- 238000007664 blowing Methods 0.000 claims description 21
- 230000000712 assembly Effects 0.000 claims description 17
- 238000000429 assembly Methods 0.000 claims description 17
- 238000001914 filtration Methods 0.000 claims description 13
- 230000000694 effects Effects 0.000 abstract description 16
- 238000010926 purge Methods 0.000 abstract description 6
- 238000005299 abrasion Methods 0.000 abstract description 5
- 239000007789 gas Substances 0.000 description 199
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 45
- 239000003546 flue gas Substances 0.000 description 45
- 238000004523 catalytic cracking Methods 0.000 description 19
- 230000008569 process Effects 0.000 description 10
- 238000007599 discharging Methods 0.000 description 7
- 238000011084 recovery Methods 0.000 description 7
- 238000006477 desulfuration reaction Methods 0.000 description 4
- 230000023556 desulfurization Effects 0.000 description 4
- 238000005265 energy consumption Methods 0.000 description 4
- 239000000843 powder Substances 0.000 description 4
- 239000002918 waste heat Substances 0.000 description 4
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- 230000005611 electricity Effects 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 230000009471 action Effects 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 230000008859 change Effects 0.000 description 2
- 239000007795 chemical reaction product Substances 0.000 description 2
- 230000001276 controlling effect Effects 0.000 description 2
- 238000011044 inertial separation Methods 0.000 description 2
- 230000007246 mechanism Effects 0.000 description 2
- JTJMJGYZQZDUJJ-UHFFFAOYSA-N phencyclidine Chemical class C1CCCCN1C1(C=2C=CC=CC=2)CCCCC1 JTJMJGYZQZDUJJ-UHFFFAOYSA-N 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000004904 shortening Methods 0.000 description 2
- 238000003466 welding Methods 0.000 description 2
- 230000002159 abnormal effect Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 239000010779 crude oil Substances 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000011010 flushing procedure Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000003502 gasoline Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- JRZJOMJEPLMPRA-UHFFFAOYSA-N olefin Natural products CCCCCCCC=C JRZJOMJEPLMPRA-UHFFFAOYSA-N 0.000 description 1
- 238000005192 partition Methods 0.000 description 1
- 230000000704 physical effect Effects 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- QQONPFPTGQHPMA-UHFFFAOYSA-N propylene Natural products CC=C QQONPFPTGQHPMA-UHFFFAOYSA-N 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 239000000779 smoke Substances 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D50/00—Combinations of methods or devices for separating particles from gases or vapours
- B01D50/20—Combinations of devices covered by groups B01D45/00 and B01D46/00
Landscapes
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Cyclones (AREA)
Abstract
The invention provides a bottom flow gas-solid separation method and a separation device of a multi-pipe cyclone separator, wherein dust-containing gas enters the multi-pipe cyclone separator to separate dust particles from gas, and the separated dust particles and part of gas enter a receiving bin from a dust discharge port at the bottom of the multi-pipe cyclone separator, and the dust particles and the gas entering the receiving bin form bottom flow; a filter in the receiving bin separates the underflow and obtains purified gas; the purge gas is discharged after passing through a flow meter and a regulating valve. Compared with the traditional mode of arranging the cyclone separator and the critical nozzle after the material receiving bin, the invention can effectively ensure the high-efficiency separation of the bottom flow gas and the solid and the long-period reliability of equipment, avoid the potential safety hazard caused by the abrasion of the critical nozzle, and further improve the separation effect of the multi-pipe cyclone separator by adjusting the gas flow entering the material receiving bin.
Description
Technical Field
The invention relates to the technical field of petrochemical industry, in particular to a bottom flow gas-solid separation method and a separation device of a multi-tube cyclone separator.
Background
Catalytic cracking is one of the most important crude oil secondary conversion processes of refineries, and is a main provider of gasoline and diesel oil as fuel and propylene as petrochemical raw material in China at present. Currently, in order to reduce the energy consumption of the device, catalytic cracking devices are equipped with a flue gas energy recovery system, and mainly utilize a flue gas turbine to convert a part of heat energy of dust-containing gas generated in catalytic cracking into electric energy.
In the related art, as shown in fig. 1, a dust-containing gas from a regenerator is first introduced into a multi-tube cyclone 10 (hereinafter referred to as a triple cyclone), and gas and dust particles of the dust-containing gas are separated; after the separation operation, in order to ensure that the multi-pipe cyclone separator 10 has higher dust removal efficiency, the dust discharge port of the multi-pipe cyclone separator 10 generally has a certain air discharge amount, so that a certain proportion of gas falls into the receiving bin 20 along with dust particles separated by the multi-pipe cyclone separator, and another part of gas enters the flue gas turbine 50 to drive the impeller of the flue gas turbine to generate electricity, then sequentially passes through the waste heat boiler, desulfurization and denitrification equipment and the like, and finally enters the chimney 130 to be discharged into the atmosphere. Where a proportion of the gas and dust particles are collectively referred to as a multi-cyclone underflow, it will be appreciated that, since there is no loss of a portion of the gas entering the receiving hopper, in the following description, the portion of the gas entering the receiving hopper through the dust discharge of the multi-cyclone 10 will be referred to as the gas in the underflow.
In order to remove dust particles contained in the underflow, a fourth cyclone (hereinafter referred to as a four-cyclone) and a critical nozzle 40 are sequentially provided after the receiving bin 20, the four-cyclone is used for removing dust particles contained in the underflow gas in the receiving bin 20, and the separated underflow gas is introduced into a flue gas duct downstream of the flue gas turbine 50 through the critical nozzle 40 and is discharged into the atmosphere through the flue gas duct.
In addition, when the multi-pipe cyclone separator 10 or the flue gas turbine 50 fails, the pipeline entering the flue gas turbine 50 can be closed, so that the dust-containing gas directly passes through a bypass with a pressure reducing pore plate 60 and then enters a chimney through equipment such as a waste heat boiler, desulfurization and denitrification and the like.
However, the above-described process for separating the underflow of a multi-tube cyclone has the following drawbacks: firstly, the granularity of the powder entering the four-screw is smaller, the powder is easy to agglomerate, so that the four-screw dipleg is often blocked, the powder separated by the four-screw cannot be smoothly discharged, and furthermore, the dust content of the gas entering the critical nozzle exceeds the standard, the abrasion of the critical nozzle and the failure of the flow control function are easily caused due to the extremely high flue gas speed in the critical nozzle, and even accidents such as abrasion and air leakage of a main flue gas pipeline are caused in serious cases, so that the safety production of the catalytic cracking device is seriously influenced. Secondly, when the main air volume of the regenerator is greatly fluctuated due to the reasons of fluctuation of raw material properties, change of process parameters, adjustment of a processing scheme and the like, the critical nozzle cannot adjust the air flow, the flow of the air entering the receiving bin cannot be always maintained at the optimized proportion of 2-8% of the dust-containing air flow, namely the separation efficiency of the multi-tube cyclone is difficult to ensure, and when the air flow entering the receiving bin deviates from the ideal proportion coefficient, the problems of the reduction of the separation efficiency of the multi-tube cyclone, the shortening of the startup period of the flue gas turbine, the increase of the total energy consumption of the catalytic cracking device and the like are caused.
