CN208566676U - A kind of equipment improving gas utilization efficiency - Google Patents
A kind of equipment improving gas utilization efficiency Download PDFInfo
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- CN208566676U CN208566676U CN201820338085.8U CN201820338085U CN208566676U CN 208566676 U CN208566676 U CN 208566676U CN 201820338085 U CN201820338085 U CN 201820338085U CN 208566676 U CN208566676 U CN 208566676U
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C13/00—Apparatus in which combustion takes place in the presence of catalytic material
- F23C13/02—Apparatus in which combustion takes place in the presence of catalytic material characterised by arrangements for starting the operation, e.g. for heating the catalytic material to operating temperature
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/07—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases in which combustion takes place in the presence of catalytic material
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23C—METHODS OR APPARATUS FOR COMBUSTION USING FLUID FUEL OR SOLID FUEL SUSPENDED IN A CARRIER GAS OR AIR
- F23C13/00—Apparatus in which combustion takes place in the presence of catalytic material
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
- B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
- B01D53/0407—Constructional details of adsorbing systems
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B1/00—Methods of steam generation characterised by form of heating method
- F22B1/02—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers
- F22B1/18—Methods of steam generation characterised by form of heating method by exploitation of the heat content of hot heat carriers the heat carrier being a hot gas, e.g. waste gas such as exhaust gas of internal-combustion engines
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
- F22B31/00—Modifications of boiler construction, or of tube systems, dependent on installation of combustion apparatus; Arrangements of dispositions of combustion apparatus
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
- F22D1/00—Feed-water heaters, i.e. economisers or like preheaters
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22G—SUPERHEATING OF STEAM
- F22G1/00—Steam superheating characterised by heating method
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F22—STEAM GENERATION
- F22G—SUPERHEATING OF STEAM
- F22G3/00—Steam superheaters characterised by constructional features; Details of component parts thereof
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/08—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating
- F23G5/10—Incineration of waste; Incinerator constructions; Details, accessories or control therefor having supplementary heating electric
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G5/00—Incineration of waste; Incinerator constructions; Details, accessories or control therefor
- F23G5/44—Details; Accessories
- F23G5/46—Recuperation of heat
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G7/00—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals
- F23G7/06—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases
- F23G7/061—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating
- F23G7/063—Incinerators or other apparatus for consuming industrial waste, e.g. chemicals of waste gases or noxious gases, e.g. exhaust gases with supplementary heating electric heating
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/70—Organic compounds not provided for in groups B01D2257/00 - B01D2257/602
- B01D2257/702—Hydrocarbons
- B01D2257/7022—Aliphatic hydrocarbons
- B01D2257/7025—Methane
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2259/00—Type of treatment
- B01D2259/40—Further details for adsorption processes and devices
- B01D2259/40083—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption
- B01D2259/40088—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating
- B01D2259/4009—Regeneration of adsorbents in processes other than pressure or temperature swing adsorption by heating using hot gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/10—Waste heat recuperation reintroducing the heat in the same process, e.g. for predrying
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2206/00—Waste heat recuperation
- F23G2206/20—Waste heat recuperation using the heat in association with another installation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
- F23G—CREMATION FURNACES; CONSUMING WASTE PRODUCTS BY COMBUSTION
- F23G2900/00—Special features of, or arrangements for incinerators
- F23G2900/50213—Preheating processes other than drying or pyrolysis
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/20—Capture or disposal of greenhouse gases of methane
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P80/00—Climate change mitigation technologies for sector-wide applications
- Y02P80/10—Efficient use of energy, e.g. using compressed air or pressurized fluid as energy carrier
- Y02P80/15—On-site combined power, heat or cool generation or distribution, e.g. combined heat and power [CHP] supply
Abstract
A kind of equipment improving gas utilization efficiency, the equipment includes: coal bed gas delivery pipeline, methane normal pressure absorbing unit, catalyst warm-up unit and catalyst oxidation reactor；The catalyst oxidation reactor includes catalytic combustion unit, coal bed gas preheating unit and waste heat recovery unit；The catalyst warm-up unit is used to preheat the catalyst bed in the catalytic combustion unit；The entrance of the coal bed gas preheating unit is connected with the outlet of the coal bed gas delivery pipeline, and the outlet of the coal bed gas preheating unit is connected with the entrance of the catalytic combustion unit.The utility model may be implemented ultralow concentration gas and efficiently, economically utilize, to increase substantially coal bed gas efficiency.
Description
Technical field
The utility model belongs to clean energy technology field, and in particular to a kind of equipment for improving gas utilization efficiency.
Background technique
Coal bed gas is also referred to as gas, is a kind of clean energy resource, less currently with the coal bed gas got up, it is contemplated that national coal seam
The 13 planning ends that gas utilizes, also only 30% coal bed gas total resources can be utilized.As shown in Figure 1, concentration is lower than
10% gas (referred to as ultralow concentration gas), including wind resource assessment (concentration is 0.2% or so) are not all utilized, and straight
Run in and is put into atmosphere.
