CN211097980U - Continuous gas-solid filtering device - Google Patents
Continuous gas-solid filtering device Download PDFInfo
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- CN211097980U CN211097980U CN201921896600.5U CN201921896600U CN211097980U CN 211097980 U CN211097980 U CN 211097980U CN 201921896600 U CN201921896600 U CN 201921896600U CN 211097980 U CN211097980 U CN 211097980U
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Abstract
The utility model discloses a continuous gas-solid filtering device, which comprises at least 2 filters and a buffer tank; the lower side of any filter is provided with a gas inlet before filtration; the upper side of any filter is provided with a filtered gas outlet; the bottom of any filter is provided with an ash discharge port; the lower side of any filter is provided with a back-blowing outlet which is used for being communicated with a back-blowing inlet of the buffer tank; the top of the buffer tank is communicated with an inlet of a vacuum pump through a dust remover, and an outlet of the vacuum pump is connected to a pre-filtering gas inlet pipeline communicated with a pre-filtering gas inlet. And, a continuous drum filtration process is accordingly provided. The utility model discloses the device can avoid the secondary raise dust of blowback in-process, reduces the extreme load of filter media, when realizing the long periodic motion of filter equipment, reduces the investment, and can not introduce blowback gaseous impurities, greatly increased the filterable application of gas-solid.
Description
Technical Field
The utility model belongs to the technical field of the gas-solid separation, concretely relates to continuous gas-solid filter equipment.
Background
Gas-solid filtration separation refers to a method for separating and purifying a mixed gas containing solids with dispersion or coagulation properties, and is an important chemical unit operation. The method is widely applied to the fields of petrochemical industry, coal burning, electric power, metallurgy, cement, textile, environmental protection and the like.
At present, there are many gas-solid separation methods in industry to filter and separate dusty gas to purify industrial gas or recycle valuable resources, mainly including: the gravity settling method has the advantages that the gravity settling device has simple structure and low cost, but the gas velocity is low, the equipment is large, and only coarse particles with the particle size of more than 100 mu m can be separated; the washing and separating method has small equipment floor area, low investment and is suitable for treating gas containing harmful substances, but the method needs washing liquid, so the method can only be used at lower temperature, and needs a liquid recovery and circulation system, so the application is greatly limited; the electric dust removal method has good separation efficiency on particles with the particle size of 0.01-1 mu m, but requires that the specific resistance value of the particles is 104-5×1010Omega cm, the cost of separation equipment is high, and the requirements of operation management are high; the bag type filtering method has the advantages of higher filtering efficiency, simple equipment and low cost, but the service life of the filtering bag is shorter, and the filtering bag cannot be directly applied to filtering high-temperature dust-containing gas and is only suitable for low-temperature occasions; the metal filter element material filtering method has the advantages of high filtering efficiency, simple equipment, adaptability to different working conditions, low manufacturing cost, long service life and wide application prospect at present.
In the filtering process of the metal filter element filter, dust-containing gas enters from the lower part of the filter and flows upwards through the filter element, solid particles are intercepted on the outer surface of the filter element under the filtering action of the filter element, and after being filtered, clean gas is desorbed from the inner surface of the filter element and then is discharged from the upper part of the filter. When the filter cake on the surface of the filter element reaches a certain thickness, the filter element needs to be subjected to online back flushing, compressed air enters from a top subarea of the filter by sequentially controlling a plurality of groups of back flushing valves, and is accelerated by an accelerator and then blown from the inner surface to the outer surface of the filter element, so that the filter cake on the outer surface of the filter element is separated from the surface of the filter element under the action of instantaneous reverse pressure difference, and the pressure difference between the inside and the outside of the filter element is recovered, thereby completing regeneration. The principle is schematically shown in the utility model of figure 1.
However, in the filtering mode, the back-flushing valves are grouped to perform on-line back flushing on the filter elements, a large number of valves and back-flushing pipelines are needed, the investment of a filtering system is increased, the grouped back flushing is performed in the same filter, the residual groups are still filtered while one group of filter elements perform back flushing, and filtered gas can drive filter cake dust subjected to back flushing to form secondary dust. Especially, when processing the process gas, the blowback gas often becomes the impurity of the process gas, often limiting its application.