In addition to catalytic cracking units in refineries, some industrial fluidized bed reactors often employ similar multi-tube cyclones as described above, such as methanol-to-olefins units in coal-based plants. In the device for preparing olefin from methanol, a multitube cyclone separator is arranged outside a reactor and a regenerator, and is also called as triple cyclone in industry for short. Wherein the effect of the reactor trirotation is to further separate particles carried in the reaction product gas, and the effect of the regenerator trirotation is the same as the trirotation in the regenerator of the catalytic cracking unit. Because of different physical properties of gas media and different gas flow rates, at present, most of three-rotation reactors and three-rotation regenerators of a methanol-to-olefin device are not provided with flue gas turbines similar to a catalytic cracking device.
However, in order to maintain the efficient operation of the three-cyclone reactor or the three-cyclone regenerator, a certain proportion of gas needs to flow out of the dust discharge port at the bottom of the three-cyclone reactor, and the gas needs to be separated from the particles after the three-cyclone separation.
Disclosure of Invention
In the prior art, when a cyclone separator arranged behind a receiving bin is used for separating gas and dust particles in underflow entering the receiving bin, the problems that the dust content in the separated gas exceeds the standard, a critical nozzle is easy to wear, the separation performance of the multi-pipe cyclone separator is further reduced and the like are easily caused due to the fact that a dipleg of the cyclone separator is easy to bridge or blow-by. The invention provides a method and a device for separating bottom flow gas from solid of a multi-tube cyclone separator, which are used for solving a plurality of problems in the prior art.
In order to achieve the above purpose, the embodiment of the present invention adopts the following technical scheme:
In one aspect, the embodiment of the invention provides a method for separating bottom flow gas and solid of a multi-tube cyclone separator, which comprises the steps that dust-containing gas enters the multi-tube cyclone separator to separate dust particles from the gas.
Dust particles and a part of gas collected after the separation operation enter a receiving bin from a dust discharge port at the bottom of the multi-pipe cyclone separator, and the dust particles and the gas entering the receiving bin form underflow.
And a filter is arranged in the receiving bin and is used for separating gas and dust particles in the underflow and obtaining purified gas.
The purified gas leaving the filter is discharged after passing through a flow meter and a regulating valve for regulating the flow ratio of the gas entering the receiving bin to the dust-containing gas entering the inlet of the multi-tube cyclone.
The method for separating the bottom flow gas and the solid of the multi-pipe cyclone separator, wherein a filter is arranged in the receiving bin and is used for separating gas and dust particles in the bottom flow and obtaining purified gas, and the method further comprises the following steps: the gas and dust particles in the bottom flow are pre-separated through a pre-separator arranged in the receiving bin, and after a part of dust particles in the bottom flow are separated by the pre-separator, the unseparated dust particles and gas enter a filter for further separation.
The method for separating bottom flow gas from solid of the multi-pipe cyclone separator, wherein the regulating valve is used for regulating the proportion of gas entering the material receiving bin to dust-containing gas entering the inlet of the multi-pipe cyclone separator, and the method further comprises the following steps: the regulating valve is used for regulating the flow of the purified gas obtained after passing through the filter according to the flow of the dust-containing gas entering the inlet of the multi-pipe cyclone separator, so that the flow ratio of the purified gas to the dust-containing gas is between 2% and 8%.
The embodiment of the invention also provides a underflow gas-solid separation device of the multi-pipe cyclone separator, which comprises the multi-pipe cyclone separator, a receiving bin and a filter; the receiving bin is provided with a dust inlet which is connected with a dust outlet at the bottom of the multi-pipe cyclone separator; the filter is arranged in the receiving bin and is used for filtering gas and dust particles in the bottom flow entering the receiving bin; the gas outlet of the filter is connected with an exhaust pipeline, and the exhaust pipeline is provided with a flowmeter and a regulating valve.
The underflow gas-solid separation device of the multi-pipe cyclone separator, wherein the receiving bin is provided with an outlet; the filter comprises a tube plate, a filter head and a plurality of vertical filter tubes; the tube plate is arranged on an outlet of the receiving bin, a plurality of filter tubes are arranged below the tube plate in an array mode, the filter seal head is arranged above the tube plate, and the filter seal head and the tube plate enclose a purified gas cavity.
The purification gas chamber is internally provided with a plurality of back-blowing air openings, each back-blowing air opening is communicated with one filter pipe, and the back-blowing air openings are used for carrying out back-blowing on the plurality of filter pipes one by one or group by group in sequence through a manual or automatic control program so as to clean dust particles attached to the filter pipes.
The underflow gas-solid separation device of the multi-pipe cyclone separator is characterized in that a preseparator is further arranged in the receiving bin, and an inlet of the preseparator is connected with a dust inlet and is used for preseparating gas and dust particles in the underflow so as to reduce the quantity of dust particles carried in the gas entering the filter.
The underflow gas-solid separation device of the multi-pipe cyclone separator comprises a shell, wherein the shell is provided with an air inlet channel, an air outlet channel and a dust exhaust pipeline, the air inlet channel is connected with a dust inlet, and the air outlet channel and the dust exhaust pipeline are both communicated with the inner cavity of a receiving bin.
The underflow gas-solid separation device of the multi-pipe cyclone separator, wherein the preseparator comprises a supporting piece and a baffle plate assembly; the supporting piece is horizontally arranged on the inner wall of the receiving bin and is positioned between the dust inlet and the filter; the baffle assembly comprises a plurality of baffles which are arranged on the supporting piece at intervals along the extending direction perpendicular to the dust inlet and are positioned on the side surface of the supporting piece away from the filter; gaps are reserved between adjacent baffles; the baffle is used for colliding with gas and dust particles in the bottom flow so that part of the dust particles in the bottom flow are deposited to the bottom of the receiving bin along the surface of the baffle, and the gas and the unseparated dust particles in the bottom flow enter the filter through the gap for further separation.
The underflow gas-solid separation device of the multi-pipe cyclone separator comprises a plurality of baffle assemblies, wherein the baffle assemblies are arranged on a support at intervals along the extending direction parallel to the dust inlet; gaps in adjacent baffle assemblies are arranged in a staggered manner.
The underflow gas-solid separation device of the multi-pipe cyclone separator is characterized in that the baffle plates are arranged at two ends of the baffle plate along the direction perpendicular to the extending direction of the dust inlet, the baffle plates extend along the direction towards the dust inlet, and a preset included angle is formed between the baffle plates.
