CN101275744A - Apparatus for comprehensively utilizing coal mine to ventilate mash gas - Google Patents
Apparatus for comprehensively utilizing coal mine to ventilate mash gas Download PDFInfo
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- CN101275744A CN101275744A CNA200710064889XA CN200710064889A CN101275744A CN 101275744 A CN101275744 A CN 101275744A CN A200710064889X A CNA200710064889X A CN A200710064889XA CN 200710064889 A CN200710064889 A CN 200710064889A CN 101275744 A CN101275744 A CN 101275744A
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Abstract
A device for the coal ventilation gas comprehensive utilization, a reactor outlet end with the same structure is connected into a U-shape reactor through a heat taking device; the entrance of the reactor is filled with a honeycomb heat retaining mass; the outlet end is a catalyst bed layer; an electric heater is arranged between the heat retaining mass outlet end and the catalyst bed layer; the entrance of the raw gas is provided with a valve set for controlling the conversion of the current direction in the reactor; the raw gas enters the reactor, and generates the catalytic combustion on the catalyst bed layer; a saddle type bed temperature distribution is realized in the reactor by processing the periodic switch through the current direction of the reaction gas, the burning end gas is fetched out by the heat taking device. The invention has higher heat reclaim efficiency; when the concentration of the methane in the ventilation gas and the flow of the ventilation gas change, the high efficiency selfheating operation can be realized.
Description
Technical field
The present invention relates to a kind of coal mine to ventilate mash gas gas comprehensive utilization technique, solved big and concentration of methane concentration lower (＜1.0%), gas flow and flow and had trans-utilization problem than the ventilating gas gas of great fluctuation process, can be applicable to the processing of Device in Gas, realize that reduction of greenhouse gas discharge and energy reclaim.
Background technology
The huge reserves of coal bed gas and the high enthalpy of combustion of methane wherein make it have potential energy and recycle value.In addition, formally effective along with Kyoto Protocol, CO
2The reduction of discharging volume has become the much-sought-after item on investment circle.And the greenhouse effects of methane are CO
221 times, therefore, coal bed gas comprehensive utilization can produce direct economic benefit, also can produce indirect environmental benefit simultaneously.At present, the coal bed gas comprehensive utilization arouses extensive attention at home and abroad.
Now developed the dense Device in Gas trans-utilization of multiple high technology, carried conversion etc. as coal bed gas generating, pipeline.Coal bed gas generating total installation of generating capacity reaches 90,000 kW in China.And account for the ventilating gas gas of coal bed methane total amount more than 70%, owing to methane concentration low (＜1.0%), difficult collection, large-minded (40-500m
3/ s), and the flow velocity of gas and instability of flow, therefore, the comprehensive utilization of ventilating gas gas has very big challenge.
The utilization of ventilating gas gas mainly realizes by dual mode, promptly transforms as basic fuel with as auxiliary fuel.As auxiliary fuel, be used for substituting combustion air and infeed pulverized-coal burner, kiln, this mode is one of better approach of ventilating gas gas utilization, but must near the coalmine ventilation mouth large-sized boiler be arranged, and limited by the region.And as the ventilating gas transform mode of basic fuel, mainly comprise at present and carry dense and low concentration directly transforms.There is bigger techno-economic question in the former, and treating capacity is limited.Therefore, main application approach directly transforms for low dense methane.Low dense direct conversion can be divided into direct burning (＞1000 ℃) and catalytic combustion (400-600 ℃) again according to the kinetics mechanism of methane conversion, and these two kinds of transform modes all are based on the heat-accumulation combustion principle.
Sweden Megtec company (US005997277 and US6302188) has developed the heat storage type combustion converter that is used to remove volatile organic matter, and material, the cross section structure of heat-storing material improved.But the mode of employing thermal oxide has the requirement of comparison harshness inevitably to the material of reactor, and the startup of system is slower in addition.Because for the stable methane of macroscopic property, when its concentration during at 3000～5000ppm, on-catalytic directly burning to open the combustion temperature be about 1300～1400 ℃.In addition, based on the heat-storage catalytic theory of combustion, US2003/0070549 has increased the adsorption desorption device before the heat-accumulation combustion reactor, at first fuel gas is concentrated, and catalyst combustion reaction takes place then, the system process more complicated.In addition, the combustion catalyst that the heat-storage catalytic combustion process of patent report is used is a beaded catalyst, and the ventilating gas system for handling bigger for gas flow will certainly increase resistance drop.The Starting mode (Chinese patent ZL20040120402) at reactor outer wall winding heat tape that adopts simultaneously is difficult to satisfy commercial Application; In addition, do not consider the recycling of heat, therefore, to intrasystem difficult control of temperature.