Currently, domestic coal mine, which is discharged into every year in the ultralow concentration gas of atmosphere, 300 billion cubic meter methane.If it
Use as fuel and can substitute nearly 100,000,000 tons of fire coals, 930,000 tons of reducing emission of sulfur dioxide, 520,000 tons of NOx, emission reduction particulate matter
1260000 tons.Methane is important greenhouse gases, and 300 billion cubic meter methane of discharge are equivalent to 5.5 hundred million tons of carbon dioxide of discharge.Cause
This, these gas of emission reduction have great meaning, and are used using these ultralow concentration gas as fuel, can more supplement state
The deficiency of interior deliverability of gas.
The concentration of ultralow concentration gas is low, air quantity conference increases the cost of gas utilization, influences gas utilization efficiency.Transformation
Ultralow concentration gas concentration can be improved in absorption (PSA) method, but huge to electricity consumed by ultralow concentration gas pressurization, therefore
It is economically infeasible.CN104014223A discloses a kind of ventilation air methane absorber, using temp.-changing adsorption method absorption wind row watt
Methane in this, wherein using many small filter cores, and the thinner thickness of adsorbent material, which is based on laboratory
Small-scale device experiment propose, many technical problems of Gonna breakthrough are gone back in large-scale industrial production.In addition, the absorber
It is only capable of methane concentration being increased to 1%, shows to be still not perfect in structure design.
CN103306717A discloses a kind of first Adsorption Concentration, then the scheme of heat accumulating type oxidation.The concentration of wind resource assessment
It is first concentrated to 1%, enters back into heat accumulating type oxidation device and aoxidizes, the heat that releases of gas oxidation generated electricity again, heat supply etc.
UTILIZATION OF VESIDUAL HEAT IN.
This method the problem is that:
1) gas waste is big.Methane oxidized apparatus needs to consume the 20% of whole gas, to maintain its 1100-1200 DEG C
Operation temperature.
2) heat utilization ratio is low.The device is discharged into the temperature of flue gas in atmosphere at 130 DEG C or more, has taken away a large amount of heat
Amount.
3) generating efficiency is low.The higher concentration gas being blended into wind resource assessment directly generates electricity in gas generator, often stands
Square rice can at least generate electricity 3.5kWh, and be blended into wind resource assessment, and every cubic metre of gas of steam-electric power processed is only capable of generating electricity
2.5kWh.Blending is more, and power generation loss is bigger.
4) device efficiency is low, takes up a large area.The a large amount of honeycomb ceramic heat accumulators of oxidation unit accumulate gas oxidation release
Heat out, equipment land occupation are larger.Domestic majority coal mine all build mountain area in, and level land is few, implements the cost of floor space of the technology very
It is high.
5) ultralow concentration gas utilizes dimension-limited system.Highly concentrated gas flow is mutually small in coal mine, and unstable, and wind
The flow of gas-removing is big, concentration is low.Do not have it is enough blend high concentration gas, influence the utilization (wind resource assessment of wind resource assessment
In methane total amount account for 50% or more of whole coal bed gas).
6) a large amount of solid-state castoffs, pollution environment are caused.Every regenerative oxidation device all uses tens cubic metres of honeycomb
Ceramic heat storage body.Heat storage total amount is at 1000 cubic metres or so used in the oxidation unit of one project.These heat storages take 1-2
Replacement is primary, causes a large amount of solid refuses, forms new environmental pollution.
7) investment of equipment is big, deficiency in economic performance.The investment of regenerative oxidation technology power generation is 1.1 ten thousand yuan/kW, not only much
Higher than 0.45 ten thousand yuan/kW of thermoelectricity, also above 0.65 ten thousand yuan/kW of low-concentration gas power generation, the investment repayment phase usually 6 years with
On.This also counteracts technology coal mine large-scale application at home.
In addition, the gas density in this method is lower (being lower than 1.0%), if gas density increases, in heat accumulating type device
Portion's temperature is difficult to control, and can burn device, therefore this method is technically left to be desired.
Utility model content
In order to solve the problems such as gas utilization in the prior art is at high cost, utilization efficiency is low, the utility model proposes
A kind of equipment economically and efficiently improving gas utilization efficiency.