The embodiment of the invention provides a method and a device for separating bottom flow gas and solid of a multi-pipe cyclone separator, wherein dust-containing gas enters the multi-pipe cyclone separator to separate dust particles from gas, and the dust particles and a part of gas collected after separation operation enter a receiving bin from a bottom dust discharge port of the multi-pipe cyclone separator, and the dust particles entering the receiving bin and the part of gas form bottom flow; a filter is arranged in the receiving bin and is used for separating gas and dust particles in the underflow and obtaining purified gas; the purified gas leaving the filter is discharged after passing through a flow meter and a regulating valve for regulating the flow ratio of the gas entering the receiving bin to the dust-containing gas entering the inlet of the multi-tube cyclone. According to the embodiment, the gas and dust particles entering the underflow are separated through the filter arranged in the receiving bin, compared with a traditional mode that the cyclone separator and the critical nozzle are sequentially arranged after the receiving bin, the high-efficiency separation of the underflow gas and the solid of the multi-pipe cyclone separator and the long-period reliability of equipment can be effectively guaranteed, potential safety hazards caused by abrasion of the critical nozzle are avoided, and meanwhile, the flow ratio of the gas entering the receiving bin to the dust-containing gas can be adjusted in real time, so that the separation effect of the multi-pipe cyclone separator is further improved.
In addition to the technical problems, the technical features constituting the technical solutions, and the beneficial effects caused by the technical features of the technical solutions described above, the method and the device for separating bottom flow gas and solid of a multi-tube cyclone separator provided by the embodiments of the present invention can solve other technical problems, other technical features included in the technical solutions, and beneficial effects caused by the technical features, which are described in further detail in the detailed description of the present invention.
Drawings
The accompanying drawings, which are incorporated in and constitute a part of this specification, illustrate embodiments consistent with the disclosure and together with the description, serve to explain the principles of the disclosure.
FIG. 1 is a schematic process flow diagram of an energy recovery system in a conventional catalytic cracking process;
FIG. 2 is a schematic structural view of an underflow gas-solid separation device of a multi-tube cyclone separator according to an embodiment of the present invention;
FIG. 3 is a schematic structural view of another underflow gas-solid separation device for a multi-tube cyclone according to an embodiment of the present invention;
FIG. 4 is a cross-sectional view taken along the direction A-A shown in FIG. 3;
Fig. 5 is a schematic diagram of the process flow of the invention applied to a flue gas energy recovery system in catalytic cracking.
Reference numerals illustrate:
10: a multi-tube cyclone separator;
20: a material receiving bin;
201: an outlet;
202: a dust inlet;
30: a cyclone separator;
40: a critical nozzle;
50: a flue gas turbine;
60: a pressure reducing orifice plate;
70: a filter;
701: a tube sheet;
702: a filter tube;
703: a filter head;
80: a preseparator;
801: an air intake passage;
802: an air outlet channel;
803: a dust discharge pipe;
804: a support;
805: a baffle;
806: a partition plate;
807: a gap;
90: a flow meter;
100: a regulating valve;
110: discharging the material tank;
120: a valve;
130: and (5) a chimney.
Detailed Description
For the purpose of making the objects, technical solutions and advantages of the embodiments of the present invention more apparent, the technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings in the embodiments of the present invention, and it is apparent that the described embodiments are some embodiments of the present invention, but not all embodiments of the present invention. All other embodiments, which can be made by those skilled in the art based on the embodiments of the invention without making any inventive effort, are intended to be within the scope of the invention. Thus, the following detailed description of the embodiments of the invention, as presented in the figures, is not intended to limit the scope of the invention, as claimed, but is merely representative of selected embodiments of the invention.
Embodiments of the invention and features of the embodiments may be combined with each other without conflict. The invention will be described in detail below with reference to the drawings in connection with embodiments.
Taking an industrial catalytic cracking device as an example, a process flow of a flue gas energy recovery system in the catalytic cracking device in the prior art is described, as shown in fig. 1, high-temperature flue gas from a regenerator firstly passes through a multi-pipe cyclone separator 10 to remove most of particles contained in the flue gas, and then the flue gas enters a flue gas turbine 50 to drive an impeller to generate electricity, and then enters a chimney 130 to be discharged into the atmosphere. Part of the flue gas enters the receiving bin 20 along with dust particles separated by the multi-pipe cyclone separator 10, the dust particles contained in the part of the gas are removed by the cyclone separator 30 after the part of the gas enters the receiving bin 20, and then the purified gas passes through the critical nozzle 40 and then enters the main flue gas pipeline.
When the multi-pipe cyclone 10 or the flue gas turbine 50 fails, the pipe into the flue gas turbine 50 may be closed so that the high temperature flue gas is discharged into the stack 130 directly through a bypass with a pressure reducing orifice plate 60. Since the cyclone separator 10 is further provided with two stages of cyclones connected in series upstream of the multi-cyclone separator 10, the multi-cyclone separator 10 and the cyclone separator 30 for treating the underflow of the multi-cyclone separator in the flue gas energy recovery system can be simply referred to as three-cyclone and four-cyclone, respectively.
In the actual industrial operation process, as the powder discharged by the three-rotation separation is generally smaller in granularity and higher in viscosity in a high-temperature smoke environment, the four-rotation material leg cannot be smoothly discharged. When the dipleg is provided with a wing valve and other air locking mechanisms, abnormal operation phenomena such as bridging and the like often occur to the four-rotation dipleg; when the air locking mechanism is not arranged, the four-rotation material leg always has air blow-by, and the separation efficiency is seriously reduced. In a word, the separation effect of the design is often difficult to ensure, so that the dust content of the gas entering the critical nozzle is often out of standard, the critical nozzle is easily worn out, the flow control function is invalid, and accidents such as local wear and gas leakage of a main flue gas pipeline are even caused in severe cases. In addition, industrial catalytic cracking device often causes the main air volume of regenerator to have great fluctuation due to the reasons of fluctuation of raw material property, change of technological parameters, adjustment of processing scheme and the like, but the critical nozzle can not carry out flow adjustment on the underflow, so that the flow of gas entering the four-rotation cyclone separator and the flow of flue gas entering the multi-tube cyclone separator can not always keep the ideal proportional relationship of 2-8%, and when the flow of flue gas entering the four-rotation cyclone separator is too small or too large, the problems of reduced three-rotation separation performance, shortened startup period of the flue gas turbine, increased total energy consumption of the device and the like are caused.
Based on the technical problems, the embodiment of the invention provides a bottom flow gas-solid separation method and a separation device of a multi-pipe cyclone separator, wherein the method does not need to arrange a traditional cyclone separator and a critical nozzle after a receiving bin, but arranges a filter at the top of the receiving bin, and purified gas is obtained after filtration and is discharged after passing through a flowmeter and a regulating valve, so that the separation effect of the multi-pipe cyclone separator can be improved.
