CN212999197U - Gas-material separation device, activated carbon transportation system and adsorption and desorption system - Google Patents
Gas-material separation device, activated carbon transportation system and adsorption and desorption system Download PDFInfo
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- CN212999197U CN212999197U CN202021019349.7U CN202021019349U CN212999197U CN 212999197 U CN212999197 U CN 212999197U CN 202021019349 U CN202021019349 U CN 202021019349U CN 212999197 U CN212999197 U CN 212999197U
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Abstract
The utility model provides a gas material separator, active carbon transportation system and absorption analytic system, this gas material separator includes: the device comprises a box body, a feed inlet, an extraction opening, a discharge opening and a fluidizing device; the feed inlet is arranged at the upper end or the upper part of the side surface of the box body; the discharge port is arranged at the lower end of the box body; the air extraction opening is arranged on the box body; the feed inlet, the extraction opening and the discharge opening are communicated with the interior of the box body; the air suction port is communicated with an external negative pressure source through a negative pressure pipeline; the fluidization device is arranged in the box body, and the upper end of the fluidization device is communicated with the feed inlet; the lower end of the fluidizing device is communicated with the discharge hole. The technical scheme provided by the application can control the diameter of the activated carbon particles separated from the activated carbon discharged from the adsorption tower or the desorption tower, so that the activated carbon powder with large influence on the system can be accurately removed, and the service life of the equipment is prolonged.
Description
Technical Field
The utility model relates to a separator box, concretely relates to gas-material separator belongs to metal sintering technical field. The utility model discloses still relate to an active carbon conveying system independently bleeds. The utility model discloses still relate to a prevent that flue gas escape from adsorbing analytic system.
Background
The application of the existing activated carbon flue gas purification process gradually becomes the mainstream process of steel flue gas purification.
For a large-scale flue gas purification device, the adsorption tower and the desorption tower are both moving beds, and the active carbon is recycled between the adsorption tower and the desorption tower through a conveyor. Besides the activated carbon, part of leaked flue gas exists from the adsorption tower to the conveyor.
As shown in fig. 7, when the sintering flue gas passes through the activated carbon layer, due to the pressure difference, part of the flue gas enters the conveyor along with the activated carbon passing through the discharging device (which may be a round rod and a rotary valve, or only a rotary valve) of the adsorption tower, the flue gas has high water content, and corrosive liquid drops can be condensed in the conveyor to corrode the conveyor. The activated carbon conveyor is a key operation device in the flue gas purification device.
The prior art has the following disadvantages: when the air draft is insufficient, the flue gas sinks to the conveying equipment to corrode the conveying equipment; when the air pumping quantity is too large, the negative pressure of the air pumping opening is too large, and the flue gas can sink more due to the increase of the pressure difference, so that a dust removal system is influenced; because of differences such as equipment manufacturing, wearing and tearing, every point flue gas deflection is different, and the deflection can change along with time, and current updraft ventilator is fixed updraft ventilator, can not do the differentiation design to every point and different time.
Therefore, it is an urgent technical problem to be solved by those skilled in the art to provide a gas-material separation device, which can control the diameter of activated carbon particles separated from activated carbon discharged from an adsorption tower or a desorption tower, so as to accurately remove activated carbon powder having a large influence on the system, thereby protecting activated carbon-related equipment, preventing the equipment from being worn and corroded, and prolonging the service life of the equipment.
SUMMERY OF THE UTILITY MODEL
To the not enough of above-mentioned prior art, the utility model discloses can control the diameter of the active carbon granule that separates from adsorption tower or analytic tower exhaust active carbon to getting rid of that can be accurate influences the big active carbon powder of system, in order to realize the protection to the relevant equipment of active carbon, prevent wearing and tearing and corruption to equipment, extension equipment life. The utility model provides a gas material separator, this gas material separator includes: the device comprises a box body, a feed inlet, an extraction opening, a discharge opening and a fluidizing device; the feed inlet is arranged at the upper end or the upper part of the side surface of the box body; the discharge port is arranged at the lower end of the box body; the air extraction opening is arranged on the box body; the feed inlet, the extraction opening and the discharge opening are communicated with the interior of the box body; the air suction port is communicated with an external negative pressure source through a negative pressure pipeline; the fluidization device is arranged in the box body, and the upper end of the fluidization device is communicated with the feed inlet; the lower end of the fluidizing device is communicated with the discharge hole.
According to the utility model discloses a first embodiment provides a gas-material separator:
a gas-material separation device, comprising: the device comprises a box body, a feed inlet, an extraction opening, a discharge opening and a fluidizing device; the feed inlet is arranged at the upper end or the upper part of the side surface of the box body; the discharge port is arranged at the lower end of the box body; the air extraction opening is arranged on the box body; the feed inlet, the extraction opening and the discharge opening are communicated with the interior of the box body; the air suction port is communicated with an external negative pressure source through a negative pressure pipeline; the fluidization device is arranged in the box body, and the upper end of the fluidization device is communicated with the feed inlet; the lower end of the fluidizing device is communicated with the discharge hole.
Preferably, the fluidizing device comprises: a bearing inclined plane, a fluidizing gas nozzle and a fluidizing gas pipeline; the plurality of fluidizing gas nozzles are arranged on the bearing inclined plane; dividing the bearing inclined plane into n sections of fluidization areas; the fluidizing gas nozzle is communicated with the fluidizing gas pipeline.
Preferably, the fluidizing gas pipeline branch outlet fluidizing branch pipes are respectively communicated with the fluidizing gas nozzles on each section of the fluidizing zone; and a fluidization control valve is arranged on the fluidization branch pipe.
Preferably, the gas-material separation device further comprises: a blending device; the blending device comprises: uniformly mixing a nozzle; the mixing spout is arranged in the box body, and the spraying direction of the mixing spout is the space above the fluidizing device.
Preferably, the mixing device further comprises: a blending angle adjusting mechanism; the mixing spout is arranged in the box body through a mixing angle adjusting mechanism.
Preferably, the mixing nozzle is positioned above the discharge port.
Preferably, the spraying direction of the mixing nozzle forms an angle G with the flowing direction of the activated carbon, and the angle G is 90-180 degrees; preferably G is 135-170 °; more preferably G is between 145 and 160.
Preferably, the central axis of the feeding port and the central axis of the discharging port are arranged in a staggered mode.
Preferably, the gas-material separation device further comprises: a first airflow adjustment mechanism; the first air flow adjusting mechanism is arranged on the air pumping opening.
Preferably, the gas-material separation device further comprises: a first air pressure detection device; the first air pressure detection device is arranged on the box body.
Preferably, the first air pressure detection device detects that the air pressure in the box body is Pi, and the Pi is-30 Pa to-200 Pa; preferably, Pi is-50 Pa to-100 Pa; more preferably Pi is-60 Pa to-75 Pa.
Preferably, the gas-material separation device further comprises: a balance tube; the balance pipe is arranged at the feed inlet.