Summary of the invention
The object of the present invention is to provide a kind of device that fully utilizes ventilating gas gas, recycle to realize reduction of greenhouse gas discharge and energy.
For achieving the above object, the device of comprehensive utilization coal mine to ventilate mash gas provided by the invention is that two identical reactor outlet ends of structure connect into U type reactor by a heat-obtaining device;
This reactor inlet end parts is filled with honeycomb heat accumulation body;
This reactor outlet end is divided into beds;
Heat storage go out and beds between be furnished with electric heater;
The unstripped gas porch is provided with the conversion that valve group control gas flows at inside reactor;
Unstripped gas enters reactor, with catalyst generation catalytic combustion, carries out periodically switching " saddle-shape " bed temperature distribution in the realization response device that flows to of reacting gas by the valve group on beds, and combustion tail gas is drawn by the heat-obtaining device.
Described device, wherein, reactor cross section is square or circular configuration, the reactor inlet end and the port of export are taper.
Described device, wherein, the catalyst of employing is particle or integer catalyzer.
Described device, wherein, catalyst is noble metal or metal oxide catalyst.
Described device, wherein, heat storage is the particle or the integral honeycomb ceramic heat storage body of high heat capacity.
Described device, wherein, electric heater is made up of some groups of finned tubes.
Described device, wherein, the heat-obtaining device is coil heat exchanger or plate wing electric heater.
Described device, wherein, the valve group of control gas flow is pneumatic operated valve or magnetic valve.
Described device, wherein, the reactor inlet end and the port of export are provided with cuboid or cylinder bodily form screen or sieve plate as gas distribution grid.
Described device, wherein, by some groups of U type combination of reactors.
The advantage that the present invention has:
One, integral honeycomb heat storage of Cai Yonging and catalyst have higher block resistance, and high intensity and low resistance drop are specially adapted to that gas flow is big, methane concentration is low, and there are the ventilating gas comprehensive regulation system of fluctuation in flow and concentration simultaneously; This system has stronger self-maintenance capability.
Two, several groups of pipe wing electric heaters according to the certain space positional alignment of Cai Yonging have bigger area of heat transfer, and gas can thermally equivalents.Therefore, system has fast toggle speed, and is suitable for further amplification and practical application.
Three, adopt the mode of middle part heat-obtaining (heat exchange or extension high-temp combustion tail gas), the system that makes has bigger operating flexibility, is applicable to that also the catalytic combustion of other fuel gas of high concentration, high heating value removes.
Four, design special gas distribution grid, gas is distributed on catalyst equably, improved the utilization rate of catalyst; In addition, this system has the higher thermal efficiency, has realized that ventilating gas gas efficiently utilizes, and has also realized CO simultaneously
2Reduce discharging.
Description of drawings
Fig. 1 is the experimental implementation flow process;
Fig. 2 forces distribution mode for gas;
Fig. 3 is a flow-reversal technology;
Fig. 4 is a thermometric mode in the system;
Fig. 5 is the Temperature Distribution in the reactor under the different operating modes;
Fig. 6 is methane exit concentration and a conversion ratio stable under the different operating modes;
Fig. 7 falls for intrasystem pressure under the different operating modes;
Fig. 8 is the cyclically-varying rule of temperature in the system;
The specific embodiment
Device provided by the invention is to be applied to catalytic combustion flow to change technology, have start fast, ignition temperature is gentle and system from keeping characteristics such as performance is strong.Solved traditional heat accumulating type catalytic combustion converter, it is slow that high ignition temperature requires height, system to start to reactor material, problems such as cost height; Solve the heat accumulating type catalytic oxidizer internal resistance that causes owing to beaded catalyst effectively and fallen bigger problem; System's ignition temperature is controlled, and the thermal efficiency is higher;
The technical solution used in the present invention is: one, utilize the efficient low dense methyl hydride combustion catalyst of exploitation, when reaction temperature about 550 ℃, methane just can transform fully; And this catalyst has high heat endurance.Two, the integer catalyzer combustion technology of Cai Yonging, under high-speed, the resistance drop of system is still very little; Big for gas flow, as to have certain dust content ventilating gas system has stronger practicality.Three, adopt from the method for combustion system middle part heat-obtaining or carrying-off partial combustion tail gas, can control and heat recovery by the implement device temperature stabilization, when fluctuation takes place in methane concentration device still prodigiosin enough keep self-heating operation under the steady temperature, improved the thermal efficiency of device simultaneously.