At present, a plurality of patents related to online back-blowing of gas filtration exist, for example, chinese patent document CN201420191303.1 discloses a gas filter and a filter element back-blowing device of the gas filter, which uses ultrasonic waves to back-blow the filter element; chinese patent document CN201420152145.9 proposes a scheme of manually performing blowback on a filter element by using an air injection pipeline for a special filter element ash removal device for a gas filtration dust remover, but the scheme requires the filter to be offline and manual operation, which increases labor cost. Chinese patent document cn201910014402.x discloses an automatic ash removal filter element dust remover, and proposes to use a control system to control a back-flushing valve corresponding to each filter element, so as to increase the back-flushing effect, but a large number of back-flushing valves need to be added. Chinese patent document CN201910014403.4 discloses a filter element dust remover with low use cost and automatic ash removal, and proposes that a piston is used for closing an air outlet hole of a filter element, and then a back-blowing valve is opened for back-blowing the filter element, so that the filter element dust remover does not interfere with the filtration of other groups of filter elements during back-blowing; but also requires a large number of blow-back valves.
Therefore, in order to reduce the investment of the filtration system and optimize the back-blowing process of the filter element, the technical personnel in the field need to provide a continuous gas-solid filtration device which can avoid introducing back-blowing gas impurities and secondary dust, and ensure that the purpose of continuous online operation of the filter is achieved under the condition of less investment.
Disclosure of Invention
The utility model aims at providing a can avoid introducing the continuous gas-solid filter equipment of blowback gas impurity and secondary raise dust, guarantee under the less condition of investment, reach the purpose of the continuous long period continuous operation of filter.
The utility model provides a technical scheme as follows:
a continuous gas-solid filtering device comprises at least 2 filters and a buffer tank;
the lower side of any filter is provided with a gas inlet before filtration; the upper side of any filter is provided with a filtered gas outlet; the bottom of any filter is provided with an ash discharge port;
the lower side of any filter is provided with a back-blowing outlet which is used for being communicated with a back-blowing inlet of the buffer tank; the top of the buffer tank is communicated with an inlet of a vacuum pump through a dust remover, and an outlet of the vacuum pump is connected to a pre-filtering gas inlet pipeline communicated with a pre-filtering gas inlet.
Preferably, the pre-filtered gas inlet is communicated with a pre-filtered gas inlet pipeline through an air inlet valve;
the filtered gas outlet is communicated with a filtered gas outlet pipeline through a gas outlet valve;
the back-blowing gas outlet is communicated with a back-blowing gas pipeline through a back-blowing valve, and the back-blowing gas pipeline is communicated with a back-blowing gas inlet on the buffer tank;
and the outlet of the vacuum pump is connected to a pre-filtering gas inlet pipeline through a circulating exhaust valve.
Furthermore, the filter comprises a shell and a filter element positioned in the middle of the shell, and the filter element is fixed on the inner wall of the shell through a tube plate;
the bottom of the filter is provided with a conical ash bucket for collecting, storing and filtering solid particles, and an ash discharge valve is arranged at an ash discharge port at the bottom of the ash bucket.
Furthermore, the bottom of the buffer tank is conical and is provided with an ash discharge port, and the ash discharge port is provided with an ash discharge valve.
Further, the pre-filtered gas inlet of the filter is located on the side wall below the tube sheet; the filtered gas outlet of the filter is located on the sidewall above the tube sheet.
Furthermore, a pre-filtering gas inlet of the filter is positioned 200-500 mm above the ash bucket.
Furthermore, a back-blowing outlet of the filter is positioned 200-500 mm above the ash bucket.
Furthermore, the distance between the back-blowing inlet of the buffer tank and the bottom of the side wall of the buffer tank is 500-1000 mm.
And the air inlet valve, the air outlet valve, the back flushing valve, the vacuum pump, the circulating exhaust valve and the ash discharge valve are all electrically connected with the control system.
Further, the control system adopts a P L C control system or a DCS control system, and/or,
and the air inlet valve, the air outlet valve, the back flushing valve, the circulating exhaust valve and the ash discharge valve are all self-control valves.