In order to achieve the above objectives, the utility model proposes the equipment of raising gas utilization efficiency include:
Coal bed gas delivery pipeline, catalyst warm-up unit and catalyst oxidation reactor；The catalyst oxidation reactor includes
Catalytic combustion unit, coal bed gas preheating unit and waste heat recovery unit；
The catalyst warm-up unit is used to preheat the catalyst bed in the catalytic combustion unit；
The entrance of the coal bed gas preheating unit is connected with the outlet of the coal bed gas delivery pipeline, the coal bed gas preheating
The outlet of unit is connected with the entrance of the catalytic combustion unit；
In terms of the flow direction of coal bed gas, the catalytic combustion unit includes the end socket, gas distributor and catalysis set gradually
Agent bed；
The high-temperature flue gas that the catalytic combustion unit generates enters the waste heat recovery unit, with the cooling side of high-temperature gas
To meter, the waste heat recovery unit includes the steam generation section set gradually and boiler feedwater preheating section, and the boiler feedwater is pre-
Hot arc is connected with boiler feedwater pipeline, and boiler feedwater enters the steam generation after the boiler feedwater preheating section is preheated
Section, the steam of generation enter steam pipe network.
Preferably, the waste heat recovery unit is including further including steam superheating section, the steam of the steam generation section generation
Into the steam superheating section, the superheated steam of generation enters steam pipe network.
Preferably, the equipment includes methane normal pressure absorbing unit, and the methane normal pressure absorbing unit includes multiple absorption
Tower, the entrance of the adsorption tower is respectively with wind resource assessment pipeline and the high-temperature flue gas pipeline phase from the catalyst oxidation reactor
Even, the outlet of the adsorption tower is connected with the coal bed gas delivery pipeline and discharge tube respectively, on the wind resource assessment pipeline,
On the high-temperature flue gas pipeline, between the outlet and the coal bed gas delivery pipeline of the adsorption tower and the discharge tube
On be provided with valve.
Preferably, the catalyst warm-up unit includes the first air-introduced machine and electric heater, the entrance of the electric heater
It is connected with the outlet of first air-introduced machine, the outlet of the electric heater is connected with the entrance of the catalytic combustion unit.
Preferably, when the catalyst oxidation reactor is compact catalytic oxidation reactor, the catalyst warm-up unit is
The heating wire or electrically heated rod being built in the catalyst oxidation reactor.
Preferably, the equipment further includes the second air-introduced machine and airflow pipe, the outlet of the airflow pipe
It is connected with the second air-introduced machine entrance, the outlet of second air-introduced machine is connected with the entrance of the coal bed gas delivery pipeline.
Preferably, air filter is provided between the outlet and the coal bed gas delivery pipeline of second air-introduced machine.
Preferably, the waste heat recovery unit further includes the drum of separate vapour and liquid, and boiler feedwater is in the boiler
Feed-water preheating section through the drum enters the steam generation section after being preheated, and the mixture of the steam of generation and water returns to institute
It states drum to be separated, the steam isolated enters steam pipe network.
Preferably, the catalyst warm-up unit includes first filter, and the coal bed gas delivery pipeline includes the second mistake
Filter and fire arrester.
Preferably, the equipment further includes low concentration gas conveyance conduit, the low concentration gas conveyance conduit with it is described
Coal bed gas delivery pipeline is connected.
Compared with prior art, the utility model has the following characteristics:
1) gas utilization rate is improved.Under the action of catalyst, the operating temperature of reactor is dropped to 400 DEG C, gas oxygen
The whole of change releases, and does not consume.
2) heat utilization ratio improves.Exhaust gas temperature is 60 DEG C, the heat dissipation of device is reduced, and makes heat utilization ratio than heat accumulating type oxygen
Change technology improves 10%.
3) generating efficiency is high.Since apparatus function is highly integrated, for power generation heat ratio heat accumulating type oxidation technology more than
10%, generating efficiency improves.
4) it is discharged without solid-state castoff.Heat storage is used for a long time, and catalyst is renewable, does not form solid-state castoff, ring
Border is friendly.
5) economic benefit improves.The equipment manufacturing cost of new process reduces, land occupation be reduced to existing regenerative oxidation technology 1/4,
Project investment is reduced to the 1/2 of existing regenerative oxidation technology, therefore better economic benefit.
Detailed description of the invention
Fig. 1 is the utilization power of coal bed gas resource；
Fig. 2 is the flow chart of gas utilization method in the utility model；
Fig. 3 is the schematic diagram of equipment in the utility model embodiment.
Specific embodiment
For the purpose of this utility model, technical solution and advantage is more clearly understood, below in conjunction with specific embodiment, and
Referring to attached drawing, the utility model is described in further detail.
The utility model uses two core technologies, with new process route, realizes ultralow concentration gas efficiently, economically
It utilizes, to increase substantially coal bed gas efficiency, as shown in Figure 2:
1. adsorbing ultralow concentration gas at normal temperatures and pressures, and desorbed with temp.-changing adsorption method.It is dense to ultralow concentration gas
Degree improves 10 times, its concentration is increased to 2% or more.
2. directly being burnt using catalysis oxidation (Catalytic Oxider, CO) device (alternatively referred to as catalytic combustion system)
The gas of 2% concentrations above, and the heat 100% for aoxidizing gas releases.