The heat-storage catalytic theory of combustion that the present invention adopts, this device comprises energy storage bed, catalytic bed, system starting device, gas distribution grid, heat recovery and utilization mode and automatic control system.What wherein energy storage bed was filled is high heat capacity and high-intensity integral honeycomb heat storage; What catalytic bed was used is whole low dense methyl hydride combustion catalyst, and it has high heat endurance and activity; At the pipe wing electric heater of beds front end setting according to spatial distribution; Arrange special-purpose gas distribution grid at the inlet of the system of system or the outlet of beds, force fluid to distribute and realize uniform Flow Field Distribution; Arrange that at two-stage catalytic bed middle part heat-obtaining device or extension combustion tail gas carry out heat exchange; Arrange that on catalyst, heat storage and heat reclaim unit thermocouple comes detected temperatures, the automatic control of implement device.
Referring to accompanying drawing 1, at arrival end leading portion partially filled integral honeycomb heat storage 6a of the present invention and 6b; Heat storage outlet deployment tube wing electric heater 7a and 7b; The inside and outside wall of reactor adopts insulation materials such as refractory brick, silica wool; Air-flow enters beds 8a and 8b through electric heater; Between catalyst 8a and 8b, arrange heat-obtaining device 10 or with partial combustion tail gas extraction system.Thereby improve the effective rate of utilization of catalyst in order to realize that in catalysis uniform fluid distributes, can arrange that cuboid or cylinder bodily form screen or sieve plate 5a, 9a, 5b and 9b come forced gas evenly to distribute at inlet or outlet according to the structure of reactor.Arranged that all thermocouple comes detected temperatures in catalyst and heat storage and reactor cavity, come Temperature Distribution in the conditioned reaction device by the quantitative relationship between the heat transferring medium flow in the temperature detecting point set up and the heat-obtaining device, thereby realize the self-heating operation of safety and stability.Ventilating gas gas infeeds in the device of the present invention through air blast 1 and cleaner 2, realizes the variation of gas flow by valve group 3a, 4a, 3b, 4b.Simultaneously fall also and detect importing and exporting the pressure of setting pressure sensors (known technology, not shown in the figures) bed.
Described integral honeycomb heat storage is to have high heat capacity, high-intensity inert ceramic material.
Described catalyst is noble metal or metal oxide honeycomb integral combustion catalyst, and this catalyst has advantages of high catalytic activity, and methane can transform fully in the time of 550 ℃.And it has thermodynamic stability preferably, and through 1000 hours catalyst stabilities test, active only had slight decline.
Described starting drive is one group of pipe wing electric heater of arranging according to the locus, and it has bigger heat transfer area, and reasonably the locus is arranged and can be made the air-flow thermally equivalent simultaneously;
Described heat-obtaining device is the coil heat exchanger according to operating mode design, also can be plate-fin heat exchanger efficiently.
Described flow distribution pattern adopts screen and sieve plate as shown in Figure 2, by numerical simulation means, and the diameter and the different distribution of apertures greatly in hole on the width of optimizing grizzly bar on the screen and the sieve plate, thereby the even distribution of realization fluid on catalyst.
Described flow-reversal is to realize the conversion that air-flow as shown in Figure 3 flows at inside reactor by one four two logical or two triple valves or four two-way valves, can be that pneumatic operated valve also can be a magnetic valve, realize the keying of valve group by relay, thereby changed the direction of air-flow.As open valve 3b and 4a, shut off valve 3a and 4b can realize forward flow as shown in Figure 3 simultaneously; Otherwise, can realize the reverse flow of fluid.
At first, the electric heater outlet temperature is set at 450 ℃, infeeds ventilating gas gas, observe the variation of reaction bed temperature, start automatic control system simultaneously, carry out the switching of gas flow direction.When system's self-heating operation, close electric heater, simultaneously to infeeding heat transferring medium in the heat-obtaining device,, regulate the flow of heat transferring medium according to intrasystem variations in temperature, thus the operation of the safety and stability self-heating of the system of realization.
Embodiment one
Use above-mentioned design developed one the cover disposal ability be 20m
3The ventilating gas comprehensive treatment device of/h, its appearance and size are 934mm * 420mm * 120mm.In order to be well understood to the characteristic of ventilating gas treating apparatus under different operating modes more, in device, arranged 42 points for measuring temperature, see Fig. 4.When the entrance concentration of methane is 4000ppm, when the flow of air was 333.3L/min, (0.5min～1.5min) the reactor axial temperature distributed (Fig. 5) different switching frequencies down, and the axial temperature of reactor distributes and is typical " shape of a saddle " and distributes as can be seen; Temperature is controlled at 550 ℃ on the catalyst of the interior both sides of U-type reactor, and methane conversion can maintain more than 95%, sees Fig. 6.And the device pressure fall about 3kPa, specifically see Fig. 7.Per minute can produce 250 ℃ superheated steam 5 grams simultaneously, has the higher thermal efficiency.Heat storage, catalyst, middle heat-obtaining part and combustion tail gas outlet temperature all are cyclically-varying with the variation that flows in addition, see Fig. 8.
Embodiment two
Reaction unit and thermometric, pressure measurement scheme are with embodiment one.The entrance concentration of methane is 3000ppm, and the flow of air is 666.6L/min, when temperature is controlled at 650 ℃ of left and right sides on the catalyst of both sides in the U-type reactor, can realize that methane conversion reaches more than 98%; And per minute can produce 270 ℃ superheated steam 5 grams.The resistance drop of bed is specifically seen Fig. 7 about 5kPa.Axial temperature distributes and is " shape of a saddle " distribution with embodiment one in the reactor; Heat storage, catalyst, middle heat-obtaining part and combustion tail gas outlet temperature are cyclically-varying with embodiment one with the variation that flows to.
Embodiment three
Reaction unit and thermometric, pressure measurement scheme are with embodiment one.The entrance concentration of methane is 3000ppm, and the flow of air is 333.3L/min, and temperature is about 360 ℃ on the catalyst of left side in the U-type reactor, and the right side temperature can realize that methane conversion reaches about 90% about 550 ℃, see Fig. 6; And per minute can produce 200 ℃ superheated steam 3 grams.Axial temperature distributes and is " shape of a saddle " distribution with case study on implementation one in the reactor; Heat storage, catalyst, middle heat-obtaining part and combustion tail gas outlet temperature are cyclically-varying with embodiment one with the variation that flows to.
Embodiment four
Reaction unit and thermometric, pressure measurement scheme are with embodiment one.The entrance concentration of methane is 5000ppm, and the flow of air is 333.3L/min, when temperature is controlled at 590 ℃ of left and right sides on the catalyst of both sides in the U-type reactor, can realize that methane conversion reaches more than 96%, sees Fig. 6; And per minute can produce 271 ℃ superheated steam 6 grams.Axial temperature distributes and is " shape of a saddle " distribution with embodiment one in the reactor; Heat storage, catalyst, middle heat-obtaining part and combustion tail gas outlet temperature are cyclically-varying with embodiment one with the variation that flows to.
Claims (10)
1. a device that fully utilizes coal mine to ventilate mash gas is that two identical reactor outlet ends of structure connect into U type reactor by a heat-obtaining device;
This reactor inlet end parts is filled with honeycomb heat accumulation body;
This reactor outlet end is divided into beds;
Heat storage go out and beds between be furnished with electric heater;
The unstripped gas porch is provided with the conversion that valve group control gas flows at inside reactor;
Unstripped gas enters reactor, with catalyst generation catalytic combustion, carries out periodically switching " saddle-shape " bed temperature distribution in the realization response device that flows to of reacting gas by the valve group on beds, and combustion tail gas is drawn by the heat-obtaining device.
2. device as claimed in claim 1, wherein, reactor cross section is square or circular configuration, the reactor inlet end and the port of export are taper.
3. device as claimed in claim 1, wherein, the catalyst of employing is particle or integer catalyzer.
4. as claim 1 or 3 described devices, wherein, catalyst is noble metal or metal oxide catalyst.
5. device as claimed in claim 1, wherein, heat storage is the particle or the integral honeycomb ceramic heat storage body of high heat capacity.
6. device as claimed in claim 1, wherein, electric heater is made up of some groups of finned tubes.
7. device as claimed in claim 1, wherein, the heat-obtaining device is coil heat exchanger or plate wing electric heater.
8. device as claimed in claim 1, wherein, the valve group of control gas flow is pneumatic operated valve or magnetic valve.
9. device as claimed in claim 1, wherein, the reactor inlet end and the port of export are provided with cuboid or cylinder bodily form screen or sieve plate.
10. as each described device of claim 1-9, wherein, by some groups of U type combination of reactors.
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| CN110939933A (en) * | 2019-11-20 | 2020-03-31 | 中国科学院广州能源研究所 | Low-concentration gas heat-storage combustion system |
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