FIG. 2 is a schematic structural view of an underflow gas-solid separation device of a multi-tube cyclone separator according to an embodiment of the present invention; FIG. 3 is a schematic structural view of another underflow gas-solid separation device for a multi-tube cyclone according to an embodiment of the present invention; FIG. 4 is a cross-sectional view taken along the direction A-A shown in FIG. 3; fig. 5 is a schematic diagram of the process flow of the invention applied to a flue gas energy recovery system in catalytic cracking.
The following specific examples are detailed descriptions taking the application of the multi-tube cyclone separator to the catalytic cracker as an example.
The underflow separation method of the multi-pipe cyclone separator provided by the embodiment of the invention comprises the following steps:
s101: the dust-laden gas enters the multi-tube cyclone 10 where the separation of dust particles from the gas takes place.
It will be appreciated that the dust-containing gas in this embodiment may be flue gas formed in the regenerator of the catalytic cracker or in the regenerator of the methanol-to-olefins unit, or may be reaction product gas formed in the reactor of the methanol-to-olefins unit. Taking a catalytic cracking unit as an example, dust particles are catalyst particles.
S102: dust particles and a part of gas collected after the separation operation enter the receiving bin 20 from a dust discharge port at the bottom of the multi-pipe cyclone separator 10, and the dust particles and the gas entering the receiving bin 20 form underflow.
In order to ensure a high separation effect of the multi-tube cyclone 10, it is generally necessary that a part of the gas enters the receiving bin 20 from the bottom dust discharge port of the multi-tube cyclone 10 together with dust particles. Another portion of the gas passes through the duct into the flue gas turbine 50.
S103: a filter 70 is arranged in the receiving bin 20, the filter 70 being arranged to separate gas and dust particles in the underflow and to obtain a cleaned gas.
In order to avoid adopting the traditional cyclone separator to separate the gas and dust particles falling into the underflow in the receiving bin 20, the filter 70 is arranged at the top of the receiving bin 20 in the embodiment, the filter 70 can separate the gas and dust particles in the underflow to obtain purified gas, and accordingly, the technical problems that in the traditional mode, the dust content of the gas of the critical nozzle 40 is easily out of standard due to unsmooth discharge of the cyclone separator 30, the critical nozzle 40 is easily worn and the flow control function is invalid, and even accidents such as local wear and leakage of a main flue gas pipeline are caused in serious cases are solved.
The filter 70 in this embodiment may be a multi-tube filter to quickly and efficiently separate gas and dust particles from the underflow.
S104: the purge gas exiting the filter 70 is discharged via the flow meter 90 and the regulating valve 100. The regulating valve 100 is used to regulate the flow ratio of gas entering the receiving bin 20 to dust-laden gas entering the inlet of the multi-cyclone 10.
The flow meter 90 is used for indicating the flow rate of the purified gas, the regulating valve 100 is used for controlling the flow rate of the purified gas, the regulating valve 100 and the flow meter 90 can realize linkage operation with the flow meter for displaying the dust-containing gas, and the proportional relation between the flow rate of the gas entering the material receiving bin 20 and the dust-containing gas entering the inlet of the multi-pipe cyclone separator 10 is regulated and controlled in real time, so that the multi-pipe cyclone separator 10 can have the optimal gas leakage flow rate ratio and gas-solid separation effect under different gas treatment capacities.
The method for separating gas and solid in the underflow of the multi-tube cyclone 10 provided by the embodiment can be applied to all devices adopting the multi-tube cyclone, and is used for separating the gas and solid in the underflow of the multi-tube cyclone 10, so that the separation efficiency of the multi-tube cyclone 10 is improved.
Compared with the mode of separating gas and dust particles in the bottom flow in the receiving bin 20 by utilizing the cyclone separator 30 in the prior art, the embodiment of the invention has the advantages that the filter 70 is arranged at the top of the receiving bin 20, the filter 70 can separate the gas and the dust particles in the bottom flow to obtain purified gas, the high-efficiency separation of the bottom flow gas and the solid of the multi-pipe cyclone separator and the long-period reliability of equipment can be effectively ensured, and the potential safety hazard caused by the abrasion of a critical nozzle is avoided; the purified gas passes through a flowmeter 90 and a regulating valve 100, the flowmeter 90 is used for indicating the flow rate of the purified gas, the regulating valve 100 is used for controlling the flow rate of the purified gas, the regulating valve 100 and the flowmeter 90 can realize linkage operation with the flowmeter of the dust-containing gas entering the multi-pipe cyclone separator 10, and the proportional relation between the flow rate of the gas entering the receiving bin 20 and the dust-containing gas entering the inlet of the multi-pipe cyclone separator 10 is regulated and controlled in real time, so that the multi-pipe cyclone separator 10 can have optimal gas leakage flow rate ratio and gas-solid separation effect under different gas treatment capacities.
On the basis of the above embodiment, a filter 70 is disposed in the receiving bin 20, and the filter 70 is used for separating gas and dust particles in the underflow and obtaining purified gas, and before this step, the method further includes:
The gas and dust particles in the underflow are pre-separated by a pre-separator 80 provided in the receiving bin 20, the pre-separator 80 being able to separate a part of the dust particles, the non-separated dust particles and gas being re-entered into the filter 70 for further separation and this step being denoted S1021.
In order to reduce the load of the filter 70 for separating dust particles, the gas and dust particles in the underflow may be pre-separated by the pre-separator 80 disposed in the receiving bin 20 before step S103, and part of the dust particles are pre-separated by the pre-separator 80, which correspondingly reduces the content of the dust particles entering the filter 70 and prolongs the service life of the filter 70.
The pre-separator 80 may be an inertial separator using an inertial separation principle, or a separator using a centrifugal separation principle, such as a cyclone separator. The primary separator need not have too high a separation efficiency, but rather requires a pressure drop that is not too high, primarily to reduce the processing load and blowback frequency of the filter 70, thereby extending the useful life of the filter 70.
As an alternative embodiment of S104, the adjusting valve 100 is used to adjust the flow rate of the purge gas obtained after passing through the filter 70 according to the flow rate of the dust-laden gas entering the inlet of the multi-pipe cyclone separator 10, so that the flow rate ratio of the purge gas to the dust-laden gas is between 2% and 8%, and the multi-pipe cyclone separator 10 has the optimal leakage flow rate ratio and dust particle separation effect under different dust-laden gas flows.
In the actual operation process, when the flow rate of the dust-containing gas entering the multi-pipe cyclone separator changes, a worker can adjust the opening degree of the regulating valve 100 in real time according to the flow rate of the dust-containing gas and the actual flow rate of the purified gas displayed by the flowmeter 90, so that the flow rate ratio of the purified gas to the dust-containing gas is between 2% and 8%, and the multi-pipe cyclone separator 10 is ensured to have the optimal leakage flow rate ratio and separation effect even under the condition of different total main wind flows, wherein the adjustment of the regulating valve can be manually adjusted by the worker or can be adjusted by an automatic control system, when the regulating valve is adjusted by the automatic control system, the regulating valve can be an electromagnetic valve, when the flowmeter of the dust-containing gas detects that the flow rate of the dust-containing gas changes, a detection signal can be transmitted to the automatic control system, and the automatic control system sends an action command to adjust the opening degree of the electromagnetic valve.