By the process of new process, first ultralow concentration gas is concentrated, the gas after concentration is in catalytic combustion system
Heat is released, carries out steam-electric power and UTILIZATION OF VESIDUAL HEAT IN (including desorption under high temperature) with these heats.The land occupation of new process is existing
Regenerative oxidation technology 1/4, project investment be reduced to the 1/2 of existing regenerative oxidation technology, to realize the height of ultralow concentration gas
Effect utilizes, and the cost using ultralow concentration gas is greatly lowered.
The utility model proposes the equipment of raising gas utilization efficiency include: that coal bed gas delivery pipeline, catalyst are pre-
Hot cell and catalyst oxidation reactor；The catalyst warm-up unit includes the first air-introduced machine and electric heater, the catalysis oxygen
Changing reactor includes catalytic combustion unit, coal bed gas preheating unit and waste heat recovery unit；
The entrance of the electric heater is connected with the outlet of first air-introduced machine；
The entrance of the catalytic combustion unit is connected with the outlet of the electric heater；
The entrance of the coal bed gas preheating unit is connected with the outlet of coal bed gas delivery pipeline；
The entrance of the catalytic combustion unit is connected with the outlet of the coal bed gas preheating unit；
In terms of the flow direction of preheating gas or coal bed gas unstripped gas, the catalytic combustion unit include the end socket set gradually,
Gas distributor and catalyst bed；
The high-temperature flue gas that the catalytic combustion unit generates enters the waste heat recovery unit, with the cooling side of high-temperature gas
To meter, the waste heat recovery unit includes the steam generation section set gradually and boiler feedwater preheating section.The boiler feedwater is pre-
Hot arc is connected with boiler feedwater pipeline, and boiler feedwater enters the steam generation after the boiler feedwater preheating section is preheated
Section, the steam of generation enter steam pipe network.
When needing superheated steam, the waste heat recovery unit is including further including steam superheating section, with the drop of high-temperature gas
Warm telegoniometer, the waste heat recovery unit include the steam superheating section, steam generation section and boiler feedwater preheating section set gradually.
The steam that the steam generation section generates enters the steam superheating section, and the superheated steam of generation enters steam pipe network.
The pressure of each pipeline can adjust according to actual needs, such as steam superheating section can be high pressure steam superheat section,
Boiler feedwater can be high pressure boiler water supply.
The equipment further includes methane normal pressure absorbing unit, and the methane normal pressure absorbing unit includes multiple adsorption towers, institute
The entrance for stating adsorption tower is connected with wind resource assessment pipeline with the high-temperature flue gas pipeline from the catalyst oxidation reactor respectively, institute
The outlet for stating adsorption tower is connected with the coal bed gas delivery pipeline and discharge tube respectively, on the wind resource assessment pipeline, described
On high-temperature flue gas pipeline, between the outlet of the adsorption tower and the coal bed gas delivery pipeline and on the discharge tube
It is provided with valve.
The equipment further includes the second air-introduced machine and airflow pipe, the outlet of the airflow pipe and described the
Two air-introduced machine entrances are connected, and the second air-introduced machine outlet is connected with the entrance of the coal bed gas delivery pipeline.
The catalyst oxidation reactor can be the catalyst oxidation reactor that several are arranged in parallel.
The coal bed gas preheating unit is heat-exchanging tube bundle or plate heat exchanger.
According to the needs for generating steam, multiple groups heat exchange coil has been can be set in the steam generation section.
The waste heat recovery unit further includes the drum of separate vapour and liquid, and boiler feedwater is preheated in the boiler feedwater
Enter the steam generation section through the drum after Duan Jinhang preheating, the mixture of the steam of generation and water return the drum into
Row separation, the steam isolated enter steam pipe network.
Using the equipment processing coal bed gas method the following steps are included:
In warm-up phase, catalyst bed is preheated using catalyst warm-up unit, closes catalyst warm-up unit, is entered
Normal operation phase；
In normal operation phase, coal bed gas is preheated using coal bed gas preheating unit, the coal bed gas after preheating is successively passed through
Cross end socket, gas distributor is distributed to catalyst bed, make preheating after coal bed gas react under the effect of the catalyst, obtain height
Warm flue gas；
The high-temperature flue gas successively passes through steam superheating section, steam generation section and boiler feedwater preheating section and carries out waste heat time
It receives, after recycling heat using coal bed gas preheating unit, discharges low-temperature flue gas.In one embodiment, the equipment of the utility model
As shown in Figure 3.Including methane normal pressure absorbing unit, air-introduced machine, catalyst oxidation reactor, catalyst warm-up unit and matched pipe
The composition such as line, valve.
Methane normal pressure absorbing unit is made of the first adsorption tower 1 and the second adsorption tower 2, and one of tower is for adsorbing wind row
Methane in gas, and being discharged into atmosphere without the air of methane, another tower high-temperature flue gas is methane from adsorbent bed
It is desorbed on layer, the gas desorbed is mixed with the low concentration gas that needs utilize, then defeated to catalyst oxidation reactor 3
It send.