Preferably, the gas-material separation device further comprises: a second airflow adjustment mechanism; the second airflow adjusting mechanism is arranged on the balance pipe.
Preferably, the gas-material separation device further comprises: a second air pressure detection device; the second air pressure detection device is arranged at the feed inlet.
Preferably, the second air pressure detecting device is located above the balance pipe.
Preferably, the balance pipe is obliquely and downwards connected with the feed inlet, and the inclination angle A is 10-90 degrees; preferably A is 20-80 °; more preferably, A is 30 to 60.
Preferably, the balance pipe is further provided with a micropore material blocking mechanism, and the micropore material blocking mechanism is arranged at the top of the balance pipe or at the joint of the balance pipe and the feed inlet.
Preferably, the gas-material separation device further comprises: a heat-insulating layer; the heat-insulating layer is arranged on the outer side or the inner side of the shell of the box body.
Preferably, the gas-material separation device further comprises: a box body heating device; the box body heating device is arranged on the inner side or the outer side of the box body.
According to the utility model discloses a second embodiment provides an autonomic active carbon conveyor system of bleeding:
an autonomous pumped activated carbon transport system, the transport system comprising: the gas-material separation device and the closed activated carbon conveying mechanism of the first embodiment; and a discharge hole of the gas-material separation device is communicated with a feed hole of the closed activated carbon conveying mechanism.
Preferably, the air extraction port of the closed activated carbon transportation mechanism is communicated with the air extraction port of the gas-material separation device and then is connected to an external negative pressure source.
According to the utility model discloses a fourth embodiment provides a prevent that sintering flue gas from escaping the analytic system of active carbon adsorption:
the utility model provides a prevent desorption system of sintering flue gas escape active carbon adsorption, this desorption system of absorption includes: the system comprises an active carbon adsorption tower, an active carbon analysis tower, a main booster fan, a gas-material separation device and a closed active carbon conveying mechanism, wherein the gas-material separation device is arranged on the first embodiment; the air inlet of the main booster fan is communicated with the original sintering flue gas pipeline; the air outlet of the main booster fan is connected to the air inlet of the activated carbon adsorption tower; the feed opening of the activated carbon adsorption tower is connected to the feed opening of the activated carbon desorption tower through a closed activated carbon transportation mechanism, and/or the feed opening of the activated carbon adsorption tower is connected to the feed opening of the activated carbon desorption tower through a closed activated carbon transportation mechanism;
wherein, the feed opening of active carbon adsorption tower and/or active carbon analytic tower is connected with gas material separator's feed inlet, and gas material separator's discharge gate and closed active carbon transport mechanism intercommunication.
Preferably, the air suction port of the gas-material separation device is connected to an original sintering flue gas pipeline at the upstream of the main booster fan through a negative pressure pipeline; or the air exhaust port of the gas-material separation device is connected to the dust removal system through a negative pressure pipeline.
According to the fourth embodiment of the utility model, a material gas material separation control method under active carbon is provided:
a gas-material separation control method for blanking of activated carbon comprises the following steps: 1) gas material basic separation: separating the flue gas and the activated carbon powder from the activated carbon discharged from the adsorption tower or the desorption tower to obtain flue gas and dust mixed gas; 2) actively mixing flue gas and dust mixed gas: spraying uniform mixing gas into the flue gas and dust mixed gas obtained in the step 1) to obtain flue gas and dust mixed gas; 3) and (3) pumping flue gas and dust mixed gas meeting the particle size requirement: monitoring the maximum dust particle size A in the flue gas and dust mixed gas in real time, and continuously pumping the flue gas and dust mixed gas if the maximum dust particle size meets the requirement of the gas-material separation particle size d of A; otherwise, controlling and adjusting the particle size of the activated carbon powder of the flue gas and dust mixed gas separated in the step 1).
Preferably, in step 1), the method comprises the following steps: 1a) sectionally fluidizing the activated carbon discharged from the adsorption tower or the desorption tower: the active carbon discharged from the adsorption tower or the desorption tower sequentially passes through n sections of fluidization areas, high-pressure fluidization gas is blown into the active carbon from the bottom of each fluidization area, the flow rate of the high-pressure fluidization gas in each fluidization area is Pn, and n is 1, 2, 3 or 4 … …; 1b) the flow rate Pn of the fluidizing high-pressure gas in each fluidizing zone is controlled so that P1 > P2 > P3 > … … Pn.
Preferably, in step 1b), the fluidization high-pressure gas velocity Pn ═ u in the last stage of the fluidization zonemfAnd satisfy umfFormula (1);
wherein d is the particle size of the activated carbon to be separated, umfIs the fluidization velocity, rho is the fluid density, mu is the fluid viscosity, rhopIs the activated carbon dust density to be separated.
Preferably, in the step 3), if the maximum dust particle size a meets the requirement of the gas-material separation particle size d, the step of continuously extracting the flue gas and dust mixed gas specifically comprises the following steps: analyzing the flue gas and dust mixed gas by adopting a light scattering particle size measuring method to obtain the maximum dust particle size A in the flue gas and dust mixed gas; if A is from 0.8 to 1.3d, preferably A is from 0.9 to 1.1d, more preferably A is from 0.95 to 1.05 d; judging that the maximum dust particle size meets the requirement that A meets the gas-material separation particle size d.
Preferably, in the step 3), otherwise, the particle size of the activated carbon powder of the flue gas and dust mixed gas separated in the step 1) is controlled and adjusted to be specific; the fluidizing high-pressure gas velocity Pn of the last section of the fluidizing zone is adjusted in a wind velocity interval E by controlling the wind velocity, wherein E is 0.8-1.3umfPreferably E is 0.9-1.1umfMore preferably E is 0.95 to 1.05umf。
Preferably, if the maximum dust particle size is judged to meet the requirement that A is larger than the gas-material separation particle size d, Pn < u is adjustedmf(ii) a If the maximum dust particle size is judged to meet the requirement that A is smaller than the gas-material separation particle size d, regulating Pn to be more than umf。
Preferably, in the step 2), the blending gas is sprayed into the upper part of the activated carbon flowing area from the outlet of the activated carbon flowing area, and the spraying direction of the blending gas forms an angle G with the flowing direction of the activated carbon, wherein the angle G is 90-180 degrees; preferably G is 135-170 °; more preferably G is between 145 and 160.
In a first embodiment of the present invention, the separation box comprises: the device comprises a box body, a feed inlet, an extraction opening and a discharge opening; the active carbon enters the box body from the feeding hole, and the active carbon is discharged from the discharging hole after being temporarily stopped in the box body. At the moment, the pumping hole is communicated with an external negative pressure source, so that the flue gas or the acid gas entering the box body along with the activated carbon can be pumped out, the corrosion of the flue gas or the acid gas to downstream equipment is prevented, and the purpose of prolonging the service life of the downstream process equipment is realized.
The utility model discloses an in the first embodiment, the axis of feed inlet and the axis of discharge gate dislocation set each other. Can make the active carbon can not directly arrange away after getting into gas material separator, the extension active carbon will be at the distance and the time that the box flows through to be favorable to the acid gas in the active carbon gap to be taken away.