Utilize the utility model discloses the device can also provide a continuous gas-solid filtration technology, include following step:
s1, allowing dust-containing gas to enter from the lower parts of the filters in parallel, allowing the dust-containing gas to flow upwards through the filter elements, intercepting solid particles on the outer surfaces of the filter elements under the filtering action of the filter elements, and discharging the filtered clean gas from the upper parts of the filters after the clean gas is desorbed from the inner surfaces of the filter elements to realize gas-solid separation; collecting and storing the filtered solid particles in an ash bucket at the lower part of the filter;
in the process of filtering and separating, a vacuum pump is started to vacuumize the buffer tank, and after the gas in the buffer tank is pumped out by the vacuum pump after dust is removed by a dust remover on the top, the gas enters a gas inlet pipeline before filtering through a circulating exhaust valve to be mixed with the gas before filtering, and the dust is filtered and collected again; when the vacuum degree of the buffer tank meets the requirement, closing the vacuum pump and the circulating exhaust valve, and keeping the buffer tank in vacuum for later use;
s2, when the filter runs for a set time or a set pressure difference, closing an air inlet valve and an air outlet valve of one filter, quickly opening a back-flushing valve between a buffer tank and the filter, instantly enabling the filter to be in a reverse pressure difference state, enabling filtered air in the filter to reversely flow to the outer surface through the inner surface of the filter element under the action of the reverse pressure difference, sucking the filtered air into the buffer tank, stripping a filter cake on the outer surface of the filter element from the outer surface of the filter element under the action of the instantaneous reverse pressure difference or the back-flushing action, and recovering the pressure difference between the inside and the outside of the filter element; the filter cake dust falls into the ash bucket under the action of gravity, a small amount of dust is sucked into the buffer tank along with the back flushing gas, and the dust carried by the back flushing gas can settle into the ash bucket at the bottom of the buffer tank after the back flushing gas enters the buffer tank;
s3, repeating the step S1 to vacuumize the buffer tank, and repeating the step S2 to perform online ash removal on another filter; continuously circulating, and alternately realizing the ash removal and regeneration of a plurality of filters;
in the above steps, the solid particles collected and stored in the ash hopper are discharged periodically through an ash discharge valve; dust in the buffer tank is collected at the cone bottom, and is discharged out of the system through the dust discharge valve before the buffer tank is vacuumized each time.
Preferably, the pressure of the buffer tank for vacuum standby is controlled to be below 0.005 MpaA.
Preferably, in step S2, after the blowback valve between the buffer tank and the filter is opened rapidly, the blowback duration is controlled to be 1-5S.
The utility model discloses can bring following beneficial effect:
1) the utility model can realize the simultaneous filtration of a plurality of filters by connecting a plurality of filters with the buffer tank in parallel, and can vacuumize the buffer tank for standby by utilizing the matching of the buffer tank and the vacuum pump; because the back-blowing outlet of the filter is communicated with the back-blowing inlet of the buffer tank, the vacuum environment in the buffer tank can enable the filter to form reverse pressure difference, filtered purified gas in the filter is back-blown (as back-blowing gas) and is sucked into the buffer tank through the inner surface and the outer surface of the filter element, and a filter cake on the outer surface of the filter element is peeled from the outer surface of the filter element under the action of the reverse pressure difference or the back-blowing, so that the regeneration of the filter is realized; specifically, reverse pressure difference is formed on the two sides of the inlet and the outlet of the filter element under the action of vacuum, and then filtered clean gas is driven to perform online ash removal on the filter element, so that online continuous operation of the filter element is ensured. Therefore, the utility model discloses utilize and strain the back gas and carry out reverse effort to the filter core and carry out the deashing of filter core, gaseous carrying out integral blowback to the filter through purifying the back, the blowback is quick, can not arouse in the blowback operation dust by the secondary pollution to the filter core. On the other hand, the blowback gas pumped into the buffer tank returns to the filter for re-filtration through the dust remover and the exhaust valve, and impurity pollutants are not introduced due to different components of the blowback gas and the filtered gas. And the design that a plurality of filters are connected in parallel can ensure that the whole device is always in a filtering operation state by carrying out back flushing regeneration on each filter in turn, thereby realizing the long-period operation of the filtering device.
2) The utility model discloses compare with current dust removal technique, the cooperation through buffer tank and vacuum pump can replace the huge blowback valve of quantity among these prior art, and the small investment is convenient for maintain, has improved the reliable and stable nature of operation.
3) High temperature to often meeting in the practical application filters, the utility model discloses owing to adopt the purification gas blowback after straining, can not arouse the temperature reduction, need not to consume energy heating blowback gas, further energy-conserving this reduction, and safer.
To sum up, the utility model discloses the device can avoid the secondary raise dust of blowback in-process, reduces the extreme load of filter media, when realizing the long period operation of filter equipment, reduces the investment, and can not introduce blowback gaseous impurities, greatly increased the filterable application of gas-solid.
Drawings
Fig. 1(a, b) is a schematic diagram of the filtration and back-blowing of a filter in the prior art.
Fig. 2 is a schematic structural diagram of a specific embodiment of the continuous gas-solid filtering device of the present invention.
Fig. 3 is a schematic structural diagram of the filter of the present invention.
The notations in the figures have the following meanings:
1(A, B) -filter, 10-shell, 11-filter element, 12-tube plate, 13-ash bucket, 14(A, B) -ash discharge valve I;
2-a buffer tank and 20-an ash discharge valve II;
3-a dust remover; 4-a vacuum pump;
5-pre-filtered gas inlet line, 50(A, B) -inlet valve, 51-cycle exhaust valve;
6-filtered gas outlet line, 60(A, B) -outlet valve;
7-blowback gas line, 70(A, B) -blowback valve;
8-control the system.