Adsorption tower switches to desorber after being filled methane, desorbs methane with high-temperature flue gas, the methane in desorber is complete
After complete solution is inhaled, by valve transfer at adsorption tower, adsorbed methane.
Two absorption towers have been used in the present embodiment, but can also use three towers or multitower form.
Normal pressure methane adsorbent in absorption tower can be molecular sieve, be also possible to MOF (metal-organic
Framework) material or other porous materials etc..High-performance adsorbent material can reduce the dosage of absorbent, reduce absorption tower
Cost.The shape of adsorbent, can be particle, be also possible to whole (honeycomb style) and various other forms.
It is adsorbed by normal pressure, improves the concentration of wind resource assessment, reduce the treating capacity of oxidation unit, substantially reduce oxygen
Disguise the quantity set, land occupation needed for reducing project.The electric energy of normal pressure absorption consumption is minimum, and the heat of desorption of methane comes from oxygen
Makeup is set, and outside heat is not needed.
Second air-introduced machine 4 dilution air into coal bed gas, control will enter the coal bed gas of catalyst oxidation reactor 3 as needed
Concentration avoids reactor from catalyst bed temperature runaway occur.
Catalyst oxidation reactor 3 realizes the catalysis burning of coal bed gas, and the heat of burning with infra-red radiation and high temperature cigarette
Gas convection current form, which passes to, to be needed to add hot medium.Coal bed gas is preheated using the heat that flue gas carries, waste heat recycling is realized, to mention
The thermal efficiency of high catalytic combustion device.
The structure of catalyst oxidation reactor 3 from bottom upwards be respectively end socket, gas distributor, catalyst bed, be used for
The waste heat recovery unit (such as tubular heat exchanger or plate heat exchanger) of waste heat recycling, the coal bed gas for preheating coal bed gas preheat single
The chimney of first (such as plate heat exchanger), flue gas discharge.It is cut after the end socket and gas distributor of the reacted device of coal bed gas along reactor
The flow velocity in face is uniform, makes its homogenous combustion on catalyst bed of coal bed gas, catalyst bed is avoided hot-spot occur.
Boiler feedwater after boiler feedwater preheating section is preheated through drum 5 enter steam generation section, the steam of generation and
The mixture of water returns to drum 5 and is separated, and the steam isolated enters steam superheating section and forms superheated steam, superheated steam into
Enter steam pipe network.
Catalyst in catalyst oxidation reactor 3 can be noble metal catalyst, the flue-gas temperature formed after catalysis burning
It is 500-600 DEG C.In practical application, metal oxide catalyst can also be used, the temperature of flue gas is up to 1000 DEG C, Huo Zhegeng
Change other types of catalyst into.
The air quantity of a usual returnairshaft is suitable with the present embodiment, and the flow of low concentration gas is also suitable with embodiment, therefore
One catalytic oxidizing equipment is set, is taken up little area, pipeline arrangement is simple, reduces investment outlay and maintenance cost.It is of course also possible to use more
A compact catalytic oxidation unit is used in parallel.
In one embodiment, catalyst warm-up device is made of the first air-introduced machine 6 and electric heater 7, for being catalyzed
Oxidation reactor 3 enters preheating catalyst bed before normal operating, enables coal bed gas in catalyst bed completely burned.Separately
It outside, can be using preheating catalysts beds such as built-in heating wire, electrically heated rods to small-sized catalytic combustion device.
To prevent the particle blocking catalyst in air and coal bed gas, need that suitable filter, example are arranged on pipeline
Such as air filter 8, fuel filter 9 and the filter 10 that goes into operation.Fire arrester 11 on coal bed gas delivery pipeline is avoided that catalysis
Burner causes coalbed methane system to explode after there is fire, explosion accident.
When using equipment catalysis burning coal layer gas, firstly, the catalyst bed of catalyst oxidation reactor 3 is preheated
To assigned temperature.Start the first air-introduced machine 6 and electric heater 7, hot wind is sent into reactor 3, the end socket and gas of reacted device
After distributor, hot wind equably preheating catalyst bed after catalyst bed is preheating to set temperature, closes the first air-introduced machine 6
With electric heater 7, and the valve V9 between closing electric heater outlet reactor in connecting pipeline.
V1, V6 are opened, V2, V5 are closed.Wind resource assessment enters the first adsorption tower 1 through V1, adsorbs the first from wind resource assessment
Air is discharged by V6 in alkane.Close V3, V4, V7, V8.
The second air-introduced machine 4 of starting, the dilution air into low concentration gas as needed make its concentration be lower than the explosion of methane
The limit.Low concentration gas enters the end socket and gas distributor of reactor 3 from pipeline, and catalysis combustion occurs on catalyst bed
Burn, in the form of infra-red radiation and high-temperature flue gas convective heat transfer gas oxidation heat transfer to boiler feedwater, steam is made, and
Make steam superheating.The coal bed gas that remaining heat transfer is preheated to needs realizes waste heat recycling.It discharges flue-gas temperature and is lower than 100
DEG C, with the latent heat in recovered flue gas, further increase the thermal efficiency of equipment.