As shown in fig. 2, the embodiment of the present invention further provides a multi-cyclone underflow separation device comprising a multi-cyclone 10, a receiving bin 20, and a filter 70; the receiving bin 20 is provided with a dust inlet 202, and the dust inlet 202 is connected with a bottom dust discharge port of the multi-pipe cyclone separator 10; a filter 70 is provided within the receiving bin 20, the filter 70 being for filtering gas and dust particles in the underflow entering the receiving bin 20; the gas outlet of the filter 70 is connected to an exhaust pipe, and a flow meter 90 and a regulating valve 100 are provided in the exhaust pipe.
The multi-pipe cyclone separator 10 can be connected with a regenerator in a catalytic cracking device, and can also be connected with a reactor or a regenerator of a methanol-to-olefin device for carrying out gas-solid separation on dust-containing gas.
The multi-pipe cyclone separator 10 may include a housing and a filter pipe disposed in the housing, wherein the housing has a dust discharge port, and the dust discharge port may be connected to the receiving bin 20 through a connection pipe to introduce a part of gas and dust particles into the receiving bin 20, and another part of gas separated by the multi-pipe cyclone separator 10 enters the gas turbine 50 to drive an impeller of the gas turbine 50 to rotate to generate electricity, for example, the multi-pipe cyclone separator 10 is applied to a catalytic cracker.
The receiving bin 20 may include a bin body, and a dust inlet 202 disposed on the bin body, where the dust inlet 202 may be connected to a dust outlet of the multi-cyclone separator 10, so that the multi-cyclone separator 10 separates dust particles and a part of gas, that is, underflow, and enters the receiving bin 20 through the dust inlet 202. In addition, the bin body can be of a conical structure or a square structure.
The filter 70 is arranged in the receiving bin 20, wherein the filter 70 can filter the gas and dust particles in the bottom flow entering the receiving bin 20 so as to realize the purification and separation of the gas and the dust particles, and avoid the gas containing the dust particles from being directly discharged into the air, thereby not only causing environmental pollution, but also causing the loss of the catalyst.
The gas outlet of the filter 70 is connected to an exhaust pipe, which may be directly connected to the atmosphere or may be connected to the atmosphere through a chimney 130, which is not particularly limited herein.
Wherein, the flow meter 90 and the regulating valve 100 are arranged on the exhaust pipe, the flow meter 90 is used for displaying the flow of the purified gas discharged through the exhaust pipe, and the flow of the purified gas flowing through the exhaust pipe is controlled by the arrangement of the regulating valve 100. While the flow meter 90 and the regulating valve 100 may be conventional products in the prior art, the description of this embodiment is omitted here.
When the total main air flow rate of the regenerator in the catalytic cracking unit is changed, the flow rate of the dust-containing gas entering the multi-pipe cyclone separator 10 is changed, and the opening degree of the regulating valve 100 can be adjusted according to the actual flow rate of the clean gas displayed by the flowmeter 90, so that the flow rate ratio of the clean gas to the dust-containing gas is between 2% and 8%, thereby ensuring that the multi-pipe cyclone separator 10 has the optimal air leakage flow rate ratio and separation effect even under different total main air flows.
When a part of the gas and dust particles enter the receiving hopper 20, the filter 70 filters the gas and dust particles in the underflow flowing into the receiving hopper 20, and the filtered purge gas passes through the gas outlet of the filter 70, enters the exhaust duct, and adjusts the flow rate of the purge gas in the exhaust duct by using the flow meter 90 and the adjusting valve 100 provided in the exhaust duct.
The embodiment of the invention provides a bottom flow gas-solid separation device of a multi-pipe cyclone separator 10, which comprises the multi-pipe cyclone separator 10, a receiving bin 20 and a filter 70; the receiving bin 20 is provided with a dust inlet 202, and the dust inlet 202 is connected with a bottom dust discharge port of the multi-pipe cyclone separator 10; a filter 70 is provided within the receiving bin 20, the filter 70 being for filtering gas and dust particles in the underflow entering the receiving bin 20; the gas outlet of the filter 70 is connected to an exhaust pipe, and a flow meter 90 and a regulating valve 100 are provided in the exhaust pipe. According to the embodiment of the invention, the filter 70 arranged in the material receiving bin 20 is used for filtering the gas and dust particles entering the material receiving bin 20, the traditional mode that the four-rotation and critical nozzles 40 are sequentially arranged behind the material receiving bin 20 is not needed, the gas and dust particles entering the material receiving bin 20 are separated, and the problems that the critical nozzles 40 are worn and the flow control function is invalid due to exceeding of the dust content of the gas caused by unsmooth material discharging of the four-rotation material legs, and even accidents such as local wear and leakage of a main flue gas pipeline are caused in serious cases are avoided.
In addition, the flow rate of the purified gas on the exhaust pipeline can be displayed in real time through the flowmeter 90, and the flow rate of the purified gas on the exhaust pipeline is regulated through the regulating valve 100, so that the flow rate ratio of the purified gas to the dust-containing gas is between 2% and 8%, and the phenomenon that the flow rate of the gas entering the receiving bin 20 is too large or too small, which causes the reduction of the separation performance of the multi-pipe cyclone separator 10, the shortening of the startup period of the flue gas turbine 50 and the increase of the total energy consumption of the catalytic cracking device, is prevented.
As an alternative embodiment of the filter 70, the receiving bin 20 has an outlet 201; the filter 70 includes a tube sheet 701, a plurality of vertical filter tubes 702, and a filter head 703; the tube plate 701 is arranged on the outlet 201, the plurality of filter tubes 702 are arranged below the tube plate 701 in an array manner, the filter seal head 703 is arranged above the tube plate 701, and the filter seal head 703 and the tube plate 701 enclose a purified gas cavity; the inside of the purifying gas chamber is provided with a plurality of back-blowing air openings, each back-blowing air opening is communicated with one filter pipe, namely, the number of the back-blowing air openings is equal to that of the filter pipes, the inside of the purifying gas chamber is provided with the back-blowing air openings which are arranged in one-to-one correspondence with the plurality of filter pipes 702, each back-blowing air opening is communicated with one filter pipe, and the back-blowing air openings carry out back-blowing on the plurality of filter pipes one by one or group by group sequentially through a manual or automatic control program so as to clean dust particles attached to the filter pipes.
The tube sheet 701 may be secured to the outlet 201 of the receiving hopper 20 by welding or bolting to the outlet 201 of the receiving hopper 20, and the shape of the tube sheet 701 may be matched to the shape of the outlet 201 of the receiving hopper 20.