Detailed Description
The technical solution of the present invention will be clearly and completely described below with reference to the specific embodiments. The following examples are only for illustrating the technical solutions of the present invention more clearly, and the protection scope of the present invention is not limited thereby.
Example 1
As shown in FIG. 2, the continuous gas-solid filtering device comprises at least 2 filters 1 and a buffer tank 2;
the lower side of any filter 1 is provided with a gas inlet before filtration; the upper side of any filter 1 is provided with a filtered gas outlet; the bottom of any filter 1 is provided with an ash discharge port;
the lower side of any filter is provided with a back-blowing outlet which is used for being communicated with a back-blowing inlet of the buffer tank 2; the top of the buffer tank 2 is communicated with the inlet of a vacuum pump 4 through a dust remover 3, and the outlet of the vacuum pump 4 is connected to a pre-filtering gas inlet pipeline 5 communicated with a pre-filtering gas inlet.
In the embodiment, the plurality of filters are connected with the buffer tank in parallel, so that the plurality of filters can filter simultaneously, and the buffer tank can be vacuumized for later use by matching the buffer tank with the vacuum pump; because the blowback export of filter and the blowback entry intercommunication of buffer tank, the vacuum environment in the buffer tank can make the filter form reverse pressure difference in the twinkling of an eye, and then makes the interior back-flushing (as blowback gas) of the post-filtration purified gas blowback of filter, through filter core internal surface, surface and in being sucked to the buffer tank, the filter cake of filter core surface is under reverse pressure difference or blowback effect, peels off with the filter core surface, realizes the regeneration to the filter. Therefore, the utility model discloses utilize and purify the back gas and carry out integral blowback to the filter, the blowback is quick, can not arouse in the blowback operation dust by the secondary pollution to the filter core. In addition, the back-blowing gas pumped into the buffer tank is back blown into the filter for re-filtering through the dust remover and the exhaust valve, so that impurity pollutants cannot be introduced due to different components of the back-blowing gas and the filtering gas. And the design that a plurality of filters are connected in parallel can ensure that the whole device is always in a filtering operation state by carrying out back flushing regeneration on each filter in turn, thereby realizing the long-period operation of the filtering device. By the foregoing, through the utility model discloses the numerous blowback valve of quantity among the prior art can be replaced to the cooperation of buffer tank and vacuum pump among the filter equipment, and the small investment is convenient for maintain. Wherein, the setting of buffer tank top intercommunication dust remover 3 can reduce the vacuum pump 4 suction time, and the dust is to the wearing and tearing that the 4 blades of vacuum pump caused.
As a preferred embodiment, the pre-filtered gas inlet communicates with the pre-filtered gas inlet conduit 5 through an inlet valve 50; the filtered gas outlet is communicated 6 with a filtered gas outlet pipeline through a gas outlet valve 60; the back-blowing gas outlet is communicated with a back-blowing gas pipeline 7 through a back-blowing valve 70, and the back-blowing gas pipeline 7 is communicated with a back-blowing gas inlet on the buffer tank 2; the outlet of the vacuum pump 4 is connected in communication with a pre-filtered gas inlet line 5 through a recycle exhaust valve 51.
In the embodiment, the filter recirculates to the pre-filter gas inlet of the filter through the back-flushing gas pipeline, the buffer tank, the vacuum pump, the circulating exhaust valve and the pre-filter gas inlet pipeline which are connected with the back-flushing gas outlet, so that the back-flushing gas in the filter can be used as the back-flushing gas to carry out integral back-flushing on the filter, and the back-flushing gas pumped into the buffer tank is circulated and returned to the filter for re-filtering, so that the integral circulating suction back-flushing and filtering of the filter are formed, and other gas impurities are prevented from being introduced into the gas to be filtered; is particularly suitable for the field of process gas filtration.
Preferably, as shown in fig. 3, the filter 1 includes a housing 10 and a filter element 11 located in the middle of the housing 10, wherein the filter element 11 is fixed on the inner wall of the housing 10 by a tube plate 12; the bottom of the filter is provided with a conical ash bucket 13 for collecting and storing filtered solid particles, and an ash discharge valve I14 is arranged at an ash discharge port at the bottom of the ash bucket 13.
Preferably, the bottom of the buffer tank 2 is conical and is provided with an ash discharge port, and the ash discharge port is provided with an ash discharge valve II 20.
Preferably, the device also comprises a control system 8, wherein the air inlet valve 50, the air outlet valve 60, the blowback valve 70, the vacuum pump 4, the circulating exhaust valve 51, the ash discharge valve I14 and the ash discharge valve II 20 are all electrically connected with the control system, preferably, the control system adopts a P L C control system or a DCS control system, and more preferably, the air inlet valve 40, the air outlet valve 50, the blowback valve 60, the circulating exhaust valve 51, the ash discharge valve I14 and the ash discharge valve II 20 all adopt self-control valves.
