CN102703150B - Dual-fluidized bed low-concentration methane concentrating method and system thereof - Google Patents
Dual-fluidized bed low-concentration methane concentrating method and system thereof Download PDFInfo
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Abstract
The invention discloses a dual-fluidized bed low-concentration methane concentrating method. The dual-fluidized bed low-concentration methane concentrating method comprises the following steps: firstly, adsorbing low-concentration methane in a bubbling fluidized bed adsorption reactor; secondly, making part of adsorbing granules enter a fast-bed desorption reactor for desorbing and enter a cyclone separator after desorption; and finally, performing gas-solid separation in the cyclone separator, making the adsorbing granules enter the bubbling fluidized bed adsorption reactor for reuse, and making a mixed gas consisting of steam and methane enter a condensate separator for separating out high-concentration methane. The invention further discloses a dual-fluidized bed low-concentration methane concentrating system. Through high-pressure adsorption and high-temperature desorption in the bubbling fluidized bed adsorption reactor and the fast-bed desorption reactor with different functions, methane in low-concentration coal bed gas is concentrated and purified, and efficient utilization of the coal bed gas in a mining area and environmental protection are realized.
Description
Technical field
The present invention relates to a kind of low-concentration methane concentrated method and system thereof, mainly be applicable to low concentration coal-bed gas and other contains the concentrated of low-concentration methane gas and purifies.
Background technology
Along with the continuous growth of energy demand, the distributed low-grade energy of development utilization becomes save energy, solves one of main path of current energy dilemma, and coal bed gas resource widely distributed, that reserves are abundant provides reliable source of the gas to guarantee.China's coal bed gas resource is approximately 36.7 tcms, and is suitable with natural gas reserves, occupies third place in the world.It is calculated that, 1000 cubic metres of coal-seam gas are equivalent to 1 ton of standard coal, estimate that accordingly the coal-seam gas reserves of China are equivalent to 35,000,000,000 tons of standard coals or 24,000,000,000 tons of oil.
At present, for methane concentration higher than the utilization that can directly act as a fuel of 35% coal-seam gas.But often effectively do not utilize lower than 30% part for methane concentration, but direct dilution discharge is in atmosphere.The coal-seam gas that is discharged in atmosphere has not only caused the huge waste of the energy, and has aggravated topsoil and Greenhouse effect.The methane of unit mass affects GWP(Global Warming Potential to the atmosphere Greenhouse effect) be 21.5 times of carbonic acid gas, be 7 times of carbonic acid gas to the destructiveness of ozonosphere.Therefore, the comprehensive of the coal-seam gas of lower concentration effectively utilizes for improving and Optimization of Energy Structure, reduces topsoil and has important economy and environment protection significance.
In low concentration coal-bed gas methane content is often lower than 30%, and in mine air-lack mash gas, methane content is even lower than 1%, and the amount of adopting fluctuation is larger, and reserves distribute and disperse, and Financial cost is high if adopt pipe-line transportation system to provide and deliver, and inconvenience is safeguarded.Therefore, industrially often this directly long distance transportation is separated concentration as the low concentration coal-bed gas that civilian and industrial raw material use, in order to realize safety, convenient, economic remote conveying.
Mainly contain following several method for low-concentration methane gas concentrated: low-temperature deep partition method, membrane separation process and adsorption-desorption method.Wherein, low-temperature deep partition method gas product methane concentration is high, but device is complicated, and facility investment is large, C0
2, impurity easy blocking pipe when low temperature fractionation such as water, first remove complex process; Though membrane separation process technology equipment is simple, the operation less investment, true testing the stage still, also there is a big difference from industrial applications; The adsorption-desorption method comprises two processes of adsorption and desorption regeneration, namely utilizes boost (or cooling), step-down (or intensification) to realize the sorption and desorption sepn process to methane.The adsorption-desorption method has that energy consumption is low, the sorbent material cost is than the advantage such as low, that initial investment is few, running period is short, the gas processing amount is large, so utilize the technology of adsorption-desorption method concentrating low-concentration coal-seam gas relatively ripe.Research for the adsorption-desorption method at present mainly concentrates on pressure-swing adsorption concentration methane in tower,, for guaranteeing continuous concentration purification methane, often needs the alternation of many group adsorption towers, has both increased facility investment, has increased again floor space.