Taking the orientation shown in fig. 2 as an example, a filter tube 702 is arranged below the tube plate 701, a filter seal 703 is arranged above the tube plate 701, and the tube plate 701 and the filter seal 703 enclose a purified gas chamber, wherein the outlet 201 can be arranged on the filter seal 703. In addition, a plurality of through holes arranged in an array can be formed in the tube plate 701, a filter tube 702 is fixedly arranged on each through hole, and the filter tubes 702 can extend in the vertical direction to extend into the material receiving bin 20, so that purified gas separated by the filter tubes 702 can enter the purified gas chamber through the through holes.
When the underflow enters the collection bin 20, the gas in the underflow enters the interior of the filter tube 702 through the filter holes of the filter tube 702, and dust particles are blocked and deposited on the outer wall of the filter tube 702 or in the collection bin 20, so that the separation of the gas and the dust particles in the underflow is realized.
Because the filter 70 is used for a long time, dust particles deposited on the outer wall of the filter tube 702 are more and more, the filter tube 702 needs to be cleaned regularly in time, otherwise, the filtering effect of the filter 70 is reduced, and therefore, the back-blowing air openings corresponding to the filter tubes 702 one by one are arranged in the purified gas chamber, in the embodiment, the opening and closing of the back-blowing air openings can be controlled in a manual or automatic control program mode, so that the filter tubes 702 are back-blown sequentially one by one or group by group, and dust particles attached to the filter tubes 702 are cleaned.
The back-blowing tuyere can be connected with external high-pressure air flow, and the air flow is introduced into the filter pipe 702, so that dust particles attached to the filter pipe 702 fall into the material receiving bin 20 under the action of the high-pressure air flow. In this embodiment, the filtering pipes 702 may be back-blown one by one, or the plurality of filtering pipes 702 may be divided into a plurality of groups, and only one group of filtering pipes 702 or one filtering pipe 702 is back-blown each time, so that the excessive gas amount in the material receiving bin 20 is avoided, the excessive gas pressure in the material receiving bin 20 is caused, the amount of the underflow entering the material receiving bin 20 through the dust exhaust port is reduced, and the separation effect of the multi-pipe cyclone separator is further reduced. It will be appreciated that reference to sequentially referring to this embodiment refers to back-flushing the filter tubes in a certain order.
In addition, to achieve independent control of each blowback port, a valve may be provided on each blowback port, and a worker may selectively open one or more of the valves to blowback the filter tube 702. Further, in order to realize automatic control, a controller can be also arranged, and the opening and closing of the valve are controlled by the controller, so that the automatic control of the back-blowing air port is realized.
As a possible embodiment, a preseparator 80 is further provided in the receiving bin 20, and an inlet of the preseparator 80 is connected to the dust inlet 202 for preseparating gas and dust particles in the underflow to reduce the amount of dust particles carried in the gas entering the filter 70.
In order to reduce the workload of the filter 70, a pre-separator 80 may be disposed in the receiving bin 20, and the pre-separator 80 is used to perform a first treatment on the gas and the dust particles in the underflow, so that part of the dust particles are separated first, and thus the dust particles entering the filter 70 are reduced, so as to achieve the purpose of reducing the workload of the filter 70.
As an alternative embodiment of the preseparator 80, the preseparator 80 comprises a housing having an air inlet channel 801, an air outlet channel 802 and a dust exhaust duct 803, the air inlet channel 801 being connected to the dust inlet 202, the air outlet channel 802 and the dust exhaust duct 803 both communicating with the inner cavity of the receiving bin 20.
Referring to fig. 2, the gas and dust particles in the underflow enter the housing through the gas inlet channel 801, the gas and dust particles in the underflow form centrifugal force during movement, the weight of the dust particles is large, and the received centrifugal force is also large, so that the dust particles can fall into the receiving bin 20 along with the dust discharge pipeline 803, and the lighter gas can be discharged into the receiving bin 20 through the gas outlet pipeline 802, and finally collected at the filter 70. It will be appreciated that in this embodiment the separation principle of the preseparator 80 is the same as that of a cyclone separator.
As another alternative embodiment of the preseparator 80, the preseparator 80 includes a support 804 and a baffle assembly; the support 804 is horizontally disposed on the inner wall of the receiving bin 20 and is located between the dust inlet 202 and the filter 70; the baffle assembly comprises a plurality of baffles 805, the plurality of baffles 805 are distributed on the support 804 at intervals along the extending direction perpendicular to the dust inlet 202, and are positioned on the side of the support 804 away from the filter 70; adjacent baffles 805 have a gap 807 therebetween; the baffle 805 is configured to collide with the gas and dust particles in the underflow so that a portion of the dust particles in the underflow are deposited along the surface of the baffle to the bottom of the receiving bin 20, and the gas and unseparated dust particles in the underflow enter the filter 70 through the gap 807 for further separation.
Referring to fig. 3, the preseparator 80 provided in this embodiment adopts the principle of inertial separation to separate dust particles, where the preseparator 80 may include a support 804, where the support 804 is used as a carrier of a baffle assembly and may be fixed on an inner wall of the receiving bin 20, and a fixing manner of the support 804 and the receiving bin 20 may be a fixing manner of welding or bolting, where the support 804 is horizontally disposed on the inner wall of the receiving bin 20, so that installation of the baffle assembly may be facilitated, and in addition, the support 804 may be a plate-shaped body extending along a direction parallel to the dust inlet 202.
When the gas and dust particles in the underflow enter the receiving bin 20 from the dust, the dust particles firstly collide with the baffle assembly extending along the vertical direction, the baffle assembly intercepts the dust particles, so that part of the dust particles move downwards along the surface of the baffle assembly arranged vertically and directly fall into the receiving bin 20, and the other part of the dust particles are intercepted and adsorbed on the outer surface of the filtering pipe 702 along with the gas passing through the filtering pipe 702 of the filter 70 and continuously proceed along with the back blowing of the back blowing tuyere, and the part of the dust particles fall into the receiving bin 20.
To enhance the separation effect of the preseparator 80, the baffle assembly comprises a plurality of baffles 805, the plurality of baffles 805 being spaced apart on the lower surface of the support 804 in a direction perpendicular to the extension of the dust inlet 202, with gaps 807 between adjacent baffles. In this embodiment, the baffle assembly is designed to be composed of a plurality of baffles, rather than using a whole plate with a larger area, so that the gas in the underflow can flow into the filter 70 along the gap 807 quickly, and the separation efficiency of the filter 70 is improved.
In this embodiment, the extending direction perpendicular to the dust inlet is the arrow direction in fig. 4, and in order to further enhance the separation effect of the preseparator 80, please continue to refer to fig. 4, the baffle assemblies may be multiple groups, and the multiple groups of baffle assemblies are distributed on the support 804 at intervals along the extending direction parallel to the dust inlet 202; gaps 807 in adjacent baffle assemblies are offset.