In the first embodiment of the present invention, the negative pressure value of the pumping hole can be appropriately adjusted by the first airflow adjusting mechanism, so that only the gas in the box body is controlled to be pumped. Without extracting the activated carbon microparticles.
In the first embodiment of the present invention, the air pressure value Pi in the box body is obtained in real time by the first air pressure detecting device. Thereby better controlling the first airflow adjustment mechanism.
The utility model discloses an in the first embodiment, set up balanced pipe in feed inlet department, balanced pipe makes the feed inlet be in external intercommunication, can adjust the gaseous atmospheric pressure of feed inlet department. Prevent the upstream acid gas from being actively adsorbed due to the overlarge negative pressure at the feed inlet. The air pressure value at the feed inlet can be accurately adjusted through the second air flow adjusting mechanism and the second air pressure detection device.
In the first embodiment of the present invention, the balance tube is inserted into the feed inlet obliquely downward, so that the active carbon powder can be prevented from escaping from the balance tube. And by combining the micropore material blocking mechanism, foreign matters can enter the gas-material separation device to influence the internal gas flow and material flow.
The utility model discloses an in the first embodiment, the heat preservation makes the box have the heat preservation function, combines box heating device, can keep getting into the activated carbon of gas-material separator's temperature and not reduce, and the preferred scheme is that the temperature improves slightly. Thereby preventing the active carbon from condensing in the gas-material separation device and preventing the separation box from being blocked.
The box body heating device is specifically an electric heating device or a steam heating device; the temperature in the separation box was: 110 ℃ and 140 ℃, preferably 120 ℃.
The utility model discloses an in the second embodiment, the active carbon conveying system who has gas-material separator can effectually prevent that the sintering flue gas of the subsidiary adsorption tower of active carbon or the acid gas of analytic tower from getting into the active carbon conveying mechanism to extension active carbon conveying mechanism's life, the active carbon conveying system of independently bleeding that provides in order to realize this application has the super high durability.
The utility model discloses an in the second embodiment, activated carbon transport mechanism is closed activated carbon transport mechanism, prevents that activated carbon adsorption's flue gas from scattering and disappearing in the transportation, and the extraction opening and the outside negative pressure source intercommunication of closed activated carbon transport mechanism's airtight cover can prevent sintering flue gas and/or acid gas's escape, improve the environmental quality in the production process.
The utility model discloses an in the third embodiment, prevent that sintering flue gas from escaping the active carbon adsorption tower of the analytic system of active carbon adsorption and the feed opening department of active carbon analytic tower all communicate with closed active carbon transport mechanism through gas material separator. The sintering flue gas of the active carbon adsorption tower and/or the acid gas of the active carbon desorption tower can be effectively prevented from entering the active carbon transportation system, so that the durability of the active carbon transportation mechanism is effectively improved.
The utility model discloses an in the third embodiment, utilize the negative pressure that main booster fan formed in its upstream to regard as gas material separator's outside negative pressure source, can realize above-mentioned beneficial effect under the condition that does not increase equipment cost.
The utility model discloses an in the fourth embodiment, separate out flue gas and activated carbon powder from adsorption tower or desorption tower exhaust active carbon earlier, recycle obtains flue gas dust mixing gas through spouting mixing gas with flue gas dust mixing gas mixing. The maximum dust particle size A in the flue gas and dust mixed gas is monitored in real time, and if the maximum dust particle size A meets the requirement of a gas-material separation particle size d, the flue gas and dust mixed gas is continuously extracted; if the maximum dust particle size A does not meet the requirement of the gas-material separation particle size d, namely the maximum particle size A is far larger than d or A is far smaller than d, the particle size of the activated carbon powder separated in the step 1) needs to be controlled and adjusted. The technical scheme that this application provided can control the diameter of the active carbon granule that separates from the active carbon of adsorption tower or analytic tower exhaust to get rid of that can be accurate influences the big active carbon powder of system, with the protection of realization to the relevant equipment of active carbon, prevent wearing and tearing and corruption to equipment, extension equipment life.
In a fourth embodiment of the present invention, in step 1), the fluidized effect on the activated carbon particles is utilized to separate the activated carbon powder meeting the requirement from the activated carbon particles. And spraying fluidizing high-pressure gas upwards at the bottom of the activated carbon flowing area to enable activated carbon powder with a certain particle size to be in a suspension state, and blowing the activated carbon powder with the particle size smaller than the particle size away from the activated carbon flowing area, so that the activated carbon powder is suspended above the activated carbon flowing area. In step 1b), the particle size of the activated carbon powder blown off from the activated carbon particles in different fluidization zones is controlled to be different by controlling the injection flow rate of the high-pressure fluidizing gas in the different fluidization zones. The spraying speed Pn of the fluidization area at the upstream of the activated carbon is greater than the spraying speed Pn of the fluidization area at the downstream of the activated carbon, so that a large amount of activated carbon powder is preferentially blown out in the fluidization area at the upstream of the activated carbon, wherein the activated carbon powder has the particle size far greater than the requirement of the gas-material separation particle size d. In the subsequent fluidization area, the spraying speed of the fluidization high-pressure gas is gradually reduced, so that the activated carbon powder exceeding the gas-material separation particle size d is settled and falls into the activated carbon particle flowing area, namely enters and returns to the activated carbon particles, and the separation and screening of the activated carbon powder and dust are realized. Therefore, the precision in the gas-material separation process can be improved.
It should be noted that the phenomenon that solid particles exhibit a fluid-like state under the action of a fluid is called fluidization, that is, fluidization.
In a fourth embodiment of the present invention, in step 1b), the fluidizing high-pressure gas flow rate Pn ═ u in the last stage of the fluidizing zonemfSatisfy the formula
When Pn is equal to umfAnd when the dust particles with the diameter of d are in a suspension state, the dust particles with the diameter smaller than d are separated from the fluidized bed layer and float above the activated carbon particle layer, and the dust particles with the diameter larger than d are continuously deposited in the activated carbon particle layer.
By controlling the flow rate of the fluidizing high-pressure gas in the last section of the fluidizing zone, the size of the dust particles which finally leave the zone through which the activated carbon particles flow can be controlled. In the fluidizing zone in P1 … … Pn-1, the flow of the fluidizing high-pressure gas is greater than umfThen the dust particles with the particle size less than or equal to d are blown away from the fluidized bed layer, and the dust particles with the particle size greater than d are deposited back to the activated carbon particles in the last end fluidized zone; and the dust particles with the particle size equal to d are suspended above the area through which the activated carbon particles flow; dust particles with a particle size smaller than d flow over the area through which the activated carbon particles flow under the action of the gas flow. Under the action of the uniform mixing gas in the step 2), the flue gas separated from the activated carbon particles and the activated carbon powder with the particle size less than or equal to d are uniformly mixed to obtain the flue gas and dust uniform mixing gas, so that the monitoring of the maximum particle size of the flue gas and dust uniform mixing gas in the step 3) is facilitated.
The utility model discloses a fourth embodiment, adopt the light scattering particle size survey method to carry out the particle size survey analysis to flue gas dust mixing gas. Under the action of the fluidization high-pressure body with fixed flow and the uniform mixing gas with fixed flow, the concentration of the uniform mixing gas of the flue gas and the dust is uniform, and the particle size can be measured by light scattering, so that a uniform particle size result can be observed. The proportion of the flue gas and dust mixed gas is different according to different dust particle sizes, and the overall refractive index and the light transmittance of the flue gas and dust mixed gas are different. Thereby measuring the maximum particle size value A in the flue gas and dust uniformly-mixed gas.
In the fourth embodiment of the present invention, in step 3), the fluidization high-pressure gas flow velocity Pn of the last section of the fluidization region is controlled in the wind speed interval E so that the particle size of the finally discharged dust satisfies the requirement of the gas-material separation particle size d.
The utility model discloses an in the fourth embodiment, can be rapidly with flue gas dust mist mixing through spouting into mixing gas, improve step 3), utilize the degree of accuracy of light scattering survey.
The principles of the present application are explained in more detail:
in a fourth embodiment, the bulk flowing substance is divided into: streams and gas streams, i.e., flow of activated carbon and flow of gas.
Material flow: the active carbon and the sinking flue gas enter the gas-material separator from the feed inlet of the separation box, and the active carbon enters the conveyor from the discharge outlet of the separation box by means of gravity.
Airflow: the flue gas sinking along with the activated carbon and the activated carbon powder lift gas generated by the material receiving and transportation of the dust-containing conveyer of the conveyer are driven by the gas pressure difference and are discharged from the gas extraction opening of the separation box. The air extraction opening of each separation box is provided with a first air flow adjusting mechanism, and a pressure value Pi inside the separation box is detected on the side of the first air pressure detection device on each separation box. And for each separating box, the opening degree of the first airflow regulating mechanism is regulated to be automatically interlocked with the pressure value Pi, and the air extraction amount from the air extraction opening is controlled by controlling the opening degree of the first airflow regulating mechanism, so that the pressure value of the corresponding separating box is maintained to be a set target value P. P is a slight negative pressure, and is generally controlled to be between-50 Pa and-100 Pa, preferably between-30 Pa and-200 Pa. Because the internal pressure of conveyer is 0, the raise dust of conveyer also upwards gets into the separator box through the bin outlet of separator box, also takes away from the extraction opening.
The balance pipe of each feed inlet has an auxiliary air flow balancing function, and the activated carbon cannot overflow from the balance pipe due to the fact that the balance pipe is inclined upwards. Because the pressure of the separation box is controlled to be micro negative pressure, a small amount of air flows in the balance pipe under the general condition, and the flow direction is from the outside to the inner flow of the active carbon discharge pipe. And a small amount of air is finally discharged into the main booster fan together with the sinking flue gas and the raised dust in the conveyor from the air extraction opening. In special cases, when the low-smoke gas changes sharply, the first airflow regulating mechanism needs a certain time (such as 40s) to regulate the target pressure, and the balance pipe can play a role in buffering and regulating so as not to enable the pressure in the separation box to deviate from the target value too far. The microporous plate or the microporous net on one side can prevent impurities from falling into the system and not influencing the air flow.
The technical scheme provided by the application also relates to a method for controlling the first airflow adjusting mechanism Vi, which comprises the following steps: PID control is performed by using the actual pressure value Pi and the target pressure value P of the corresponding separation tank. The control flow is shown in FIG. 8
It should be further noted that there are a plurality of discharge points, generally 6-18, at the lower part of the adsorption tower or the desorption tower, because the wear of the equipment is different at each point after manufacturing, or installing, or operating for a certain time, and the sinking smoke gas amount is different at each point. The system is provided with a pressure detection and air extraction regulating valve for each separation, each separation box is independently controlled, and each separation box is dynamically controlled; therefore, the air suction quantity can be controlled more accurately.
In the present invention, the length of the box body of the gas-material separation device is 10-500cm, preferably 20-400cm, more preferably 30-300cm, and even more preferably 40-200 cm.
In the present invention, the width of the box body of the gas-material separation device is 5-200cm, preferably 10-150cm, more preferably 15-120cm, and even more preferably 20-100 cm.
In the utility model, the outer diameter of the feed inlet is 10-95%, preferably 20-90%, more preferably 30-85% of the width of the box body.
In the utility model, the external diameter of the air extraction opening is 10-95%, preferably 20-90%, more preferably 30-85% of the width of the box body.
In the utility model, the outer diameter of the discharge port is 10-95%, preferably 20-90%, more preferably 30-85% of the width of the box body.
Compared with the prior art, the application of the method,
1) a dust remover is cancelled, so that the equipment investment of the dust remover of the active carbon device and the auxiliary electric power, automation and civil engineering investment of the dust remover are reduced by about 200 ten thousand yuan and the equipment maintenance is reduced, and the active carbon flue gas purification system is simpler and has lower running cost;
2) the sinking flue gas is sent to the adsorption tower again, further desulfurization, denitration, dust removal, more environmental protection. According to the original scheme, the sinking flue gas and the dust of the conveyor enter a dust remover for treatment, and the dust remover only has a dust removing function and does not have a desulfurization function and a denitration function. It should be explained that although the flue gas is the flue gas which sinks in the adsorption tower, the flue gas is adsorbed by activated carbon for a longer time, and although the flue gas contains SO2 and NOx, the content of the flue gas is very low, and the ultra-low emission level is achieved.
Compared with the prior art, the utility model discloses following beneficial effect has:
1. according to the technical scheme provided by the application, the flue gas sinking along with the activated carbon can not enter the conveying equipment and corrode the conveyer of the conveyer, which is the key equipment of the flue gas purification device;
2. according to the technical scheme provided by the application, the negative pressure value is controlled, so that the sinking smoke gas amount cannot be increased in the whole system;
3. according to the technical scheme provided by the application, each discharging point is independently controlled, and each discharging point is dynamically controlled; thereby improving the durability of the entire system.
Drawings
FIG. 1 is a schematic perspective structural view of a gas-material separation device without a balance pipe in an embodiment of the present invention;
FIG. 2 is a schematic perspective view of a gas-material separator with a balance tube according to an embodiment of the present invention;
FIG. 3 is a schematic structural view of a fluidizing device of a gas-material separating device according to an embodiment of the present invention;
FIG. 4 is a schematic view of the communication of the fluidized gas pipeline of the gas-material separation device according to the embodiment of the present invention;
FIG. 5 is a sectional view of the internal structure of the gas-material separator with a balance tube according to the embodiment of the present invention;
fig. 6 is a schematic structural diagram of an activated carbon adsorption and desorption system for preventing sintering flue gas from escaping in the embodiment of the present invention;
fig. 7 is a schematic structural diagram of an active carbon adsorption desorption system for preventing sintering flue gas from escaping in the embodiment of the present invention, in which a main booster fan is used as an external negative pressure source;
fig. 8 is a schematic structural diagram of a gas-material separation device installed at the bottom of the desorption tower in the embodiment of the present invention;
FIG. 9 is a schematic view of a prior art configuration in which an activated carbon adsorption tower is in communication with an activated carbon conveyor;
fig. 10 is a feedback flow chart of the adjustment of the gas-material separation device according to the air pressure value in the embodiment of the present invention.
Reference numerals:
1: a gas-material separation device; 2: a closed activated carbon transport mechanism; a: an activated carbon adsorption tower; b: an activated carbon desorption tower; c: a main booster fan;
101: a box body; 102: a feed inlet; 103: an air extraction opening; 104: a discharge port; 105: a second air pressure detection device; 106: a balance tube; 107: a second airflow adjustment mechanism; 108: a heat-insulating layer; 109: a box body heating device;
s: a fluidizing device; s01: supporting the inclined plane; s02: a fluidizing gas nozzle; sn: a fluidizing zone; h: a blending device; h1: uniformly mixing a nozzle; h2: a blending angle adjusting mechanism;
Lfluidization: a fluidizing gas conduit; l isFluidization branch pipe: a fluidization branch pipe; fFluidization: a fluidization control valve;
lf: a negative pressure pipeline; ls: an original sintering flue gas pipeline; pi: a first air pressure detection device; and Vi: a first airflow adjustment mechanism.
Detailed Description
According to the utility model discloses a first embodiment provides a gas-material separator:
a gas-material separation device, comprising: the device comprises a box body 101, a feed inlet 102, an extraction opening 103, a discharge outlet 104 and a fluidizing device S; the feed inlet 102 is arranged at the upper end or the upper part of the side surface of the box body 101; the discharge port 104 is arranged at the lower end of the box body 101; the extraction opening 103 is arranged on the box body 101; the feed inlet 102, the extraction opening 103 and the discharge opening 104 are communicated with the interior of the box body 101; the air pumping port 103 is communicated with an external negative pressure source through a negative pressure pipeline Lf; the fluidizing device S is arranged in the box body 101, and the upper end of the fluidizing device S is communicated with the feeding hole 102; the lower end of the fluidizing device S is communicated with the discharge port 104.
Preferably, the fluidizing device S comprises: bearing inclined plane S01, fluidizing gas nozzle S02 and fluidizing gas pipeline LFluidization(ii) a A plurality of the fluidizing gas nozzles S02 are disposed on the holding slope S01; dividing the bearing inclined plane S01 into n sections of fluidization areas Sn; the fluidizing gas nozzles S02 and the fluidizing gas pipe LFluidizationAnd (4) communicating.
Preferably, the fluidizing gas conduit LFluidizationTapping a fluidisation manifold LFluidization branch pipeRespectively communicated with the fluidizing gas nozzles S02 on each section of the fluidizing zone Sn; the fluidization branch pipe LFluidization branch pipeIs provided with a fluidization control valve FFluidization。
Preferably, the gas-material separation device further comprises: a blending device H; the blending device H comprises: mixing spout H1; the mixing spout H1 sets up in the box 101, just mixing spout H1 jet direction does fluidization device S upper space.
Preferably, the mixing device H further includes: a blending angle adjusting mechanism H2; the mixing spout H1 is arranged in the box body 101 through a mixing angle adjusting mechanism H2.
Preferably, the mixing nozzle H1 is located above the discharge port 104.
Preferably, the spraying direction of the mixing nozzle H1 forms an angle G with the flowing direction of the activated carbon, and G is 90-180 degrees; preferably G is 135-170 °; more preferably G is between 145 and 160.
Preferably, the central axis of the inlet 102 and the central axis of the outlet 104 are arranged in a staggered manner.
Preferably, the gas-material separation device further comprises: a first airflow adjusting mechanism Vi; the first air flow adjusting mechanism Vi is disposed on the suction port 103.
Preferably, the gas-material separation device further comprises: a first air pressure detecting device Pi; the first air pressure detecting device Pi is provided on the case 101.
Preferably, the first air pressure detecting device Pi measures the air pressure in the box 101 to be Pi, and the Pi is-30 Pa to-200 Pa; preferably, Pi is-50 Pa to-100 Pa; more preferably Pi is-60 Pa to-75 Pa.
Preferably, the gas-material separation device further comprises: a balance tube 106; the equalization pipe 106 is disposed at the feed inlet 102.
Preferably, the gas-material separation device further comprises: the second airflow adjusting mechanism 107; the second airflow adjusting mechanism 107 is provided on the balance pipe 106.
Preferably, the gas-material separation device further comprises: a second air pressure detecting device 105; the second air pressure detecting device 105 is disposed at the inlet 102.
Preferably, the second air pressure detecting device 105 is located above the balance pipe 106.
Preferably, the balance pipe 106 is obliquely downwards connected to the feed inlet 102, and the inclination angle A is 10-90 degrees; preferably A is 20-80 °; more preferably, A is 30 to 60.
Preferably, a micropore stop mechanism is further arranged on the balance pipe 106, and the micropore stop mechanism is arranged at the top of the balance pipe 106 or at the joint of the balance pipe 106 and the feed inlet 102.
Preferably, the gas-material separation device further comprises: an insulating layer 108; the insulating layer 108 is disposed outside or inside the outer shell of the case 101.
Preferably, the gas-material separation device further comprises: a tank heating device 109; the tank heating device 109 is disposed inside or outside the tank 101.
According to the utility model discloses a second embodiment provides an autonomic active carbon conveyor system of bleeding:
an autonomous pumped activated carbon transport system, the transport system comprising: the gas-material separation device 1, the closed activated carbon transport mechanism 2; and a discharge hole 104 of the gas-material separation device 1 is communicated with a feed inlet of the closed activated carbon conveying mechanism 2.
Preferably, the air extraction port of the closed activated carbon transportation mechanism 2 is connected to the air extraction port 103 of the gas-material separation device 1 and then connected to an external negative pressure source.
According to the utility model discloses a third embodiment provides a prevent sintering flue gas escape active carbon adsorption analytic system:
the utility model provides a prevent desorption system of sintering flue gas escape active carbon adsorption, this desorption system of absorption includes: an activated carbon adsorption tower A, an activated carbon desorption tower B, a main booster fan C, a gas-material separation device 1 as claimed in any one of claims 1 to 6, and a closed activated carbon transportation mechanism 2; the air inlet of the main booster fan C is communicated with the original sintering flue gas pipeline Ls; the air outlet of the main booster fan C is connected to the air inlet of the activated carbon adsorption tower A; the feed opening of the activated carbon adsorption tower A is connected to the feed opening of the activated carbon analysis tower B through the closed activated carbon transportation mechanism 2, and/or the feed opening of the activated carbon adsorption tower A is connected to the feed opening of the activated carbon analysis tower B through the closed activated carbon transportation mechanism 2;
wherein, the feed opening of the activated carbon adsorption tower A and/or the activated carbon desorption tower B is connected with the feed opening 102 of the gas-material separation device 1, and the discharge opening 104 of the gas-material separation device 1 is communicated with the closed activated carbon transportation mechanism 2.
Preferably, the air exhaust port 103 of the gas-material separation device 1 is connected to an original sintering flue gas pipeline Ls upstream of the main booster fan C through a negative pressure pipeline Lf; or the air exhaust port 103 of the gas-material separation device 1 is connected to the dust removal system through a negative pressure pipeline Lf.
When a plurality of separation boxes are used, the first air pressure detection devices of the plurality of separation boxes are marked as follows: p1, P2, P3, P4 … …; the first airflow adjusting mechanism of the plurality of separating boxes is as follows: v1, V2, V3 and V4 … ….
According to the fourth embodiment of the utility model, a material gas material separation control method under active carbon is provided:
a gas-material separation control method for blanking of activated carbon comprises the following steps: 1) gas material basic separation: separating the flue gas and the activated carbon powder from the activated carbon discharged from the adsorption tower or the desorption tower to obtain flue gas and dust mixed gas; 2) actively mixing flue gas and dust mixed gas: spraying uniform mixing gas into the flue gas and dust mixed gas obtained in the step 1) to obtain flue gas and dust mixed gas; 3) and (3) pumping flue gas and dust mixed gas meeting the particle size requirement: monitoring the maximum dust particle size A in the flue gas and dust mixed gas in real time, and continuously pumping the flue gas and dust mixed gas if the maximum dust particle size meets the requirement of the gas-material separation particle size d of A; otherwise, controlling and adjusting the particle size of the activated carbon powder of the flue gas and dust mixed gas separated in the step 1).
Preferably, in step 1), the method comprises the following steps: 1a) sectionally fluidizing the activated carbon discharged from the adsorption tower or the desorption tower: the active carbon discharged from the adsorption tower or the desorption tower sequentially passes through n sections of fluidization areas, high-pressure fluidization gas is blown into the active carbon from the bottom of each fluidization area, the flow rate of the high-pressure fluidization gas in each fluidization area is Pn, and n is 1, 2, 3 or 4 … …; 1b) the flow rate Pn of the fluidizing high-pressure gas in each fluidizing zone is controlled so that P1 > P2 > P3 > … … Pn.
Preferably, in step 1b), the fluidization high-pressure gas velocity Pn ═ u in the last stage of the fluidization zonemfAnd satisfy umfFormula (1);
wherein d is the particle size of the activated carbon to be separated, umfIs the fluidization velocity, rho is the fluid density, mu is the fluid viscosity, rhopIs the activated carbon dust density to be separated.
Preferably, in the step 3), if the maximum dust particle size a meets the requirement of the gas-material separation particle size d, the step of continuously extracting the flue gas and dust mixed gas specifically comprises the following steps: analyzing the flue gas and dust mixed gas by adopting a light scattering particle size measuring method to obtain the maximum dust particle size A in the flue gas and dust mixed gas; if A is from 0.8 to 1.3d, preferably A is from 0.9 to 1.1d, more preferably A is from 0.95 to 1.05 d; judging that the maximum dust particle size meets the requirement that A meets the gas-material separation particle size d.
Preferably, in the step 3), otherwise, the particle size of the activated carbon powder of the flue gas and dust mixed gas separated in the step 1) is controlled and adjusted to be specific; the fluidizing high-pressure gas velocity Pn of the last section of the fluidizing zone is controlled by controlling the wind speedAdjusting the wind speed interval E to be 0.8-1.3umfPreferably E is 0.9-1.1umfMore preferably E is 0.95 to 1.05umf。
Preferably, if the maximum dust particle size is judged to meet the requirement that A is larger than the gas-material separation particle size d, Pn < u is adjustedmf(ii) a If the maximum dust particle size is judged to meet the requirement that A is smaller than the gas-material separation particle size d, regulating Pn to be more than umf。
Preferably, in the step 2), the blending gas is sprayed into the upper part of the activated carbon flowing area from the outlet of the activated carbon flowing area, and the spraying direction of the blending gas forms an angle G with the flowing direction of the activated carbon, wherein the angle G is 90-180 degrees; preferably G is 135-170 °; more preferably G is between 145 and 160.
In the present invention, the length of the box body of the gas-material separation device is 10-500cm, preferably 20-400cm, more preferably 30-300cm, and even more preferably 40-200 cm.
In the present invention, the width of the box body of the gas-material separation device is 5-200cm, preferably 10-150cm, more preferably 15-120cm, and even more preferably 20-100 cm.
In the utility model, the outer diameter of the feed inlet is 10-95%, preferably 20-90%, more preferably 30-85% of the width of the box body.
In the utility model, the external diameter of the air extraction opening is 10-95%, preferably 20-90%, more preferably 30-85% of the width of the box body.
In the utility model, the outer diameter of the discharge port is 10-95%, preferably 20-90%, more preferably 30-85% of the width of the box body.
Example 1
A gas-material separation device, comprising: the device comprises a box body 101, a feed inlet 102, an extraction opening 103, a discharge outlet 104 and a fluidizing device S; the feed inlet 102 is arranged at the upper end or the upper part of the side surface of the box body 101; the discharge port 104 is arranged at the lower end of the box body 101; the extraction opening 103 is arranged on the box body 101; the feed inlet 102, the extraction opening 103 and the discharge opening 104 are communicated with the interior of the box body 101; the air pumping port 103 is communicated with an external negative pressure source through a negative pressure pipeline Lf; the fluidizing device S is arranged in the box body 101, and the upper end of the fluidizing device S is communicated with the feeding hole 102; the lower end of the fluidizing device S is communicated with the discharge port 104.
Example 2
Example 1 was repeated except that the fluidizing device S comprised: bearing inclined plane S01, fluidizing gas nozzle S02 and fluidizing gas pipeline LFluidization(ii) a A plurality of the fluidizing gas nozzles S02 are disposed on the holding slope S01; dividing the bearing inclined plane S01 into n sections of fluidization areas Sn; the fluidizing gas nozzles S02 and the fluidizing gas pipe LFluidizationAnd (4) communicating.
Example 3
Example 2 was repeated, except that the fluidizing gas conduit LFluidizationTapping a fluidisation manifold LFluidization branch pipeRespectively communicated with the fluidizing gas nozzles S02 on each section of the fluidizing zone Sn; the fluidization branch pipe LFluidization branch pipeIs provided with a fluidization control valve FFluidization。
Example 4
Example 3 was repeated except that the gas-material separating device further included: a blending device H; the blending device H comprises: mixing spout H1; the mixing spout H1 sets up in the box 101, just mixing spout H1 jet direction does fluidization device S upper space.
Example 5
Example 4 is repeated except that the kneading apparatus H further comprises: a blending angle adjusting mechanism H2; the mixing spout H1 is arranged in the box body 101 through a mixing angle adjusting mechanism H2. The mixing nozzle H1 is positioned above the discharge hole 104.
Example 6
Example 5 was repeated except that the direction of injection of the mixing port H1 was at an angle G of 175 degrees to the direction of flow of the activated carbon.
Example 7
Example 6 is repeated, except that the central axis of the inlet 102 and the central axis of the outlet 104 are offset from each other.
Example 8
Example 7 was repeated except that the gas-material separating device further included: a first airflow adjusting mechanism Vi; the first air flow adjusting mechanism Vi is disposed on the suction port 103.
Example 9
Example 8 was repeated except that the gas-material separating device further included: a first air pressure detecting device Pi; the first air pressure detecting device Pi is provided on the case 101.
Example 10
Example 9 was repeated except that the first air pressure detecting means Pi measured the air pressure Pi inside the case 101, Pi was-50 Pa.
Example 11
Example 10 was repeated except that the gas-material separating device further included: a balance tube 106; the balance tube 106 is arranged at the feed inlet 102; this gas-material separation device still includes: the second airflow adjusting mechanism 107; the second airflow adjusting mechanism 107 is provided on the balance pipe 106.
Example 12
Example 11 was repeated except that the gas-material separating device further included: a second air pressure detecting device 105; the second air pressure detecting device 105 is disposed at the inlet 102. The second air pressure detecting device 105 is located above the balance pipe 106.
Example 13
Example 12 was repeated except that the balance tube 106 was inclined downward into the feed inlet 102 at an angle A of 45. The balance pipe 106 is further provided with a micropore stock stop which is arranged at the top of the balance pipe 106 or at the joint of the balance pipe 106 and the feed inlet 102.
Example 14
Example 13 was repeated except that the gas-material separating device further included: an insulating layer 108; the insulating layer 108 is disposed outside or inside the outer shell of the case 101.
Example 15
Example 14 was repeated except that the gas-material separation apparatus further included: a tank heating device 109; the tank heating device 109 is disposed inside or outside the tank 101.
Example 16
An autonomous pumped activated carbon transport system, the transport system comprising: a gas-material separation device 1 and a closed activated carbon conveying mechanism 2 in the first embodiment; and a discharge hole 104 of the gas-material separation device 1 is communicated with a feed inlet of the closed activated carbon conveying mechanism 2.
Example 17
Example 16 was repeated except that the extraction port of the closed activated carbon transport mechanism 2 was connected to the extraction port 103 of the gas-material separation device 1 and then connected to an external negative pressure source.
Example 18
The utility model provides a prevent desorption system of sintering flue gas escape active carbon adsorption, this desorption system of absorption includes: the system comprises an active carbon adsorption tower A, an active carbon desorption tower B, a main booster fan C, a gas-material separation device 1 and a closed active carbon conveying mechanism 2, wherein the gas-material separation device is arranged on the main booster fan; the air inlet of the main booster fan C is communicated with the original sintering flue gas pipeline Ls; the air outlet of the main booster fan C is connected to the air inlet of the activated carbon adsorption tower A; the feed opening of the activated carbon adsorption tower A is connected to the feed opening of the activated carbon analysis tower B through the closed activated carbon transportation mechanism 2, and/or the feed opening of the activated carbon adsorption tower A is connected to the feed opening of the activated carbon analysis tower B through the closed activated carbon transportation mechanism 2; wherein, the feed opening of the activated carbon adsorption tower A and/or the activated carbon desorption tower B is connected with the feed opening 102 of the gas-material separation device 1, and the discharge opening 104 of the gas-material separation device 1 is communicated with the closed activated carbon transportation mechanism 2.
Example 19
Example 18 is repeated, except that the air suction port 103 of the gas-material separation device 1 is connected to the original sintering flue gas pipeline Ls at the upstream of the main booster fan C through the negative pressure pipeline Lf; or the air exhaust port 103 of the gas-material separation device 1 is connected to the dust removal system through a negative pressure pipeline Lf.
Claims (36)
1. A gas-material separation device, characterized in that, this gas-material separation device includes: the device comprises a box body (101), a feed inlet (102), an extraction opening (103), a discharge opening (104) and a fluidizing device (S); the feed inlet (102) is arranged at the upper end or the upper part of the side surface of the box body (101); the discharge hole (104) is arranged at the lower end of the box body (101); the air extraction opening (103) is arranged on the box body (101); the feed inlet (102), the extraction opening (103) and the discharge opening (104) are communicated with the interior of the box body (101); the air pumping port (103) is communicated with an external negative pressure source through a negative pressure pipeline (Lf);
the fluidization device (S) is arranged in the box body (101), and the upper end of the fluidization device (S) is communicated with the feeding hole (102); the lower end of the fluidizing device (S) is communicated with the discharge hole (104); the length of the box body (101) is 10-500 cm.
2. Gas-material separation device according to claim 1, wherein the fluidization device (S) comprises: a bearing inclined plane (S01), a fluidizing gas nozzle (S02) and a fluidizing gas pipeline (L)Fluidization)；
A plurality of said fluidization gas nozzles (S02) are arranged on said holding ramp (S01); dividing the supporting slope (S01) into n sections of fluidizing zones (Sn); the fluidizing gas nozzles (S02) and the fluidizing gas duct (L)Fluidization) And (4) communicating.
3. The gas-material separation device according to claim 2, characterized in that: the fluidizing gas conduit (L)Fluidization) Tapping a fluidisation branch (L)Fluidization branch pipe) Respectively communicated with the fluidizing gas nozzles (S02) on each section of the fluidizing zone (Sn); the fluidization branch pipe (L)Fluidization branch pipe) Is provided with a fluidization control valve (F)Fluidization)。
4. The gas-material separation device according to claim 2 or 3, further comprising: a kneading device (H); the mixing device (H) comprises: a mixing spout (H1); mixing spout (H1) sets up in box (101), just mixing spout (H1) jet direction does fluidization device (S) top space.
5. The gas-material separation device according to claim 4, wherein the blending device (H) further comprises: a blending angle adjusting mechanism (H2); the blending nozzle (H1) is arranged in the box body (101) through a blending angle adjusting mechanism (H2).
6. The gas-material separation device of claim 5, wherein the mixing spout (H1) is located above the discharge port (104).
7. The gas-material separation device of claim 6, wherein the spraying direction of the mixing nozzle (H1) forms an angle G with the flowing direction of the activated carbon, and G is 90-180 degrees.
8. The gas-material separation device according to claim 7, wherein G is 135 ° to 170 °.
9. The gas-material separation device according to claim 8, wherein G is 145 ° to 160 °.
10. The gas-material separation device according to claim 4, wherein the central axis of the feed inlet (102) and the central axis of the discharge outlet (104) are arranged in a staggered manner; and/or
This gas-material separation device still includes: a first airflow adjusting mechanism (Vi); the first air flow adjusting mechanism (Vi) is arranged on the air suction opening (103).
11. The gas-material separation device according to claims 5-9, wherein the central axis of the inlet (102) and the central axis of the outlet (104) are arranged in a staggered manner; and/or
This gas-material separation device still includes: a first airflow adjusting mechanism (Vi); the first air flow adjusting mechanism (Vi) is arranged on the air suction opening (103).
12. The gas-material separation device of claim 10, further comprising: a first air pressure detecting device (Pi); the first air pressure detection device (Pi) is arranged on the box body (101).
13. The gas-material separation device of claim 11, further comprising: a first air pressure detecting device (Pi); the first air pressure detection device (Pi) is arranged on the box body (101).
14. The gas-material separating device according to claim 12 or 13, wherein the first air pressure detecting means (Pi) detects an air pressure Pi inside the box (101), Pi being-30 Pa to-200 Pa.
15. The gas-material separator according to claim 14, wherein Pi is-50 Pa to-100 Pa.
16. The gas-material separator according to claim 15, wherein Pi is-60 Pa to-75 Pa.
17. The gas-material separation device according to any one of claims 1 to 3, 5 to 10, 12 to 13, and 15 to 16, further comprising: a balance tube (106); the equalizing tube (106) is disposed at the feed inlet (102).
18. The gas-material separation device of claim 4, further comprising: a balance tube (106); the equalizing tube (106) is disposed at the feed inlet (102).
19. The gas-material separation device of claim 11, further comprising: a balance tube (106); the equalizing tube (106) is disposed at the feed inlet (102).
20. The gas-material separation device of claim 17, further comprising: a second airflow adjusting mechanism (107); the second airflow adjusting mechanism (107) is arranged on the balance pipe (106).
21. The gas-material separation device according to claim 18 or 19, further comprising: a second airflow adjusting mechanism (107); the second airflow adjusting mechanism (107) is arranged on the balance pipe (106).
22. Gas-material separation device according to any one of claims 18-20, further comprising: a second air pressure detection device (105); the second air pressure detection device (105) is arranged at the feed opening (102); and/or
The balance pipe (106) is obliquely and downwards connected to the feed inlet (102), and the inclination angle A is 10-90 degrees.
23. The gas-material separation device of claim 17, further comprising: a second air pressure detection device (105); the second air pressure detection device (105) is arranged at the feed opening (102); and/or
The balance pipe (106) is obliquely and downwards connected to the feed inlet (102), and the inclination angle A is 10-90 degrees.
24. The gas-material separation device of claim 21, further comprising: a second air pressure detection device (105); the second air pressure detection device (105) is arranged at the feed opening (102); and/or
The balance pipe (106) is obliquely and downwards connected to the feed inlet (102), and the inclination angle A is 10-90 degrees.
25. Gas-material separation device according to claim 22, characterized in that the second air pressure detection device (105) is located above the equalization pipe (106); and/or
A is 20-80 degrees.
26. Gas-material separation device according to claim 23, characterized in that the second air pressure detection device (105) is located above the equalization pipe (106); and/or
A is 20-80 degrees.
27. Gas-material separation device according to claim 24, characterized in that the second air pressure detection device (105) is located above the equalization pipe (106); and/or
A is 20-80 degrees.
28. Gas-material separation device according to any one of claims 25-27, wherein a is 30-60 °.
29. The gas-material separation device according to claim 28, wherein a micropore baffle mechanism is further arranged on the balance pipe (106), and the micropore baffle mechanism is arranged at the top of the balance pipe (106) or at the connection part of the balance pipe (106) and the feed inlet (102).
30. A gas-material separation device according to any one of claims 1 to 3, 5 to 10, 12 to 13, 15 to 16, 18 to 20, 23 to 27 and 29, further comprising: an insulating layer (108); the heat insulation layer (108) is arranged on the outer side or the inner side of the shell of the box body (101); and/or
This gas-material separation device still includes: a box heating device (109); the box body heating device (109) is arranged on the inner side or the outer side of the box body (101).
31. The gas-material separation device of claim 4, further comprising: an insulating layer (108); the heat insulation layer (108) is arranged on the outer side or the inner side of the shell of the box body (101); and/or
This gas-material separation device still includes: a box heating device (109); the box body heating device (109) is arranged on the inner side or the outer side of the box body (101).
32. The gas-material separation device of claim 11, further comprising: an insulating layer (108); the heat insulation layer (108) is arranged on the outer side or the inner side of the shell of the box body (101); and/or
This gas-material separation device still includes: a box heating device (109); the box body heating device (109) is arranged on the inner side or the outer side of the box body (101).
33. An autonomous pumped activated carbon transport system, the transport system comprising: a gas-material separation device (1), a closed activated carbon transport means (2) according to any one of claims 1 to 32; and a discharge hole (104) of the gas-material separation device (1) is communicated with a feed inlet of the closed activated carbon conveying mechanism (2).
34. The system for transporting the activated carbon through automatic air exhaust according to claim 33, wherein the air exhaust port of the closed activated carbon transporting mechanism (2) is connected with the air exhaust port (103) of the gas-material separating device (1) and then connected with an external negative pressure source.
35. The utility model provides a prevent that sintering flue gas from escaping active carbon adsorption analytic system which characterized in that, this adsorption analytic system includes: an activated carbon adsorption tower (A), an activated carbon desorption tower (B), a main booster fan (C), the gas-material separation device (1) as claimed in any one of claims 1 to 34, and a closed activated carbon transportation mechanism (2); the air inlet of the main booster fan (C) is communicated with the original sintering flue gas pipeline (Ls); the air outlet of the main booster fan (C) is connected with the air inlet of the active carbon adsorption tower (A); the feed opening of the activated carbon adsorption tower (A) is connected to the feed opening of the activated carbon desorption tower (B) through a closed activated carbon transportation mechanism (2), and/or the feed opening of the activated carbon adsorption tower (A) is connected to the feed opening of the activated carbon desorption tower (B) through the closed activated carbon transportation mechanism (2);
wherein, the feed opening of the activated carbon adsorption tower (A) and/or the activated carbon desorption tower (B) is connected with the feed opening (102) of the gas-material separation device (1), and the discharge opening (104) of the gas-material separation device (1) is communicated with the closed activated carbon conveying mechanism (2).
36. The activated carbon adsorption desorption system for preventing sintering flue gas from escaping according to claim 35, wherein the extraction opening (103) of the gas-material separation device (1) is connected to the original sintering flue gas pipeline (Ls) at the upstream of the main booster fan (C) through a negative pressure pipeline (Lf); or the air extraction opening (103) of the gas-material separation device (1) is connected into a dust removal system through a negative pressure pipeline (Lf).
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| CN114733312A (en) * | 2022-04-02 | 2022-07-12 | 金能科技股份有限公司 | Device and method for improving utilization rate of coke oven flue gas desulfurization and denitrification active carbon |
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| CN114733312A (en) * | 2022-04-02 | 2022-07-12 | 金能科技股份有限公司 | Device and method for improving utilization rate of coke oven flue gas desulfurization and denitrification active carbon |
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