Superheated steam enters the circulation of drum 5, and dry saturated steam enters steam pipe network, is used for steam turbine power generation.
Coal bed gas needs to be preheating to the temperature of setting, just can enter reactor, to maintain the temperature of catalyst bed, makes first
Lasting catalysis burning can occur on catalyst bed for alkane.
After first adsorption tower 1 is filled methane, V2, V5 are opened, closes V1, V6, high-temperature flue gas enters the first adsorption tower through V2
1, methane is desorbed, low concentration gas pipeline is entered by V5.V3, V8 are opened, the second adsorption tower 2 starts adsorbed methane.
By an adsorption cycle, the second adsorption tower 2 is filled methane, then by valve transfer, with high-temperature flue gas desorption the
Methane in two adsorption towers 2, with 1 adsorbed methane of the first adsorption tower.The methane desorbed can be made to be conveyed continuously in this way
In catalyst oxidation reactor, to realize steady, continuous catalyst combustion reaction in catalyst oxidation reactor.
The process flow of the utility model can utilize wind resource assessment and low concentration gas, the wind resource assessment after concentration simultaneously
Utilization is aoxidized in the same catalytic oxidizing equipment with low concentration gas.Process flow is simplified, project land occupation is reduced, reduces
Project investment.Wind resource assessment and low concentration gas are utilized simultaneously, can just use whole gas of coal mine, i.e. realization gas
The target of zero-emission.
Embodiment 1
The low concentration gas and methane concentration that one catalytic oxidizing equipment is 5% using the methane concentration of coal mine drainage be
0.2% wind resource assessment power generation.The flow of low concentration gas is 300Nm3/ min, the flow of wind resource assessment are 14000Nm3/ min,
35 tons of 4.3MPa are produced per hour, and 384 DEG C of steam, pushing turbine, power generation capacity is 6MW.It can using the technique of the utility model
All gas utilizations of current coal mine drainage to atmosphere are got up, zero drawing-off gas of coal mine is realized.
Adsorbent is molecular sieve 5A.Under normal pressure, every kg molecular sieve adsorbs 1g methane, and the adsorption/desorption period is 10min,
The molecular sieve dosage of each adsorption tower is 300 tons.Wind resource assessment is after adsorption tower, flow 1400Nm3/ min, concentration 2%
Low concentration gas.It is flow 1700Nm after the gas mixing of two kinds of concentration3/ min, concentration 2.5%.
Catalytic combustion reactor sectional dimension is 6.0m × 6.0m, and end socket shape is taper, and gas distributor uses two sections
Combined sieve plate constructional, quantity, spacing and the size of aperture by etc. the design of resistances principle.Catalyst is load 0.6w% noble metal
Integral catalyzer, noble metal is palladium, and carrier is the cordierite honeycomb ceramic of 200 mesh, catalyst amount 10m3This implementation
The steam pressure generated in example is higher, and waste heat recovery unit uses tubular heat exchanger.Coal bed gas (low concentration gas) preheating is single
Member is plate air preheater.
Firstly, opening valve V9, start the first air-introduced machine 6 and electric heater 7, hot wind is sent into reactor 3, reacted device
End socket and gas distributor after, hot wind equably preheating catalyst bed after catalyst bed is preheating to 400 DEG C, closes the
One air-introduced machine 6 and electric heater 7, and close the valve V9 between electric heater outlet and reactor in connecting pipeline.
Low concentration gas enters the end socket and gas distributor of reactor 3 from pipeline, and urges on catalyst bed
Change burning, the boiler feedwater of 5.6MPa is heated in the form of infra-red radiation and 550 DEG C of smoke convection heat transfers, the water that 4.3MPa is made steams
Gas.Flue gas after cooling transfers heat to coal bed gas in coal bed gas preheating unit.The discharge flue-gas temperature of this equipment controls
At 100 DEG C hereinafter, with the latent heat in recovered flue gas.
The data acquisition and control of catalyst oxidation reactor 3 is completed by Siemens S7-300 type PLC.
Compared with previous heat accumulating type method for oxidation, up to 2%, heating efficiency mentions the methane concentration in the utility model
Height, and idle air continuous oxidation do not need switching flow direction, and without regenerative structure, system is simple, steady, and failure rate is low；
Built in waste heat boiler, do not need to extract flue gas, waste heat boiler does not arrange 300-450 DEG C of flue gas, and heating efficiency is high, and does not need
Mixing machine mixes the flue gas of different temperatures；When using noble metal catalyst, flue-gas temperature is 400-600 DEG C, when using golden
When belonging to oxide catalyst, the temperature of flue gas is up to 1000 DEG C；It is different according to the desorption performance of adsorbent, it can be with appropriate adjustment solution
The temperature of smoking gas；Low-temperature flue gas temperature can be down to 60 DEG C.Above-mentioned technical advantage, which combines, makes the technology of the utility model
Scheme land occupation is only that the 1/4 of heat accumulating type oxidation, project investment is reduced to the 1/2 of regenerative oxidation technology, and heating efficiency is than storing
Hot type scheme is high by 20% or more.