The gas and dust particles in the underflow first collide with the baffles in the first group of baffle assemblies close to the dust inlet 202, so that part of dust particles move downwards along the surfaces of the vertically arranged baffles and directly fall into the receiving bin 20, and the other part of dust particles enter the second group of baffle assemblies along with the gas through gaps 807 between the adjacent baffles to perform secondary pre-separation, the dust particles and the gas after the secondary pre-separation enter the third group of baffle assemblies through gaps 807 in the second group of baffle assemblies to perform the third pre-separation, and finally, the unseparated dust particles and the gas enter the filter 70 to perform final separation.
It will be appreciated that the number of baffle assemblies in this embodiment is not limited to the three groups described above, and may be freely selected according to practical situations. In addition, the number of baffles in each group of baffle assemblies can be freely designed, for example, the number of baffles in the first group of baffle assemblies can be three, the number of baffles in the second group of baffle assemblies can be four, and the number of baffles in the third group of baffle assemblies can be five.
Further, the baffles are provided with baffles 806 along two ends perpendicular to the extending direction of the dust inlet 202, the baffles 806 extend along the direction facing the dust inlet 202, and the baffles 806 have a preset included angle, preferably, the preset included angle is 90 degrees, so that the baffles and the two baffles 806 form a U-shaped structure with an opening facing the dust inlet 202. By providing a baffle 806, the contact area and contact time of the baffle assembly with the gas and dust particles in the underflow can be increased, increasing the separation efficiency of the preseparator 80.
In order to facilitate discharging, a discharging tank 110 is arranged at the bottom of the receiving bin 20, a valve 120 is arranged between the discharging tank 110 and the receiving bin 20, so that particles can be continuously transferred from the receiving bin 20 to the discharging tank and then discharged out of the device.
As shown in fig. 5, the multi-pipe cyclone underflow gas-solid separation device provided in this embodiment may be applied to a flue gas energy recovery system in a catalytic cracking device, and includes a multi-pipe cyclone 10, where the multi-pipe cyclone 10 has a dust exhaust port and a separation gas outlet, the separation gas outlet is connected with a flue gas turbine 50, another part of gas in the multi-pipe cyclone may enter the flue gas turbine 50 through the separation gas outlet, and part of heat energy of high-temperature flue gas purified by the multi-pipe cyclone 10 is converted into electric energy by the flue gas turbine 50, and the port of the flue gas turbine 50 is connected with a chimney 130.
The dust discharging port of the multi-pipe cyclone separator is sequentially connected with the receiving bin 20, the flowmeter 90 and the regulating valve 100, wherein the receiving bin 20 is internally provided with the preseparator 80 and the filter 70, after gas and dust particles in underflow are separated by the preseparator 80 and the filter 70, the dust particles are deposited in the receiving bin 20, and pure gas is introduced into the chimney 130 through an exhaust pipeline.
The separated gas outlet of the multi-pipe cyclone separator 10 can be sequentially connected with a depressurization orifice plate 60, a waste heat boiler, desulfurization and denitrification equipment and the like, and when the multi-pipe cyclone separator 10 or the flue gas turbine 50 fails, a pipeline entering the flue gas turbine 50 can be closed, so that high-temperature flue gas directly passes through a bypass with the depressurization orifice plate 60 and then enters the chimney 130 through the waste heat boiler, the desulfurization and denitrification equipment and the like.
Finally, it should be noted that: the above embodiments are only for illustrating the technical solution of the present invention, and not for limiting the same; although the invention has been described in detail with reference to the foregoing embodiments, it will be understood by those of ordinary skill in the art that: the technical scheme described in the foregoing embodiments can be modified or some or all of the technical features thereof can be replaced by equivalents; such modifications and substitutions do not depart from the spirit of the invention.
Claims (6)
1. A method for separating bottom flow gas from solid in a multi-tube cyclone separator, comprising:
the dust-containing gas enters a multi-pipe cyclone separator to separate dust particles from the gas;
dust particles and a part of gas collected after the separation operation enter a receiving bin from a dust discharge port at the bottom of the multi-pipe cyclone separator, and the dust particles and the gas entering the receiving bin form underflow;
a filter is arranged in the receiving bin and is used for separating gas and dust particles in the underflow and obtaining purified gas;
The purified gas leaving the filter is discharged through a flowmeter and a regulating valve, and the regulating valve is used for regulating the flow ratio of the gas entering the material receiving bin to the dust-containing gas entering the inlet of the multi-pipe cyclone separator;
a filter is arranged in the receiving bin and is used for separating gas and dust particles in the underflow and obtaining purified gas, and the method further comprises the following steps:
The gas and dust particles in the bottom flow are pre-separated through a pre-separator arranged in a receiving bin, and after a part of dust particles in the bottom flow are separated by the pre-separator, the unseparated dust particles and the gas enter a filter for further separation;
The regulating valve is used for regulating the proportion of the gas entering the material receiving bin to the dust-containing gas entering the inlet of the multi-pipe cyclone separator, and the regulating valve further comprises: the regulating valve is used for regulating the flow of the purified gas obtained after passing through the filter according to the flow of the dust-containing gas entering the inlet of the multi-pipe cyclone separator, so that the flow ratio of the purified gas to the dust-containing gas is 2% -8%.
2. The underflow gas-solid separation device of the multi-pipe cyclone separator is characterized by comprising the multi-pipe cyclone separator, a receiving bin and a filter;
the receiving bin is provided with a dust inlet which is connected with a dust outlet at the bottom of the multi-pipe cyclone separator;
The filter is arranged in the receiving bin and is used for filtering gas and dust particles in the bottom flow entering the receiving bin;
the gas outlet of the filter is connected with an exhaust pipeline, and the exhaust pipeline is provided with a flowmeter and a regulating valve;
the material receiving bin is provided with an outlet; the filter comprises a tube plate, a filter head and a plurality of vertical filter tubes;
the tube plate is arranged on an outlet of the receiving bin, a plurality of filter tubes are arranged below the tube plate in an array manner, the filter end enclosure is arranged above the tube plate, and the filter end enclosure and the tube plate enclose a purified gas cavity;
A plurality of back-blowing air openings are arranged in the purifying gas chamber, each back-blowing air opening is communicated with one filter pipe, and the back-blowing air openings carry out back-blowing on the filter pipes sequentially one by one or group by group through a manual or automatic control program so as to clean dust particles attached to the filter pipes;
And a preseparator is further arranged in the receiving bin, and an inlet of the preseparator is connected with a dust inlet and is used for preseparating gas and dust particles in the underflow so as to reduce the quantity of the dust particles carried in the gas entering the filter.
3. The underflow gas-solid separation device of a multi-tube cyclone separator according to claim 2, wherein the preseparator comprises a housing having an inlet passage, an outlet passage and a dust exhaust duct, the inlet passage being connected to the dust inlet, the outlet passage and the dust exhaust duct both communicating with the interior chamber of the receiving bin.