It should be noted that the control system 8 is the prior art, the P L C control system is a new generation industrial control device formed by introducing micro-electronic technology, computer technology, automatic control technology and communication technology on the basis of the traditional sequence controller, and aims to replace the sequential control functions of relays, execution logic, timing, counting and the like, and a flexible remote control system is established, the DCS control system is a new generation control system which is based on a microprocessor and adopts the design of distributed control functions, centralized display operation, automatic control and comprehensive coordination, concretely, the P L C control system can select Siemens S7-1200 or S7-1500 series P L C, the DCS control system can select Zheda middle control JX-300 or ESC-700 system, Yanghe NTCEVP or CENTUM CS system, the Honeville S300-300 series P L C, and the corresponding opening and closing control system can also be set by using other corresponding program control procedures of the corresponding PSK L control system.
As another preferable embodiment, the volume of the buffer tank 2 is 1.5-3 times of the volume of the filter 1, so as to ensure the dust removal effect.
Preferably, the filter element is made of metal or polymer, the filtering precision is micron grade, and the filter element is made of related products sold in the market. In practical application, the filtering precision of the filter element can be adjusted according to the required treatment condition, and if the filtering precision is 0.3-1 μm, the filtering precision can be selected.
Preferably, the pre-filtration gas inlet of the filter 1 is located on the side wall below the tube sheet 12; the filtered gas outlet of the filter 1 is located on the side wall above the tube sheet 12.
Preferably, the gas inlet before filtration of the filter 1 is positioned 200-500 mm above the ash bucket 13; so as to reduce the dust entrainment in the back flushing process. Preferably, the back-blowing outlet of the filter 1 is positioned 200-500 mm above the ash bucket; so as to reduce the dust entrainment in the back flushing process. It should be noted that, in practical applications, in order to improve the sealing performance of the filter and reduce the number of openings as much as possible, the pre-filtration gas inlet and the back-blowing gas outlet are combined into one.
As another preferred embodiment, the distance between the back-blowing air inlet of the buffer tank 2 and the bottom of the side wall of the buffer tank 2 is 500-1000 mm, so that dust in air can be conveniently settled.
Example 2
Referring to fig. 2, this embodiment is a continuous gas-solid filtering process, which is characterized by comprising the following steps:
s1, allowing dust-containing gas to enter from the lower parts of the filters 1 in parallel, allowing the dust-containing gas to flow upwards through the filter element 11, intercepting solid particles on the outer surface of the filter element 11 under the filtering action of the filter element 11, and discharging the filtered clean gas from the upper part of the filter 1 after being desorbed from the inner surface of the filter element 11 to realize gas-solid separation; the filtered solid particles are collected and stored in an ash hopper 13 at the lower part of the filter 1;
in the process of filtering and separating, a vacuum pump 4 is started to vacuumize the buffer tank 2, the gas in the buffer tank 2 is pumped out by the vacuum pump 4 after dust is removed by a dust remover 3 at the top, and then enters a gas inlet pipeline 5 before filtering through a circulating exhaust valve 51 to be mixed with the gas before filtering, and the dust is filtered again; when the vacuum degree of the buffer tank 2 meets the requirement, the vacuum pump 4 and the circulating exhaust valve 51 are closed, and the buffer tank 2 is in vacuum for standby;
s2, after the filter cake on the surface of the filter element of the filter 1 reaches a certain thickness or the filter runs for a set pressure difference or set time, closing the air inlet valve 50 and the air outlet valve 60 of one of the filters, quickly opening the back flushing valve 60 between the buffer tank 2 and the filter 1, instantly enabling the filter 1 to be in a reverse pressure difference state, enabling the filtered gas in the filter to reversely flow to the outer surface through the inner surface of the filter element under the action of the reverse pressure difference, and pumping the filtered gas into the buffer tank, enabling the filter cake on the outer surface of the filter element 11 to be stripped from the outer surface of the filter element 11 under the action of the instantaneous reverse pressure difference or the back flushing, and recovering the pressure difference; in the process, the filter cake dust falls into the ash hopper 13 under the action of gravity; meanwhile, a small amount of dust is sucked into the buffer tank 2 along with the back flushing gas, and after the back flushing gas enters the buffer tank 2, the entrained dust can settle into an ash hopper at the bottom of the buffer tank;
s3, repeating the step S1 to vacuumize the buffer tank 2, and repeating the step S2 to perform online ash removal on another filter 1; continuously circulating, and alternately realizing the ash removal and regeneration of the plurality of filters 1;
in the above step, the solid particles collected and stored in the ash hopper 13 are periodically discharged through an ash discharge valve I14; dust in the buffer tank 2 is collected at the cone bottom, and is discharged out of the system through an ash discharge valve II 20 before the buffer tank 2 is vacuumized each time.