The gas type that the utility model can utilize is covered currently without the coal bed gas resource being utilized, thus real
The zero-emission of existing coal mine gas, become domestic coal bed gas it is extensive, efficiently, the breakthrough of economic utilization technology.
Particular embodiments described above has carried out into one the purpose of this utility model, technical scheme and beneficial effects
Step is described in detail, it should be understood that the foregoing is merely specific embodiment of the utility model, are not limited to this reality
With novel, within the spirit and principle of the utility model, any modification, equivalent substitution, improvement and etc. done should all include
It is within the protection scope of the utility model.
Claims (10)
1. a kind of equipment for improving gas utilization efficiency characterized by comprising
Coal bed gas delivery pipeline, catalyst warm-up unit and catalyst oxidation reactor；The catalyst oxidation reactor includes catalysis
Fuel element, coal bed gas preheating unit and waste heat recovery unit；
The catalyst warm-up unit is used to preheat the catalyst bed in the catalytic combustion unit；
The entrance of the coal bed gas preheating unit is connected with the outlet of the coal bed gas delivery pipeline, the coal bed gas preheating unit
Outlet be connected with the entrance of the catalytic combustion unit；
In terms of the flow direction of coal bed gas, the catalytic combustion unit includes the end socket, gas distributor and catalyst bed set gradually
Layer；
The high-temperature flue gas that the catalytic combustion unit generates enters the waste heat recovery unit, with the cooling direction of high-temperature gas
Meter, the waste heat recovery unit include the steam generation section set gradually and boiler feedwater preheating section, the boiler feedwater preheating
Section is connected with boiler feedwater pipeline, and boiler feedwater enters the steam generation after the boiler feedwater preheating section is preheated
Section, the steam of generation enter steam pipe network.
2. equipment as described in claim 1, which is characterized in that the waste heat recovery unit further includes steam superheating section, described
The steam that steam generation section generates enters the steam superheating section, and the superheated steam of generation enters steam pipe network.
3. equipment as described in claim 1, which is characterized in that the equipment includes methane normal pressure absorbing unit, the methane
Normal pressure absorbing unit includes multiple adsorption towers, and the entrance of the adsorption tower is respectively with wind resource assessment pipeline and from the catalysis oxygen
Change reactor high-temperature flue gas pipeline be connected, the outlet of the adsorption tower respectively with the coal bed gas delivery pipeline and discharge tube
Be connected, on the wind resource assessment pipeline, on the high-temperature flue gas pipeline, the outlet of the adsorption tower and the coal seam letter shoot
Valve is provided between road and on the discharge tube.
4. equipment as described in claim 1, which is characterized in that the catalyst warm-up unit includes that the first air-introduced machine and electricity add
Hot device, the entrance of the electric heater are connected with the outlet of first air-introduced machine, and the outlet of the electric heater is urged with described
The entrance for changing fuel element is connected.
5. equipment as described in claim 1, which is characterized in that when the catalyst oxidation reactor is compact catalytic oxidation reaction
When device, the catalyst warm-up unit is the heating wire or electrically heated rod being built in the catalyst oxidation reactor.
6. equipment as described in claim 1, which is characterized in that the equipment further includes the second air-introduced machine and air delivery pipe
Road, the outlet of the airflow pipe are connected with the second air-introduced machine entrance, the outlet of second air-introduced machine with it is described
The entrance of coal bed gas delivery pipeline is connected.
7. equipment as claimed in claim 6, which is characterized in that the outlet of second air-introduced machine and the coal seam letter shoot
Air filter is provided between road.
8. equipment as described in claim 1, which is characterized in that the waste heat recovery unit further includes separate vapour and liquid
Drum, boiler feedwater enter the steam generation section through the drum after the boiler feedwater preheating section is preheated, and generate
Steam and the mixture of water return to the drum and separated, the steam isolated enters steam pipe network.
9. equipment as described in claim 1, which is characterized in that the catalyst warm-up unit includes first filter, described
Coal bed gas delivery pipeline includes the second filter and fire arrester.
10. equipment as described in claim 1, which is characterized in that the equipment further includes low concentration gas conveyance conduit, described
Low concentration gas conveyance conduit is connected with the coal bed gas delivery pipeline.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
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| CN201710631756.XA CN107490012A (en) | 2017-07-28 | 2017-07-28 | A kind of System and method for of VOCs catalysis oxidations |
| CN201710631756X | 2017-07-28 |
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| CN201710631756.XA Pending CN107490012A (en) | 2017-07-28 | 2017-07-28 | A kind of System and method for of VOCs catalysis oxidations |
| CN201820336050.0U Active CN208124326U (en) | 2017-07-28 | 2018-03-12 | A kind of catalytic oxidation system of low calorie fuels |
| CN201810203009.0A Pending CN108286705A (en) | 2017-07-28 | 2018-03-12 | A kind of device and method improving gas utilization efficiency |
| CN201810203010.3A Pending CN108458337A (en) | 2017-07-28 | 2018-03-12 | A kind of gas combustion apparatus of near zero pollutant discharge, method and its application |
| CN201820338108.5U Active CN208108077U (en) | 2017-07-28 | 2018-03-12 | A kind of gas combustion apparatus of near zero pollutant discharge |
| CN201810202540.6A Pending CN108343978A (en) | 2017-07-28 | 2018-03-12 | A kind of catalytic oxidation system and method for low calorie fuels |
| CN201820338085.8U Active CN208566676U (en) | 2017-07-28 | 2018-03-12 | A kind of equipment improving gas utilization efficiency |
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| CN201710631756.XA Pending CN107490012A (en) | 2017-07-28 | 2017-07-28 | A kind of System and method for of VOCs catalysis oxidations |
| CN201820336050.0U Active CN208124326U (en) | 2017-07-28 | 2018-03-12 | A kind of catalytic oxidation system of low calorie fuels |
| CN201810203009.0A Pending CN108286705A (en) | 2017-07-28 | 2018-03-12 | A kind of device and method improving gas utilization efficiency |
| CN201810203010.3A Pending CN108458337A (en) | 2017-07-28 | 2018-03-12 | A kind of gas combustion apparatus of near zero pollutant discharge, method and its application |
| CN201820338108.5U Active CN208108077U (en) | 2017-07-28 | 2018-03-12 | A kind of gas combustion apparatus of near zero pollutant discharge |
| CN201810202540.6A Pending CN108343978A (en) | 2017-07-28 | 2018-03-12 | A kind of catalytic oxidation system and method for low calorie fuels |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108286705A (en) * | 2017-07-28 | 2018-07-17 | 北京化工大学 | A kind of device and method improving gas utilization efficiency |
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| CN109163338A (en) * | 2018-06-26 | 2019-01-08 | 昆明理工大学 | A kind of method and device handling liquid nitrogen washing tail-gas |
| DE102018210910A1 (en) * | 2018-07-03 | 2020-01-09 | Thyssenkrupp Ag | Process to avoid VOC and HAP emissions from plants processing synthetic gas |
| CN109404936A (en) * | 2018-10-26 | 2019-03-01 | 青岛福轮科技有限公司 | A kind of smoke processing system and processing method |
| CN109519942A (en) * | 2018-12-11 | 2019-03-26 | 武汉理工大学 | A kind of accurate self-preheating type safety and energy-saving Regenerative Combustion System and method |
| CN110030567B (en) * | 2019-04-10 | 2023-11-07 | 中国船舶重工集团公司第七一八研究所 | Organic waste gas catalytic combustion integrated device |
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| CN110822745A (en) * | 2019-10-21 | 2020-02-21 | 山西大学 | By using supercritical CO2Ventilation air catalytic oxidation device with solar heat collection, heat storage and heating functions |
| CN110822458B (en) * | 2019-10-21 | 2021-07-27 | 山西大学 | Low-concentration gas steady-state catalytic oxidation device for waste heat step utilization |
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| CN113688505A (en) * | 2021-07-29 | 2021-11-23 | 北京化工大学 | Method, system and device for quickly optimizing air quality data |
| CN114719274B (en) * | 2022-04-15 | 2023-05-19 | 福州大学 | Reaction system for coupling countercurrent integral catalytic combustion and endothermic reaction |
| CN117732242A (en) * | 2023-07-14 | 2024-03-22 | 浙江大学 | Catalytic oxidation system for efficiently converting and removing VOCs based on double-steam-bag cooperation |
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2018
- 2018-03-12 CN CN201820336050.0U patent/CN208124326U/en active Active
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- 2018-03-12 CN CN201810203010.3A patent/CN108458337A/en active Pending
- 2018-03-12 CN CN201820338108.5U patent/CN208108077U/en active Active
- 2018-03-12 CN CN201810202540.6A patent/CN108343978A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108286705A (en) * | 2017-07-28 | 2018-07-17 | 北京化工大学 | A kind of device and method improving gas utilization efficiency |
Also Published As
| Publication number | Publication date |
|---|---|
| CN108343978A (en) | 2018-07-31 |
| CN108458337A (en) | 2018-08-28 |
| CN208108077U (en) | 2018-11-16 |
| CN108286705A (en) | 2018-07-17 |
| CN107490012A (en) | 2017-12-19 |
| CN208124326U (en) | 2018-11-20 |
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