CN101319781A - Combustion of ultra-low concentration combustible gas and its thermal energy step utilization system - Google Patents
Combustion of ultra-low concentration combustible gas and its thermal energy step utilization system Download PDFInfo
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- CN101319781A CN101319781A CNA2008101502118A CN200810150211A CN101319781A CN 101319781 A CN101319781 A CN 101319781A CN A2008101502118 A CNA2008101502118 A CN A2008101502118A CN 200810150211 A CN200810150211 A CN 200810150211A CN 101319781 A CN101319781 A CN 101319781A
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Abstract
The invention relates to a system for the combustion and the heat energy cascade utilization of combustible gas with ultra low concentration. A magnet valve and a pipeline are formed into a gas circuit with periodically changed air flow direction, to be connected with a combustion chamber internally provided with heat storage medium and a heat exchanger; the heat transmission is realized between the gas and the heat storage medium and the heat exchanger. When the heat storage medium loads different catalyzer, lower initiation temperature can be realized; when the amount of the heat storage medium is sufficient, higher gas preheating temperature can be realized; through changing the amount of the catalyzer and the heat storage medium, higher operating temperature and lower combustion concentration limit can be realized, and through changing the category of the catalyzer and the commutation cycle of the magnet valve, better gas adaptability and load adjustment can be realized. Through the heat exchange of the working medium in the internal heat exchanger and the high-temperature gas after being burnt or through the high-temperature flue gas after the system is reacted, the utilization of the high grade heat energy can be realized; through reducing the exhaust fume temperature of the final product, the utilization of the low grade heat energy can be realized.
Description
Technical field
The invention belongs to the combustion apparatus technical field, particularly the burning of coal mine to ventilate mash gas and thermal energy step thereof utilize system.
Background technology
Gas is potential safety hazard maximum in the coal mining, and it is the mixture based on the multiple gases of methane (CH4); Wherein methane concentration is 85% gas, and calorific value is 34.6MJ/m3.According to statistics, 1,000,000 tons of death rates of the coal of China about 3 people in 2004, this level is more than 100 times of the U.S., more than 10 times of India.Wherein all be the accident that gas explosion causes of dying from more than 95%, gas explosion has caused tremendous loss for the ordinary production in colliery.
In the exploitation in colliery, for pre-anti-gas explosion, adopt the method for ventilation dilution usually, the concentration of gas is controlled at below 1%, this part gas is called as ventilating gas.Ventilating gas also is the huge low-grade energies of a kind of reserves, and methane concentration is 1% ventilating gas, and theoretical temperature combustion is 265 ℃.Though the concentration of gas only has an appointment 1% in the ventilating gas,, caused huge energy waste because discharge capacity is huge.According to the investigation that U.S. EPA (Environmental Protection Agency) is done, global VAM (Ventilation Air Methane) discharge capacity was 16.6Bm in 2000
3, Chinese VAM discharge capacity 6.5Bm
3, account for 39.2% of total amount.Estimate CH in 2010
4Discharge capacity will increase to 2,800 ten thousand t, and wherein 70% (China then is 90%) is from CH
4Concentration is lower than 1% coal mine to ventilate mash gas.According to China 1996 and carried out the investigation of national mine gas situation in 2000, the ventilating gas amount is respectively 10,600,000,000 m
3With 9,600,000,000 m
3, occupying the first in the world, the low heat valve of contained gas is equivalent to the low heat valve of 3,370 ten thousand t standard coals, if this part resource can be developed and utilized as the energy, this will play very important effect for the energy security that ensures China.
In addition, a large amount of fuel gas that discharge in iron and steel production and the petrochemical processing, generally all directly emptying or dischargings of burning back, its heat energy wastes, and is not fully utilized.
China's " industry security and environmental protection " (2002,28 (3)) introduced heating power two-way reaction device (Thermal Flow Reversal Reactor in, TFRR) operation principle, this reactor is divided into upper, middle and lower three parts, the middle part is the heat exchanger layer, and two parts are the heat exchange layers that can efficiently store and transmit heat that quartz sand or ceramic particle constitute up and down.When bringing into operation, use electrical heating elements that heat exchange layers is carried out preheating earlier, to reach the required temperature of ventilating gas burning, about more than 1000 ℃, feed ventilating gas then, ventilating gas is flowed through and is preheated in the process of a side heat exchange layers, reaches the temperature required generation oxidation reaction of burning, emits heat and continues to flow.Emit the part heat when flowing through the heat exchanger layer, arrive another heat exchange layers then and emit most of heat, the heat of storage burning back gas is to keep the bulk temperature in the combustion chamber.As time goes on, high temperature section in the reactor can constantly be offset to outlet side, the temperature of the heat exchange layers of inlet side can constantly reduce, for stable the carrying out that keeps burning, the flow direction of gas from top to bottom or from bottom to top need switched, fluctuateed back and forth at the reactor middle part to guarantee the high temperature section in the reactor.In order to improve the utilization efficiency of heat energy of reactor, need be controlled at a reasonable range switching time with flowing to, switching time is too short, means that the reactor heat-exchange time is too short, and import temperature can not be preheating to ignition temperature; Switching time is oversize, and it is too far away that high temperature section departs from the center, and the combustion product heat release can most of not absorbed by heat exchange layers, and exhaust gas temperature is too high, and these two all causes reactor that flame-out phenomenon takes place easily.
Because what TFRR adopted is quartz sand or ceramic particle, when gas flows through pressure drop bigger, need special supercharging equipment to overcome sometimes along the journey pressure drop, this has increased the complexity and the cost of investment of system.Simultaneously, because the heat transfer property of quartz sand or ceramic particle is relatively poor, the airflow-reversing time is longer, and this has caused its disposal ability less.In addition, because the heat energy that TFRR has only utilized the reacting gas of high temperature to emit does not reclaim the low grade heat energy in the smoke evacuation, efficiency of energy utilization is maximization not.
Catalysis heating power two-way reaction device (the Catalytic Flow Reversal Reactor that Canada's mineral products and Inst Energiteknik (CANMET) develop, CFRR) its structural design and the method for operation and TFRR are basic identical, reduce the ignition temperature of ventilating gas by adopting catalyst.But among the CFRR because adopt quartz sand and ceramic particle causes increasing special supercharging equipment, disposal ability is less and efficiency of energy utilization shortcoming such as does not maximize and still exists.In addition, because the design that CFRR adopts catalyst to separate with heat storage medium has caused more catalyst changeout difficulty, the gas bad adaptability.
The Hu Peng of Chinese University of Science and Technology flies to wait the bidirectional adverse current round reactor of invention, partition heat exchange by gas before using reacted gas and reacting, reach the purpose of pre-heating intaking and reduction exhaust gas temperature, though it is simple in structure, cost is lower, but exist gaseous species and concentration adaptability relatively poor, repacking is complicated, the more high shortcoming of cost.And should invention only be a kind of combustion reactor, not propose the comprehensive utilization scheme of heat energy.
The reciprocating multi-hole medium combustion high-temperature air generating system of people such as the Cen Kefa of Zhejiang University invention is though also can realize the purpose of overheavy firing and low pollutant emission.But it is characterized in that burner and heat storage medium are divided into independent two parts, heat storage medium only plays the effect of storage high-temperature flue gas partial heat energy.By the combustion gas switching that between both sides heat storage medium and burner, circulates, realize the multi-hole medium combustion generation high temperature air that combines with accumulation of heat.But this kind method for designing can increase the control complexity of system, and the insulation and the construction of system had higher requirement, also and the cascade utilization of the heat energy of being unrealized.
Deng Yangbo conciliates the porous medium super-thermal insulating burning device down that back and forth flows of luxuriant clear invention, though its also can realize low density gas keep burning certainly.But its principle is the fuel gas that only is applicable to that concentration ratio is higher, after lighting through igniter, keeps burning certainly by what reduce progressively that gas flow realizes low density gas.And be not suitable for original super low concentration combustible gas that just can not ignition.
The coal mine ventilation air methane oxidation device of people such as Chen Yiliang invention, though its structure is similar to the present invention, its principle is based on traditional oxidation reaction, with to the present invention is based on catalytic reaction different.And and undeclared coal mine methane or any low-concentration combustible gas of whether can only being applied to.
Summary of the invention
The burning and the thermal energy step thereof that the invention provides a kind of super low concentration combustible gas utilize system, not only can the fuel gas of super low concentration be burnt, and can carry out cascade utilization to the heat energy of its generation.
Technical scheme of the present invention is achieved in that
Blower fan links to each other with flow control valve via pipeline; Flow control valve and another flow control valve and concentration monitor epiphase connect; The concentration monitor table is connected with second magnetic valve with first magnetic valve; First magnetic valve links to each other with second magnetic valve; The 3rd magnetic valve links to each other with the 4th magnetic valve; The time relay connects control first magnetic valve and the 3rd magnetic valve; The time relay connects control second magnetic valve and the 4th magnetic valve; First magnetic valve, second magnetic valve, the 3rd magnetic valve, the 4th magnetic valve link to each other with reactor; Reactor in-built electrical heating element heater and another electrical heating elements, the honeycomb porous regenerator medium of appendix catalyst, temperature thermocouple bundle, heat exchanger; Pre-heat reclamation device links to each other with heat exchanger, the 3rd magnetic valve, the 4th magnetic valve.
But the honeycomb porous regenerator medium of appendix catalyst is selected the heat-storing material of 1000 ℃～1800 ℃ of heatproofs that the one-component that comprises high-alumina brick, silica brick, complex silicon carbide, magnesia brick, corundum, kaolin, cordierite or andalusite or multiple material mix for use, and exists uniform arbitrary shape through hole to make things convenient for gas to flow through.
Electrical heating elements is the heat tape of built-in electrically heated rod or the honeycomb porous regenerator medium that evenly heats the appendix catalyst.
Because the present invention has adopted the cellular heat storage medium of appendix catalyst, on the one hand because the existence of cellular through hole, crushing when having reduced gas flow can realize that native system is directly installed on the air exit of the ventilation shaft place or the steel chemical enterprise of mine, need not special supercharging equipment.On the other hand, owing to adopted the cellular heat storage medium of porous, the heat transfer efficiency between the gas-solid promotes greatly, has improved the disposal ability of this system.
Because the present invention on the through-hole wall of cellular heat storage medium, because the existence of porous on the inwall has increased specific area, can increase the appendix amount of catalyst with the catalyst appendix, further improves catalytic combustion efficient.Simultaneously, because adopt the catalysis of whole appendix formula, the kind of gas and the adaptability of concentration are improved a lot, if the combustion gas kind changes, the heat storage medium that only needs to change the appendix catalyst gets final product, and has saved transformation time and cost.
Because the present invention has adopted the cellular heat storage medium of appendix catalyst, if wish to reach higher operating temperature, further reduce the concentration limit of burning, the amount that only needs to increase heat storage medium gets final product; Simultaneously also realize reducing the purpose of the concentration limit of burning by the kind that changes catalyst.
Because the present invention not only can utilize the high-grade heat energy in reactor middle part, can also come preheating built-in heat exchanger working medium or hot water is provided by the low grade heat energy that reclaims tail flue gas, has realized the purpose that thermal energy step utilizes.
Cellular catalytic thermal storage medium and heat energy utilization scheme that system of the present invention adopts can not only realize reaching more elevated operating temperature and the purpose that reduces the concentration limit of burning, and can also reach the cascade utilization of heat energy.System of the present invention is good to the kind and the concentration adaptability of gas, and improvement cost is low, and the transformation means are convenient and swift.System of the present invention is applicable to the super low concentration combustible gas that comprises the combustible exhaust gas in coal mine to ventilate mash gas, natural gas, biogas, oil oil reservoir gas, blast furnace gas and iron and steel and the petrochemical iy produced.
Description of drawings
To be the present invention at the reactor middle part be provided with heat exchanger to Fig. 1 and the structural representation of waste-heat recovery device is set at afterbody.
Fig. 2 is that the present invention extracts the structural representation that the part high-temperature flue gas is done manual work and waste-heat recovery device is set at afterbody at the reactor middle part.
The present invention is described in further detail below in conjunction with accompanying drawing.
The specific embodiment
As shown in Figure 1, its system mainly comprises:
Blower fan 1 links to each other with flow control valve 2 via pipeline; Flow control valve 2 links to each other with concentration monitor table 4 with another flow control valve 3; Concentration monitor table 4 is connected with second magnetic valve 6 with first magnetic valve 5; First magnetic valve 5 links to each other with second magnetic valve 6; The 3rd magnetic valve 11 links to each other with the 4th magnetic valve 12; The time relay 13 connects control first magnetic valve 5 and the 3rd magnetic valve 11; The time relay 14 connects control second magnetic valve 6 and the 4th magnetic valve 12; First magnetic valve 5, second magnetic valve 6, the 3rd magnetic valve 11, the 4th magnetic valve 12 link to each other with reactor 15; Reactor 15 in-built electrical heating element heaters 7 and another electrical heating elements 8, the honeycomb porous regenerator medium 9 of appendix catalyst, temperature thermocouple bundle 10, heat exchanger 16; Pre-heat reclamation device 17 links to each other with heat exchanger 16, the 3rd magnetic valve 11, the 4th magnetic valve 12.
During use, starting electrical heating elements 7,8 earlier is heated to honeycomb porous regenerator medium 9 on the catalysis initiation temperature of fuel gas, and keep certain hour to guarantee that temperature is evenly constant in the whole reactor according to the measured temperature datas of temperature thermocouple bundle 10, after this close electrical heating elements.Be lower than the catalysis initiation temperature as reactor temperature in the reaction system course of work, can enable electrical heating elements once more and carry out thermal compensation.
Fuel gas enters the gas supply pipeline by flow valve 3, and control concentration by concentration monitor table 4, when contained air capacity is not enough in the fuel gas, can supply (supplying air capacity changes with the difference of the required combustion air of fuel gas) by the flow combustion air amount that fuel gas is required of air in the control and regulation blower fan 1, to guarantee the stable operation of entire reaction system.
With the mobile direction of fuel gas is example from top to bottom, magnetic valve 5,12 unlatchings this moment, and magnetic valve 6,11 cuts out.Gas flows to reactor 15 by magnetic valve 5, this moment, gas temperature was lower than the temperature of honeycomb porous regenerator medium 9, along with gas flows downward, top honeycomb porous regenerator medium 9 progressively is cooled, gas temperature constantly raises, when being increased to the catalysis initiation temperature, gas generation catalytic combustion combustion reaction is also emitted heat.This moment, the part heat was absorbed by the wall-cooling surface at middle part, and the working medium through preheating in the wall-cooling surface is heated, and led to the generating set generating.Gas constantly flows downward and heat release, and this moment, gas constantly was cooled, and bottom honeycomb porous regenerator medium 9 constantly is heated, until flow to magnetic valve 12 by outlet.Because this moment, exhaust gas temperature also had the part low grade heat energy, reclaim this part heat energy so can add the working medium that waste-heat recovery device 17 heat exchanger preheatings enter reactor middle part wall-cooling surface at afterbody.Final smoke evacuation is through the shell-and-tube heat exchanger emptying.
Along with constantly carrying out of reaction, import department's honeycomb porous regenerator medium 9 temperature can occur constantly reduces, exit honeycomb porous regenerator medium 9 temperature constantly raise, the situation that the high-temperature region of reaction is offset to the exit from the middle part, after this kind skew acquires a certain degree, the gas that might occur coming in can not be preheating to the catalysis initiation temperature or the gas heat release can not be caused the entire reaction system flame-out by bottom honeycomb porous regenerator medium 9 most of situations about absorbing.Therefore need switch the flow direction of gas by time relay controller 13,14, in certain zone, the middle part of reactor 15, do periodically skew with the high-temperature region that guarantees reaction.
Equally, when gas flow is flowed from bottom to top, magnetic valve 6,11 unlatchings this moment, magnetic valve 5,12 cuts out, and system work process is same as described above.
When quitting work, cut off earlier air-flow and supply with, re-use blower fan and whole system is purged 5min get final product.
System shown in Figure 2 mainly comprises:
Fuel gas supply line, blower fan 1, flow control valve 2,3, concentration monitor table 4, first, second, third, fourth magnetic valve 5,6,11,12, time relay controller 13,14, electrical heating elements 7,8, the honeycomb porous regenerator medium 9 of appendix catalyst, temperature thermocouple bundle 10, reactor 15, waste-heat recovery device 17, gas turbine 18.
Wherein gas combustion process is identical with system shown in Figure 1, difference is, in the high temperature reaction zone at reactor 15 middle parts, the high-temperature flue gas of extraction 50%～70% leads to gas turbine 18 generatings, the residual gas of bleeding is used for heating bottom honeycomb porous regenerator medium 9, and is used to provide the domestic hot-water via the shell-and-tube heat exchanger recovery smoke evacuation heat energy that is located at afterbody.The ratio of bleeding can not be too big or too little in this system, and the ratio of bleeding is excessive, and exit honeycomb porous regenerator medium 9 can not obtain enough heat compensations, is not enough to heat next air inlet to the catalysis initiation temperature, causes reaction system flame-out; Rate of air sucked in required is too small, and exhaust gas temperature is too high, and the waste-heat recovery device that is located at afterbody is not enough to absorb net quantity of heat, causes heat waste.
When quitting work, cut off earlier air-flow and supply with, re-use blower fan and whole system is purged 5min get final product.
Because the composition of some gas has certain fluctuation, the phenomenon that its required combustion air might occur supplying, therefore when the required air quantity not sufficient, may threaten the safe operation of system, so need guarantee the stable operation of whole system by the air mass flow that the Monitoring Data of concentration detection table 4 is controlled blower fan 1.
Because the present invention has adopted the honeycomb porous regenerator medium 9 of appendix catalyst, not only heat storage capacity is strong, the heat transfer efficiency height, and also thermal shock resistance is good, long service life.Because appendix is on the inwall of heat storage medium through hole during catalyst, there are a large amount of pores on this kind dielectric inner wall, increased specific area, improved the appendix amount of catalyst.Also appendix has strengthened the adaptability of gaseous species at the catalyst of gas with various simultaneously.In addition, the maintain and replace of this system is also simple and easy to do, and the cycle that only needs to change the kind of heat storage medium or change flow-reversal gets final product, and the low duration of cost is short.
In addition, system of the present invention also is used at the low grade heat energy in the smoke evacuation, has also improved whole utilization efficiency of heat energy.
System of the present invention designs at the present situation of methane mean concentration between 0.1%～1% in the coal mine to ventilate mash gas.Recycle at this part ventilating gas, not only can realize effective utilization of low-grade energy, can also exchange carbon for by reduction of discharging and remit and receive very big economic benefit and environmental benefit.
System of the present invention also is applicable to any fuel gas that can catalytic combustion system, these gases act as a fuel can not change the hot rerum natura of charge air flow, different fuel gas, just ignition temperature is different with caloric value, when combustion gas is not ventilating gas, the preheat temperature that only needs to change the kind of appendix catalyst and change heat storage medium gets final product, and its improvement cost is low, and is simple and easy to do.
Claims (3)
1. the burning of a super low concentration combustible gas and thermal energy step thereof utilize system, and this system comprises:
Blower fan (1) links to each other with flow control valve (2) via pipeline; Flow control valve (2) links to each other with concentration monitor table (4) with another flow control valve (3); Concentration monitor table (4) is connected with second magnetic valve (6) with first magnetic valve (5); It is characterized in that first magnetic valve (5) links to each other with second magnetic valve (6); The 3rd magnetic valve (11) links to each other with the 4th magnetic valve (12); The time relay (13) connects control first magnetic valve (5) and the 3rd magnetic valve (11); The time relay (14) connects control second magnetic valve (6) and the 4th magnetic valve (12); First magnetic valve (5), second magnetic valve (6), the 3rd magnetic valve (11), the 4th magnetic valve (12) link to each other with reactor (15); The honeycomb porous regenerator medium (9) of reactor (15) in-built electrical heating element heater (7) and another electrical heating elements (8), appendix catalyst, temperature thermocouple bundle (10), heat exchanger (16); Pre-heat reclamation device (17) links to each other with heat exchanger (16), the 3rd magnetic valve (11), the 4th magnetic valve (12).
2. the burning of super low concentration combustible gas according to claim 1 and thermal energy step thereof utilize system, it is characterized in that, the honeycomb porous regenerator medium (9) of appendix catalyst but select the one-component that comprises high-alumina brick, silica brick, complex silicon carbide, magnesia brick, corundum, kaolin, cordierite or andalusite for use or the heat-storing material of 1000 ℃～1800 ℃ of heatproofs that multiple material mixes, and exist uniform arbitrary shape through hole to make things convenient for gas to flow through.
3. the burning of super low concentration combustible gas according to claim 1 and thermal energy step thereof utilize system, it is characterized in that electrical heating elements (7,8) is built-in electrically heated rod or the heat tape that evenly heats the honeycomb porous regenerator medium (9) of appendix catalyst.
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| CNA2008101502118A CN101319781A (en) | 2008-06-30 | 2008-06-30 | Combustion of ultra-low concentration combustible gas and its thermal energy step utilization system |
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Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101839472A (en) * | 2010-04-16 | 2010-09-22 | 萧琦 | Method for reclaiming heat of ventilated gas oxidation device |
| CN101713535B (en) * | 2009-11-30 | 2011-05-18 | 重庆大学 | Burning method of gas fuel with ultra-low concentration |
| CN101518739B (en) * | 2009-03-31 | 2012-06-27 | 华南理工大学 | Integral type catalyst with heat storage function as well as preparation method and application thereof |
| CN109404960A (en) * | 2018-10-30 | 2019-03-01 | 中煤科工集团重庆研究院有限公司 | Gradient symmetry control method for vertical multi-bed RTO bell-shaped temperature zone |
| US10288348B2 (en) | 2014-01-10 | 2019-05-14 | Compass Minerals America Inc. | Method of drying salt and similar materials through the use of heat engine waste heat |
| CN110822458A (en) * | 2019-10-21 | 2020-02-21 | 山西大学 | Low-concentration gas steady-state catalytic oxidation device for waste heat step utilization |
| CN114804322A (en) * | 2022-04-29 | 2022-07-29 | 西安交通大学 | Integrated type integrated supercritical water oxidation reactor |
-
2008
- 2008-06-30 CN CNA2008101502118A patent/CN101319781A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101518739B (en) * | 2009-03-31 | 2012-06-27 | 华南理工大学 | Integral type catalyst with heat storage function as well as preparation method and application thereof |
| CN101713535B (en) * | 2009-11-30 | 2011-05-18 | 重庆大学 | Burning method of gas fuel with ultra-low concentration |
| CN101839472A (en) * | 2010-04-16 | 2010-09-22 | 萧琦 | Method for reclaiming heat of ventilated gas oxidation device |
| US10288348B2 (en) | 2014-01-10 | 2019-05-14 | Compass Minerals America Inc. | Method of drying salt and similar materials through the use of heat engine waste heat |
| CN109404960A (en) * | 2018-10-30 | 2019-03-01 | 中煤科工集团重庆研究院有限公司 | Gradient symmetry control method for vertical multi-bed RTO bell-shaped temperature zone |
| CN110822458A (en) * | 2019-10-21 | 2020-02-21 | 山西大学 | Low-concentration gas steady-state catalytic oxidation device for waste heat step utilization |
| CN114804322A (en) * | 2022-04-29 | 2022-07-29 | 西安交通大学 | Integrated type integrated supercritical water oxidation reactor |
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