Summary of the invention
For above shortcomings in prior art, one of purpose of the present invention is to provide a kind of double-fluidized-bed low-concentration methane concentration method of realizing the efficient utilization of mining area coal-seam gas and environment protection.
Two of purpose of the present invention is to provide a kind of simple in structure, double-fluidized-bed low-concentration methane concentration systems that cost of investment is low.
One of purpose of the present invention is achieved by the following technical solution:
Double-fluidized-bed low-concentration methane concentration method, the method comprises the steps:
A, will contain in the coal-seam gas input bubbling fluidized bed adsorptive reactor of low-concentration methane, make the absorbent particles in the bubbling fluidized bed adsorptive reactor be in the bubbling fluidization state, be adsorbed the absorption of agent particle under the pressure-acting of low-concentration methane 0.3 ~ 0.7MPa in the bubbling fluidized bed adsorptive reactor, the coal-seam gas after absorption is discharged the bubbling fluidized bed adsorptive reactor through back pressure valve; The coal-seam gas of described low-concentration methane refers to that the methane volume content is in 1 ~ 30% coal-seam gas;
B, part absorbent particles fall to J type material returning valve in the effect of bubbling fluidization state, pass into water vapour as the loosening wind of fluidisation in J type material returning valve, under the loosening wind action of fluidisation, the absorbent particles in J type material returning valve falls in fast bed desorption reactor; The outside wall surface of fast bed desorption reactor arranges electric heater, and passes into water vapour as fluidized wind in fast bed desorption reactor, and fast bed desorption reactor is under 200 ~ 400 ℃ of conditions; Desorption occurs in absorbent particles in fast bed desorption reactor; After desorption, fast bed desorption inside reactor divides absorbent particles under the fluidisation wind action, through riser tube, takes fast bed desorption reactor out of, enters in cyclonic separator;
C, carry out gas solid separation in cyclonic separator after, absorbent particles after desorption falls to the sorbent material refrigerating unit, in the sorbent material refrigerating unit, adopt recirculated water to carry out cooling to absorbent particles, cooled absorbent particles enters in the absorption agent holder after variable valve, control by the particle control valve of regulating absorption agent holder bottom the amount that enters solid sorbent particles in the bubbling fluidized bed adsorptive reactor, make the solid sorbent particles that enters in the bubbling fluidized bed adsorptive reactor be repeated to utilize; The mixed gas that water vapour after cyclonic separator separates and methane form enters condensation separator, adopt recirculated water to carry out cooling to mixed gas in condensation separator, water vapour is condensed into liquid water, is separated after methane is cooling, forms the high density methane product.
As a preferred embodiment of the present invention, described bubbling fluidized bed adsorptive reactor is divided into left and right two portions by the sub-material dividing plate that vertically arranges in it, the particle control valve is positioned at the right part top of bubbling fluidized bed adsorptive reactor, and described J type material returning valve is positioned at the left part below of bubbling fluidized bed adsorptive reactor.
Two of purpose of the present invention is achieved by the following technical solution:
Double-fluidized-bed low-concentration methane concentration systems, comprise bubbling fluidized bed adsorptive reactor, J type material returning valve, fast bed desorption reactor, riser tube, cyclonic separator, sorbent material refrigerating unit, variable valve, sorbent material storer, particle control valve, condensation separator and vapour generator; Fill absorbent particles in described bubbling fluidized bed adsorptive reactor, the outside wall surface of described fast bed desorption reactor arranges electric heater; Described bubbling fluidized bed adsorptive reactor is connected with fast bed desorption reactor by J type material returning valve, fast bed desorption reactor is connected with cyclonic separator by riser tube, the outlet at bottom of described cyclonic separator is connected with the import of sorbent material refrigerating unit, the outlet of described sorbent material refrigerating unit is connected with the import of sorbent material storer by variable valve, and the outlet of described sorbent material storer is connected with the bubbling fluidized bed adsorptive reactor by the particle control valve; The air outlet, top of described cyclonic separator is connected with condensation separator, the air outlet of described condensation separator is high density methane delivery port, the liquid outlet of condensation separator is connected with the import of vapour generator, and the outlet of described vapour generator is connected with fast bed desorption reactor with J type material returning valve respectively.
As a preferred embodiment of the present invention, described sorbent material refrigerating unit adopts water recirculator.
As another kind of preferred version of the present invention, solid drier is filled in the air outlet of described condensation separator.
As another preferred version of the present invention, the particle diameter of described absorbent particles is 300 ~ 600 μ m.
As a modification of the present invention scheme, described condensation separator adopts water recirculator.
As another improvement project of the present invention, the pneumatic outlet of described bubbling fluidized bed adsorptive reactor is provided with back pressure valve.
Compared with prior art, double-fluidized-bed low-concentration methane concentration method of the present invention and system thereof have the following advantages:
1, the present invention adopts absorbent particles adsorption of Low Concentration methane; adopt respectively the method for High Pressure Absorption and desorption under high temperature in the different bubbling fluidized bed adsorptive reactor of function and fast bed desorption reactor; the concentrated purification of realization to methane in low concentration coal-bed gas, realized efficient utilization and the environment protection of mining area coal-seam gas simultaneously.
2, this system is mainly completed by two different reactors of function of bubbling fluidized bed adsorptive reactor and fast bed desorption reactor, and is simple in structure, cost of investment is low.
3, adopt the fluidizing agent of overheated steam as fast bed desorption reactor, under certain hot conditions, can effectively avoid the absorption of sorbent material to water vapour; Under certain hot conditions, can prevent that water vapour and methane from reacting simultaneously; Water vapour easily separates with methane.
Description of drawings
Fig. 1 is the structural representation of double-fluidized-bed low-concentration methane concentration systems.
In figure: 1-fast bed desorption reactor; 2-electric heater; 3-riser tube; 4-cyclonic separator; 5-sorbent material refrigerating unit; 6-variable valve; 7-adsorbent storage storage; 8-particle control valve; 9-back pressure valve; 10-bubbling fluidized bed adsorptive reactor; 11-sub-material dividing plate; 12-J type material returning valve; 13-condensation separator; 14-vapour generator.
Embodiment
Below in conjunction with the drawings and specific embodiments, the present invention is described in further detail.
Double-fluidized-bed low-concentration methane concentration method, the method comprise the steps: A, will contain in the coal-seam gas input bubbling fluidized bed adsorptive reactor 10 of low-concentration methane, as shown in Figure 1.Make the absorbent particles in bubbling fluidized bed adsorptive reactor 10 be in the bubbling fluidization state, be adsorbed the absorption of agent particle under the pressure-acting of low-concentration methane 0.3～0.7MPa in bubbling fluidized bed adsorptive reactor 10, the coal-seam gas that does not contain or contain less methane after absorption is discharged bubbling fluidized bed adsorptive reactor 10 through back pressure valve 9.The coal-seam gas of low-concentration methane refers to that the methane volume content is in 1 ~ 30% coal-seam gas.
B, part absorbent particles (mainly having referred to adsorb the larger absorbent particles of methane density) fall to J type material returning valve 12 in the effect of bubbling fluidization state, pass into water vapour as the loosening wind of fluidisation in J type material returning valve 12, under the loosening wind action of fluidisation, the absorbent particles in J type material returning valve 12 falls in fast bed desorption reactor 1.The outside wall surface of fast bed desorption reactor 1 arranges electric heater 2, and pass into water vapour as fluidized wind in fast bed desorption reactor 1, fast bed desorption reactor 1 is under the hot conditions of 200 ~ 400 ℃, can effectively avoid the absorption of sorbent material to water vapour, simultaneously can prevent that water vapour and methane from reacting, water vapour easily separates with methane.Absorbent particles is in the interior generation desorption of fast bed desorption reactor 1.After desorption, the interior part absorbent particles of fast bed desorption reactor 1 under the fluidisation wind action, is taken fast bed desorption reactor 1 out of through riser tube 3, enters in cyclonic separator 4.
C, carry out gas solid separation in cyclonic separator 4 after, absorbent particles after desorption falls to sorbent material refrigerating unit 5, in sorbent material refrigerating unit 5, adopt recirculated water to carry out cooling to absorbent particles, cooled absorbent particles enters in absorption agent holder 7 after variable valve 6, control by the particle control valve 8 of regulating absorption agent holder 7 bottoms the amount that enters solid sorbent particles in bubbling fluidized bed adsorptive reactor 10, make the solid sorbent particles that enters in bubbling fluidized bed adsorptive reactor 10 be repeated to utilize.The mixed gas that water vapour after cyclonic separator 4 separates and methane form enters condensation separator 13, adopt recirculated water to carry out cooling to mixed gas in condensation separator 13, water vapour is condensed into liquid water, is separated after methane is cooling, forms the high density methane product.
Bubbling fluidized bed adsorptive reactor 10 is divided into left and right two portions by the sub-material dividing plate 11 of vertical setting, and particle control valve 8 is positioned at the right part top of bubbling fluidized bed adsorptive reactor 10, and J type material returning valve 12 is positioned at the left part below of bubbling fluidized bed adsorptive reactor 10.This sub-material dividing plate 11 can prevent from directly entering J type feed back seal valve 12 from the absorbent particles that particle control valve 8 falls.
Double-fluidized-bed low-concentration methane concentration systems, as shown in Figure 1, comprise that bubbling fluidized bed adsorptive reactor 10, J type material returning valve 12, fast bed desorption reactor 1, riser tube 3, cyclonic separator 4, sorbent material refrigerating unit 5(sorbent material refrigerating unit 5 adopts water recirculators), variable valve 6, sorbent material storer 7, particle control valve 8, condensation separator 13(condensation separator 13 adopt water recirculators) and vapour generator 14.The interior filling absorbent particles of bubbling fluidized bed adsorptive reactor 10 is (in the present embodiment, the particle diameter of selecting absorbent particles is 300 ~ 600 μ m), the pneumatic outlet of bubbling fluidized bed adsorptive reactor 10 is provided with back pressure valve 9, and the outside wall surface of fast bed desorption reactor 1 arranges electric heater 2.Bubbling fluidized bed adsorptive reactor 10 is connected with fast bed desorption reactor 1 by J type material returning valve 12, fast bed desorption reactor 1 is connected with cyclonic separator 4 by riser tube 3, the outlet at bottom of cyclonic separator 4 is connected with the import of sorbent material refrigerating unit 5, the outlet of sorbent material refrigerating unit 5 is connected with the import of sorbent material storer 7 by variable valve 6, and the outlet of sorbent material storer 7 is connected with bubbling fluidized bed adsorptive reactor 10 by particle control valve 8.The air outlet, top of cyclonic separator 4 is connected with condensation separator 13, the air outlet of condensation separator 13 is that (solid drier is filled in air outlet to high density methane delivery port, solid drier carries out drying treatment to the concentrated methane of high density), the liquid outlet of condensation separator 13 is connected with the import of vapour generator 14, and the outlet of vapour generator 14 is connected and is connected with fast bed desorption reactor with J type material returning valve 12 respectively.
Double-fluidized-bed low-concentration methane concentration systems is used for the concentrating and separating of low concentration coal-bed gas methane, by adopting the sorbent material that methane is had absorption, make the adsorption and desorption of methane complete in bubbling fluidized bed adsorptive reactor 10 and fast bed desorption reactor 1 respectively, thereby realize the concentrating and separating of methane.
The working process of this system is as follows: 1. before system started operation, 2 pairs of fast bed desorption reactors 1 of opening electric heater heated, and avoid directly passing into overheated steam, met suddenly the condensation knot and the damage sorbent material; , until in bed, temperature, higher than 100 ℃, is closed electric heater 2, pass into simultaneously overheated steam, fast bed desorption reactor 1 and riser tube 3 are carried out emptying process, in order to avoid have influence on the concentration of separating rear methane, until drain air, i.e. preparation work before completion system normal operation; Store simultaneously the absorbent particles of certain altitude in sorbent material refrigerating unit 5, can prevent that the gas in bubbling fluidized bed adsorptive reactor 10 from leaking.when 2. system is normally moved, beginning passes into low concentration coal-bed gas in bubbling fluidized bed adsorptive reactor 10, carry out adsorption process, at this moment, absorbent particles in bubbling fluidized bed adsorptive reactor 10 (adsorbs the methane in coal-seam gas under 0.3 ~ 0.7MPa) at high pressure, the density of adsorbing enough methane becomes large absorbent particles and is deposited in bubbling fluidized bed adsorptive reactor 10 bottoms, because making the larger absorbent particles of bottom density, the existence of sub-material dividing plate 11 enters J type material returning valve 12 around the lower end of sub-material dividing plate 11, flow into again in fast bed desorption reactor 1.3. in the fast bed desorption reactor 1 of high temperature (200 ~ 400 ℃), methane desorbs from absorbent particles, through riser tube 3, after separating by cyclonic separator 4, absorbent particles after desorb enters in sorbent material refrigerating unit 5 cooling, variable valve 6 is by the switching of its valve of Temperature Feedback regulating and controlling in sorbent material refrigerating unit 5, thereby control the amount that enters the absorbent particles in adsorbent storage storage 7, reenter in bubbling fluidized bed adsorptive reactor 10 and adsorb by particle control valve 8 finally.4. the high density methane vapor gas mixture after separating by cyclonic separator 4, enter condensation separator 13, and this condensation separator 13 adopts recirculated water as refrigerant, and cooled condensed water produces overheated steam by vapour generator 14.Finally, obtain the high density methane gas from the pneumatic outlet of condensation separator 13.In adsorption process, can regulate pressure and adsorption particle total amounts in bubbling fluidized bed adsorptive reactor 10 by the aperture of adjusting back pressure valve 9 and the aperture of particle control valve 8, to meet different operation conditions, efficiency optimizes the system operation.
Explanation is finally, above embodiment is only unrestricted in order to technical scheme of the present invention to be described, although with reference to preferred embodiment, the present invention is had been described in detail, those of ordinary skill in the art is to be understood that, can modify or be equal to replacement technical scheme of the present invention, and not breaking away from aim and the scope of the technical program, it all should be encompassed in the middle of claim scope of the present invention.
Claims (6)
1. double-fluidized-bed low-concentration methane concentration method, is characterized in that, the method comprises the steps:
A, will contain in the coal-seam gas input bubbling fluidized bed adsorptive reactor (10) of low-concentration methane, make the absorbent particles in bubbling fluidized bed adsorptive reactor (10) be in the bubbling fluidization state, be adsorbed the absorption of agent particle under the pressure-acting of low-concentration methane 0.3 ~ 0.7MPa in bubbling fluidized bed adsorptive reactor (10), the coal-seam gas after absorption is discharged bubbling fluidized bed adsorptive reactor (10) through back pressure valve (9); The coal-seam gas of described low-concentration methane refers to that the methane volume content is in 1～30% coal-seam gas;
B, part absorbent particles fall to J type material returning valve (12) in the effect of bubbling fluidization state, pass into water vapour as the loosening wind of fluidisation in J type material returning valve (12), under the loosening wind action of fluidisation, the absorbent particles in J type material returning valve (12) falls in fast bed desorption reactor (1); The outside wall surface of fast bed desorption reactor (1) arranges electric heater (2), and passes into water vapour as fluidized wind in fast bed desorption reactor (1), and fast bed desorption reactor (1) is under 200 ~ 400 ℃ of conditions; Desorption occurs in absorbent particles in fast bed desorption reactor (1); After desorption, the interior part absorbent particles of fast bed desorption reactor (1) under the fluidisation wind action, is taken fast bed desorption reactor (1) out of and enters in cyclonic separator (4) through riser tube (3);
C, carry out gas solid separation in cyclonic separator (4) after, absorbent particles after desorption falls to sorbent material refrigerating unit (5), in sorbent material refrigerating unit (5), adopt recirculated water to carry out cooling to absorbent particles, cooled absorbent particles enters in absorption agent holder (7) after variable valve (6), control by the particle control valve (8) of regulating absorption agent holder (7) bottom the amount that enters solid sorbent particles in bubbling fluidized bed adsorptive reactor (10), make the solid sorbent particles that enters in bubbling fluidized bed adsorptive reactor (10) be repeated to utilize, the mixed gas that water vapour after cyclonic separator (4) separates and methane form enters condensation separator (13), adopt recirculated water to carry out cooling to mixed gas in condensation separator (13), water vapour is condensed into liquid water, be separated after methane is cooling, form the high density methane product,
Described bubbling fluidized bed adsorptive reactor (10) is divided into left and right two portions by the sub-material dividing plate (11) that vertically arranges in it, particle control valve (8) is positioned at the right part top of bubbling fluidized bed adsorptive reactor (10), described J type material returning valve (12) is positioned at the left part below of bubbling fluidized bed adsorptive reactor (10), and described back pressure valve (9) is positioned at the left part top of bubbling fluidized bed adsorptive reactor (10).
2. double-fluidized-bed low-concentration methane concentration systems, it is characterized in that, comprise bubbling fluidized bed adsorptive reactor (10), J type material returning valve (12), fast bed desorption reactor (1), riser tube (3), cyclonic separator (4), sorbent material refrigerating unit (5), variable valve (6), sorbent material storer (7), particle control valve (8), condensation separator (13) and vapour generator (14), fill absorbent particles in described bubbling fluidized bed adsorptive reactor (10), the outside wall surface of described fast bed desorption reactor (1) arranges electric heater (2), described bubbling fluidized bed adsorptive reactor (10) is connected with fast bed desorption reactor (1) by J type material returning valve (12), fast bed desorption reactor (1) is connected with cyclonic separator (4) by riser tube (3), the outlet at bottom of described cyclonic separator (4) is connected with the import of sorbent material refrigerating unit (5), the outlet of described sorbent material refrigerating unit (5) is connected with the import of sorbent material storer (7) by variable valve (6), the outlet of described sorbent material storer (7) is connected with bubbling fluidized bed adsorptive reactor (10) by particle control valve (8), the air outlet, top of described cyclonic separator (4) is connected with condensation separator (13), the air outlet of described condensation separator (13) is high density methane delivery port, the liquid outlet of condensation separator (13) is connected with the import of vapour generator (14), and the outlet of described vapour generator (14) is connected 1 with J type material returning valve (12) with fast bed desorption reactor respectively) be connected, the pneumatic outlet of described bubbling fluidized bed adsorptive reactor (10) is provided with back pressure valve (9), described bubbling fluidized bed adsorptive reactor (10) is divided into left and right two portions by the sub-material dividing plate (11) that vertically arranges in it, particle control valve (8) is positioned at the right part top of bubbling fluidized bed adsorptive reactor (10), described J type material returning valve (12) is positioned at the left part below of bubbling fluidized bed adsorptive reactor (10), and described back pressure valve (9) is positioned at the left part top of bubbling fluidized bed adsorptive reactor (10).
3. double-fluidized-bed low-concentration methane concentration systems described according to right 2, is characterized in that, described sorbent material refrigerating unit (5) adopts water recirculator.
4. double-fluidized-bed low-concentration methane concentration systems described according to right 2, is characterized in that, solid drier is filled in the air outlet of described condensation separator (13).
5. double-fluidized-bed low-concentration methane concentration systems described according to right 2, is characterized in that, the particle diameter of described absorbent particles is 300 ~ 600 μ m.
6. double-fluidized-bed low-concentration methane concentration systems described according to right 2, is characterized in that, described condensation separator (13) adopts water recirculator.
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| CN108318621B (en) * | 2018-01-05 | 2021-02-12 | 南通仁隆科研仪器有限公司 | Coal bed gas detection equipment with explosion-proof and gas collection function |
| CN108728195A (en) * | 2018-06-12 | 2018-11-02 | 帕提古丽·奥布力 | A kind of gas dehydration de-heavy hydrocarbon apparatus |
| CN112844033A (en) * | 2021-01-07 | 2021-05-28 | 太原理工大学 | CO capture2Bubbling conveying fluidized bed reaction device and process |
| CN116731760B (en) * | 2023-07-20 | 2024-01-02 | 北京化工大学 | Low concentration coalbed methane hydrate method circulation purification system |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5676738A (en) * | 1995-08-22 | 1997-10-14 | Cioffi; Lawrence | VOC control/solvent recovery system |
| CN1809684A (en) * | 2003-06-20 | 2006-07-26 | 福特汽车公司 | Use of VOC as fuel for an engine |
-
2012
- 2012-05-25 CN CN2012101660391A patent/CN102703150B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5676738A (en) * | 1995-08-22 | 1997-10-14 | Cioffi; Lawrence | VOC control/solvent recovery system |
| CN1809684A (en) * | 2003-06-20 | 2006-07-26 | 福特汽车公司 | Use of VOC as fuel for an engine |
Non-Patent Citations (2)
| Title |
|---|
| Assessment of the worldwide market potential for oxidizing coal mine ventilation air methane;US EPA;《United States Environmental Protection Agency》;20030731;14 * |
| US EPA.Assessment of the worldwide market potential for oxidizing coal mine ventilation air methane.《United States Environmental Protection Agency》.2003, |
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