The utility model provides an innovative online back flushing process, which firstly vacuumizes the inside of a buffer tank for standby through the matching of the buffer tank and a vacuum pump; then, an instant reverse pressure difference is formed in the filter by utilizing the vacuum environment in the buffer tank, so that filtered purified gas in the filter is blown back (as back blowing gas) and is sucked into the buffer tank through the inner surface and the outer surface of the filter element, and a filter cake on the outer surface of the filter element is peeled from the outer surface of the filter element under the action of the reverse pressure difference or the back blowing, so that the regeneration of the filter is realized; therefore, the utility model discloses utilize and purify the back gas and carry out integral blowback to the filter, the blowback is quick, can not arouse in the blowback operation dust by the secondary pollution to the filter core. In addition, the back-blowing gas pumped into the buffer tank is back blown into the filter for re-filtering through the dust remover and the exhaust valve, so that impurity pollutants cannot be introduced due to different components of the back-blowing gas and the filtering gas. And for a plurality of filters which are filtered in parallel, back flushing regeneration can be carried out in turn according to the sequence, and the continuity and reliability of the process operation are ensured. In practical application, all valves related in the process are self-control valves and are electrically connected with the control system 8, so that the operation efficiency can be improved by combining the control system in the prior art, and the long-period continuous online filtration is realized.
As a preferred embodiment, the pressure of the vacuum reserve of the buffer tank 2 is controlled below 0.005MpaA, wherein the unit symbol MpaA represents the absolute pressure, in order to ensure the back-flushing effect on the filter 1.
As another preferred embodiment, in step S2, after the blowback valve 60 between the buffer tank 2 and the filter 1 is opened rapidly, the blowback duration is controlled to be 1-5S. That is, the time that the buffer tank 2 is in a vacuum state and sucks the filtered gas in the filter 1 is kept for 1-5 s, and if the time is smaller than the range, the back flushing effect is poor, and if the time is longer than the range, the back flushing effect cannot be increased.
Comparative example 1
The gas before filtering (raw material) is coal gas:
the components are CO: 23.8 vol% and CO2：15.91vol％、H2：29.15vol％、H2O：24.98vol％、CH4: 2.55 vol% and a small amount of H2S；
The temperature is 240 ℃; pressure 0.3 MPaA;
air volume 30000Nm3H; the dust content was 100g/Nm3。
The device and the process are as follows:
adopts the conventional filtration process and device of the internal grouping gas-solid filtration (similar to figure 1) of a single filter and the introduction of external back-blowing gas. The device comprises the following components: two filters, a back flushing tank and a back flushing heater. Wherein the filtering precision of the filter element in the filter is 1 μm.
In order to reduce the gas consumption at the moment of back flushing, each filter is divided into 12 subareas (corresponding to 12 back flushing valves); in order to avoid explosion risks, compressed nitrogen is used as back-flushing gas; in order to avoid low temperature nitrogen entering the system, causing a temperature drop inside the filter, dew point corrosion and filter cake pockets, a 20KW heater was used to heat the nitrogen to above 120 ℃.
The device has the following purification effects:
the average dust content of the purified gas is 90-100 mg/Nm3. The proportion of nitrogen in the purge gas is slightly increased, resulting in a slight decrease in the calorific value of the purge gas compared to the feedstock due to the introduction of the inert gas nitrogen.
Consumption of the device:
average consumption of nitrogen gas of 50Nm3H, average power consumption: 5 kw.
Application example 1
The pre-filtered gas (feed) was the same as in comparative example 1.
The device and the process are as follows:
adopt the utility model discloses the continuous gas-solid filter equipment who contains two filters that fig. 2 is shown can avoid introducing blowback gas impurity and secondary raise dust, and the filter is inside not subregion. Wherein, the filter precision of the filter element is the same as that of the comparative example 1. It should be noted that the apparatus used in this example is 2 filters based on the overall structure provided in example 1, and therefore, detailed descriptions of the specific structure of the apparatus in this example are not repeated here.
Specifically, the steps of filtering the raw material by using the device as shown in fig. 2 are as follows:
s1, enabling dust-containing gas to enter from the lower part of 2 filters 1A/1B in parallel, enabling the dust-containing gas to flow upwards through the filter element 11, intercepting solid particles on the outer surface of the filter element 11 through the filtering action of the filter element 11, and discharging the filtered clean gas from the upper part of the filter 1 through the gas outlet valve 60A/60B after the filtered clean gas is desorbed from the inner surface of the filter element 11, so that gas-solid separation is realized; the filtered solid particles are collected and stored in an ash hopper 13 at the lower part of the filter 1;
in the process of filtering and separating, a vacuum pump 4 is started to vacuumize the buffer tank 2, the gas in the buffer tank 2 is pumped out by the vacuum pump 4 after dust is removed by a dust remover 3 at the top, and then enters a gas inlet pipeline 5 before filtering through a circulating exhaust valve 51 to be mixed with the gas before filtering, and the dust is filtered again; when the vacuum degree of the buffer tank 2 meets the requirement, the vacuum pump 4 and the circulating exhaust valve 51 are closed, and the buffer tank 2 is in vacuum for standby;
s2, when the filter cake on the surface of the filter element of the filter 1 reaches the set pressure difference of 0.01MPa, closing the air inlet valve 50A and the air outlet valve 60A of the filter 1A, quickly opening the back-flushing valve 60A between the buffer tank 2 and the filter 1A, instantly making the filter 1A in a reverse pressure difference state, making the filtered gas in the filter 1A start back-flushing under the action of the reverse pressure difference, reversely flowing towards the outer surface through the inner surface of the filter element 11 and being sucked into the buffer tank 2, and stripping the filter cake on the outer surface of the filter element 11 from the outer surface of the filter element 11 under the action of the instant reverse pressure difference or the back-flushing, so that the pressure difference between the inside; in the process, the filter cake dust falls into the ash hopper 13 under the action of gravity; meanwhile, a small amount of dust is sucked into the buffer tank 2 along with the back-blowing gas; after the back-blowing gas enters the buffer tank 2, the entrained dust can settle and enter an ash hopper at the bottom of the buffer tank 2;
s3, closing the blowback valve 60A, opening the air inlet valve 50A and the air outlet valve 60A, recovering the filtration of the filter 1A, repeating the step S1 to vacuumize the buffer tank 2, and then performing online ash removal on the other filter 1B with reference to the step S2; continuously circulating, and alternately realizing the ash removal, regeneration and filtration of the plurality of filters 1;
in the treatment step, the solid particles collected and stored in the ash hopper 13 are periodically discharged through an ash discharge valve I14; dust in the buffer tank 2 is collected at the cone bottom, and is discharged out of the system through an ash discharge valve II 20 before the buffer tank 2 is vacuumized each time.
The device has the following purification effects:
the average dust content of the purified gas is 50-60 mg/Nm3. The composition of the other components in the purge gas is kept constant compared to the feedstock and the heating value of the purge gas is constant compared to the feedstock.
Consumption of the device:
average consumption of nitrogen gas of 0Nm3H, average power consumption: 0.5 kw.
It shows, the utility model discloses device purifying effect is obviously superior to traditional gas-solid filtration technique, and the analysis main cause has avoided blowback and filtration to carry out the secondary raise dust pollution that leads to simultaneously through the cooperation of filter, buffer tank and vacuum pump, circulation discharge valve etc. has reduced the penetration phenomenon of filtering the initial stage, and the average dust content of purified gas reduces obviously. Secondly, since no heating of the blow-back gas is required, the energy consumption of the device is less than 1/40 of that of comparative example 1. No additional consumption of nitrogen is required. In addition, the present apparatus reduces the number of valves by about 20 compared to the conventional apparatus, and does not require an additional control system or program for the blowback temperature.
Comparative example 2
The gas (raw material) before filtration is propane dehydrogenation regeneration flue gas:
the component is CO2、H2O、N2、O2(ii) a The temperature is 300 ℃; micro-positive pressure: 5KPa (g); gas quantity: 21000Nm3H; dust content: 1g/Nm3。
The device and the process are as follows:
the filter precision of the filter element is 0.3 μm, and the other parts are basically the same as the comparative example 1, except that the back blowing gas is compressed air; the power of the back-blowing heater is 30KW, and the back-blowing heater heats the back-blowing air to above 150 ℃.
The device has the following purification effects:
the average dust content of the purified gas is less than 10mg/Nm3。
Consumption of the device:
average compressed air consumption of 20Nm3H, average power consumption: 7 kw.
Application example 2
The pre-filtered gas (feed) was the same as in comparative example 2.
The device and the process are as follows:
the same as in application example 1 was applied, except that the filtration accuracy of the filter element of the filter in the apparatus was the same as in comparative example 2.
The device has the following purification effects:
the average dust content of the purified gas is less than 5mg/Nm3。
Consumption of the device: average compressed air consumption of 0Nm3H, average power consumption: 0.5 kw.
It shows, the utility model discloses device purifying effect is obviously superior to traditional gas-solid filtration technique, and the analysis main cause has avoided blowback and filtration to carry out the secondary raise dust pollution that leads to simultaneously through the cooperation of filter, buffer tank and vacuum pump, circulation discharge valve etc. has reduced the penetration phenomenon of filtering the initial stage, and the average dust content of purified gas reduces obviously. Secondly, since no heating of the blow-back gas is required, the energy consumption of the device is less than 1/60 of the energy consumption of comparative example 2. And no additional consumption of compressed air is required. In addition, the present apparatus reduces the number of valves by about 20 compared to the conventional apparatus, and does not require an additional control system or program for the blowback temperature.
It should be noted that the above embodiments can be freely combined as necessary. The foregoing is only a preferred embodiment of the present invention, and it should be noted that, for those skilled in the art, a plurality of modifications and decorations can be made without departing from the principle of the present invention, and these modifications and decorations should also be regarded as the protection scope of the present invention.
Claims (10)
1. A continuous gas-solid filtration device, characterized in that:
comprises at least 2 filters and a buffer tank;
the lower side of any filter is provided with a gas inlet before filtration; the upper side of any filter is provided with a filtered gas outlet; the bottom of any filter is provided with an ash discharge port;
the lower side of any filter is provided with a back-blowing outlet which is used for being communicated with a back-blowing inlet of the buffer tank; the top of the buffer tank is communicated with an inlet of a vacuum pump through a dust remover, and an outlet of the vacuum pump is connected to a pre-filtering gas inlet pipeline communicated with a pre-filtering gas inlet.
2. The continuous gas-solid filtration device of claim 1, wherein:
the pre-filtering gas inlet is communicated with a pre-filtering gas inlet pipeline through a gas inlet valve;
the filtered gas outlet is communicated with a filtered gas outlet pipeline through a gas outlet valve;
the back-blowing gas outlet is communicated with a back-blowing gas pipeline through a back-blowing valve, and the back-blowing gas pipeline is communicated with a back-blowing gas inlet on the buffer tank;
and the outlet of the vacuum pump is connected to a pre-filtering gas inlet pipeline through a circulating exhaust valve.
3. The continuous gas-solid filtration device of claim 2, wherein:
the filter comprises a shell and a filter element positioned in the middle of the shell, and the filter element is fixed on the inner wall of the shell through a tube plate;
the bottom of the filter is provided with a conical ash bucket for collecting and storing filtered solid particles, and an ash discharge valve is arranged at an ash discharge port at the bottom of the ash bucket;
the bottom of the buffer tank is conical and is provided with an ash discharge port, and the ash discharge port is provided with an ash discharge valve.
4. A continuous gas-solid filtration device according to claim 3, wherein:
the pre-filtration gas inlet of the filter is positioned on the side wall below the tube plate; the filtered gas outlet of the filter is located on the sidewall above the tube sheet.
5. A continuous gas-solid filtration device according to claim 3, wherein:
a gas inlet before filtration of the filter is positioned 200-500 mm above the ash bucket; and/or the presence of a gas in the gas,
and a back-blowing air outlet of the filter is positioned 200-500 mm above the ash bucket.
6. The continuous gas-solid filtration device of claim 1, wherein:
the back-blowing air inlet of the buffer tank is 500-1000 mm away from the bottom of the side wall of the buffer tank.
7. A continuous gas-solid filtration device according to claim 3, wherein:
and the air inlet valve, the air outlet valve, the back flushing valve, the circulating exhaust valve and the ash discharge valve are all self-control valves.
8. Continuous gas-solid filtration device according to claim 3 or 7, characterized in that:
the device also comprises a control system, wherein the air inlet valve, the air outlet valve, the back flushing valve, the vacuum pump, the circulating exhaust valve and the ash discharge valve are all electrically connected with the control system.
9. The continuous gas-solid filtration device of claim 8, wherein:
the control system adopts a P L C control system or a DCS control system.
10. The continuous gas-solid filtration device of claim 1, wherein:
the pressure of the buffer tank for standby vacuum is controlled below 0.005 MpaA.
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| CN201921896600.5U CN211097980U (en) | 2019-11-06 | 2019-11-06 | Continuous gas-solid filtering device |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110665300A (en) * | 2019-11-06 | 2020-01-10 | 上海蓝科石化环保科技股份有限公司 | Continuous gas-solid filtering device and process |
| CN115253535A (en) * | 2022-08-08 | 2022-11-01 | 四川华能氢能科技有限公司 | A filter equipment for hydrogen is collected |
-
2019
- 2019-11-06 CN CN201921896600.5U patent/CN211097980U/en active Active
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110665300A (en) * | 2019-11-06 | 2020-01-10 | 上海蓝科石化环保科技股份有限公司 | Continuous gas-solid filtering device and process |
| CN115253535A (en) * | 2022-08-08 | 2022-11-01 | 四川华能氢能科技有限公司 | A filter equipment for hydrogen is collected |
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