4. A multi-tube cyclone underflow gas-solid separation apparatus according to claim 3 wherein the preseparator comprises a support and baffle assembly;
the supporting piece is horizontally arranged on the inner wall of the receiving bin and is positioned between the dust inlet and the filter;
The baffle assembly comprises a plurality of baffles which are arranged on the supporting piece at intervals along the extending direction perpendicular to the dust inlet and are positioned on the side surface of the supporting piece away from the filter;
Gaps are reserved between adjacent baffles; the baffle is used for colliding with gas and dust particles in the bottom flow so that part of the dust particles in the bottom flow are deposited to the bottom of the receiving bin along the surface of the baffle, and the gas and the unseparated dust particles in the bottom flow enter the filter through the gap for further separation.
5. The underflow gas-solid separation apparatus of a multi-tube cyclone of claim 4 wherein said baffle assemblies are in a plurality of groups, said plurality of groups being mounted on a support member at intervals along a direction parallel to the direction of extension of the dust inlet; gaps in adjacent baffle assemblies are arranged in a staggered manner.
6. The underflow gas-solid separation apparatus of a multi-tube cyclone as claimed in claim 4 or 5, wherein the baffle plates are provided with a baffle plate at both ends in a direction perpendicular to the direction in which the dust inlet extends, the baffle plate extends in a direction toward the dust inlet, and the baffle plate has a predetermined angle with the baffle plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911375108.8A CN113041759B (en) | 2019-12-27 | 2019-12-27 | Bottom flow gas-solid separation method and device for multitube cyclone separator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201911375108.8A CN113041759B (en) | 2019-12-27 | 2019-12-27 | Bottom flow gas-solid separation method and device for multitube cyclone separator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN113041759A CN113041759A (en) | 2021-06-29 |
| CN113041759B true CN113041759B (en) | 2024-05-28 |
Family
ID=76506148
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201911375108.8A Active CN113041759B (en) | 2019-12-27 | 2019-12-27 | Bottom flow gas-solid separation method and device for multitube cyclone separator |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN113041759B (en) |
Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1622860A (en) * | 2002-01-24 | 2005-06-01 | 环球油品公司 | Technique of separating fine particulates from gas steam |
| CN101301640A (en) * | 2007-05-11 | 2008-11-12 | 中国石油化工集团公司 | Cyclone separating device and uses thereof |
| CN101862165A (en) * | 2009-04-20 | 2010-10-20 | 马吉 | Multistage cyclone separation device of dust collector |
| CN202506375U (en) * | 2012-04-19 | 2012-10-31 | 李小燕 | Fluidized bed reactor with predissociation facility |
| CN103623943A (en) * | 2013-09-18 | 2014-03-12 | 中国石油大学(北京) | High-temperature high-pressure cyclone separator |
| CN107349733A (en) * | 2017-08-09 | 2017-11-17 | 国电科学技术研究院 | A kind of dust collecting system and method for carbon base catalyst desulfuring and denitrifying apparatus |
| KR101803239B1 (en) * | 2017-06-23 | 2017-11-29 | 조석현 | Fine dust removing apparatus |
| CN211676949U (en) * | 2019-12-27 | 2020-10-16 | 中国石油大学(北京) | Multi-pipe cyclone separator underflow gas-solid separation device |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US7115157B2 (en) * | 2004-02-27 | 2006-10-03 | Tronox, Llc | Gas separation apparatus and methods |
-
2019
- 2019-12-27 CN CN201911375108.8A patent/CN113041759B/en active Active
Patent Citations (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1622860A (en) * | 2002-01-24 | 2005-06-01 | 环球油品公司 | Technique of separating fine particulates from gas steam |
| CN101301640A (en) * | 2007-05-11 | 2008-11-12 | 中国石油化工集团公司 | Cyclone separating device and uses thereof |
| CN101862165A (en) * | 2009-04-20 | 2010-10-20 | 马吉 | Multistage cyclone separation device of dust collector |
| CN202506375U (en) * | 2012-04-19 | 2012-10-31 | 李小燕 | Fluidized bed reactor with predissociation facility |
| CN103623943A (en) * | 2013-09-18 | 2014-03-12 | 中国石油大学(北京) | High-temperature high-pressure cyclone separator |
| KR101803239B1 (en) * | 2017-06-23 | 2017-11-29 | 조석현 | Fine dust removing apparatus |
| CN107349733A (en) * | 2017-08-09 | 2017-11-17 | 国电科学技术研究院 | A kind of dust collecting system and method for carbon base catalyst desulfuring and denitrifying apparatus |
| CN211676949U (en) * | 2019-12-27 | 2020-10-16 | 中国石油大学(北京) | Multi-pipe cyclone separator underflow gas-solid separation device |
Also Published As
| Publication number | Publication date |
|---|---|
| CN113041759A (en) | 2021-06-29 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US7547427B2 (en) | Multiple stage separator vessel | |
| US8470081B2 (en) | Process for separating particulate solids from a gas stream | |
| EP2131939B1 (en) | Filter apparatus and method | |
| US8398751B2 (en) | Direct stripping cyclone | |
| CN107107014B (en) | Particle separation catalytic chemical reactor and particle separator | |
| US20100012595A1 (en) | Direct Stripping Cyclone | |
| RU2444408C2 (en) | Intake system for cracking installation with fluid catalyst, two tubes and upflow | |
| CN211676949U (en) | Multi-pipe cyclone separator underflow gas-solid separation device | |
| JP3308543B2 (en) | Fluidized bed catalytic cracker with third vortex separator | |
| CN113041759B (en) | Bottom flow gas-solid separation method and device for multitube cyclone separator | |
| CN201304370Y (en) | Riser type third stage cyclone separator | |
| CN201333367Y (en) | Complex fly ash filter with cyclone inside for pre dust removal | |
| CN204148014U (en) | A kind of large flux high temperature dusty gas cyclone separator with pressure | |
| CN201132137Y (en) | Horizontal tube type third stage cyclone separating device | |
| CN201283319Y (en) | Vertical tube type third cyclone separator with predissociation device | |
| CN202724947U (en) | Dust collection device for coarse titanium tetrachloride production | |
| CN101658750B (en) | Composite flyash filter with built-in cyclone pre-dusting | |
| CN2568308Y (en) | Riser type No.3 stage cyclone separator | |
| CN209092956U (en) | A kind of hot precipitator using flowable particle filter layer dedusting | |
| CN209917539U (en) | Rotating bed reactor | |
| CN202289785U (en) | Rotating particle layer dedusting device for high temperature oil gas | |
| JP2019537661A (en) | Product gas filter with filter candle and zeolite supply | |
| CN216808715U (en) | Compound dust pelletizing system of efficient pyrolysis gas | |
| CN108070399A (en) | Fluidized-bed reactor and its application and the method for hydrocarbon ils absorption desulfurization | |
| CN115178017A (en) | Dust remover |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |