CN103194285A - Industrial combustion method of dimethyl ether used for replacing natural gas through conversion - Google Patents
Industrial combustion method of dimethyl ether used for replacing natural gas through conversion Download PDFInfo
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- CN103194285A CN103194285A CN2012100019051A CN201210001905A CN103194285A CN 103194285 A CN103194285 A CN 103194285A CN 2012100019051 A CN2012100019051 A CN 2012100019051A CN 201210001905 A CN201210001905 A CN 201210001905A CN 103194285 A CN103194285 A CN 103194285A
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- dimethyl ether
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Abstract
The invention discloses an industrial combustion method of dimethyl ether used for replacing natural gas through conversion. According to the invention, dimethyl ether is heated to a temperature of 350-550 DEG C; in a cracking reactor, dimethyl ether is subjected to a cracking reaction; and under an effect of a methanation catalyst, a methanation reaction is carried out, wherein reaction conditions are that a reaction temperature is 230-450 DEG C, a reaction pressure is 0.05-0.2MPa, and a space velocity is 500-25000h<-1>, such that dimethyl ether is converted into natural gas with methane as a main component. Therefore, fuel heat value is improved, and cost-saving and energy-saving effects are achieved. An economical, energy-saving, and clean combustion method is provided for applying dimethyl ether as town gas or industrial fuel.
Description
[technical field]
The present invention relates to a kind ofly transform combustion gas to improve the method for fuel gases calorific value, specifically, the present invention relates to a kind of is the industrial combustion method of substitute natural gas with dimethyl ether conversion.
[background technology]
Liquefied petroleum gas (LPG) (LPG) as fuel is very expensive, particularly, if deliver to consumption location, for example in the family, the price specific output price of LPG is high, therefore, in recent years, dme has attracted people's attention as the substitute of LPG, it has been carried out applied research, and announce as domestic gas and national standard " city gas dme " CB25035-2010 and implement on July 1st, 2011 that the application of dme liquefied gas is had pushing effect from dme, dme is in actual applications, mean calorie is 3145KJ/KG, and the calorific value of oil liquefied gas is 46000KJ/KG, and the calorific value of dme only is that the heat that produces of the heat that produces of 68%, 1.47 ton dme of oil liquefied gas calorific value and 1 ton of oil liquefied gas is suitable, consider from the angle of economy, the user uses the cost height of dme, therefore, is restricted because cost is high with dme replacement liquid liquefied oil gas.
[summary of the invention]
The objective of the invention is to effectively overcome the deficiency of above-mentioned technology, a kind of dimethyl ether conversion substitute natural gas industrial combustion method is provided, and the fuel after the conversion is compared with gas of dimethyl ether fuel, has higher calorific value, can produce bigger heat, reach economical purpose of energy saving.
Technical scheme of the present invention is achieved in that its improvements are: it may further comprise the steps:
A), the dme liquefied gas through the decompression after carry out preheating, preheating temperature is greater than 350 ℃.
B), fail in well heater through the gas of dimethyl ether after the preheating, in well heater gas of dimethyl ether is quickly heated up to 350-550 ℃, the gas of dimethyl ether after heating transfers in the cracking reactor.
C), be provided with catalyst for cracking in the cracking reactor, under the effect of catalyst for cracking scission reaction takes place through the gas of dimethyl ether after the heater heats, the gas that the reaction back generates is called synthetic gas, its main component is carbon monoxide and hydrogen, after reaction is finished, synthetic gas is transferred in the methanator.
D), be provided with methanation catalyst in the methanator, methanation reaction takes place in the synthetic gas above-mentioned steps c) under the effect of methanation catalyst, the main component that the reaction back generates gas is methane, the reaction conditions of described methanation reaction is: temperature of reaction 230-450 ℃, reaction pressure 0.05-0.2Mpa, air speed 500-25000h
-1
E), after methanation reaction finishes, namely finished the process of dme conversion substitute natural gas, subsequently, gas transmission to the burner that produces in the step d) is burnt.
In the described step a), the heat that gas of dimethyl ether carries out preheating comes from the heat that the methanation reaction of used heat that boiler smoke produces or step d) produces.
In the described step b), carry in well heater through the gas of dimethyl ether after the preheating, in well heater gas of dimethyl ether is quickly heated up to 500 ℃, the gas of dimethyl ether after heating transfers in the reactor.
In the described step c), scission reaction takes place in gas of dimethyl ether under the effect of catalyst for cracking, and the intermediate product of generation is formaldehyde, and scission reaction further takes place formaldehyde, generates carbon monoxide and hydrogen.
In the described step d), employed methanation catalyst is nickel-base catalyst.
In the described step d), the temperature of reaction that methanation reaction takes place under the effect of methanation catalyst synthetic gas is 280-400 ℃.
In the described step d), the temperature of reaction that methanation reaction takes place under the effect of methanation catalyst synthetic gas is 350 ℃.
In the described step d), the reaction pressure that methanation reaction takes place under the effect of methanation catalyst synthetic gas is 0.1Mpa.
In the described step d), the air speed that methanation reaction takes place under the effect of methanation catalyst synthetic gas is 5000-10000h
-1
In the described step d), the air speed that methanation reaction takes place under the effect of methanation catalyst synthetic gas is 7500h
-1
Beneficial effect of the present invention is: the present invention is by being converted into low-calorie dme liquefied gas the substitute natural gas of high heating value under the effect of catalyzer, under equal conditions, the efficient heat generation amount of the substitute natural gas after the conversion is equal to the efficient heat generation amount of liquefied petroleum gas (LPG) (LPG), be equal to the calorific value that has improved dme, reach economical purpose of energy saving, the combustion method of an economy, energy-conservation, cleaning is provided as city gas or industrial fuel for dme.
[description of drawings]
Fig. 1 is first embodiment of the present invention figure;
Fig. 2 is that second enforcement of the present invention is three-dimensional.
Among the figure: tank body 1; Reducing valve 2; Tensimeter 3; Reactor 4; Reactor inlet mouth 41; Reactor air outlet 42; Boiler 5; Well heater 6; Methanation catalyst 7; Combustion chamber 8; Methanator 9; Cracking reactor 10; Catalyst for cracking 11; Gas-holder 12.
[embodiment]
The invention will be further described below in conjunction with drawings and Examples.
With reference to shown in Figure 1, first embodiment of the dimethyl ether conversion substitute natural gas industrial combustion method that discloses for the present invention, in the present embodiment, the dme liquefied gas storage is in tank body 1, after reducing valve 2 decompressions, transfer in reactor 4 exocoels, tensimeter 3 is used for showing the pressure of decompression back dme, reactor 4 is provided with exocoel and inner chamber, the reaction that takes place in the inner chamber is thermopositive reaction, and the waste heat by reaction tentatively heats dme, and in exocoel, be provided with catalyst for cracking, dme after preliminary heating transfers in the boiler 5, utilizes the fume waste heat in the boiler that dme is heated, and Heating temperature is more than 350 ℃, preferably 400 ℃, after boiler 5 heating, dme generation catalyzed reaction, the equation of its reaction is:
CH
3OCH
3——→2CH
2O+H
2 (1)，
2CH
2O——→2CO+2H
2 (2)；
In the reaction formula (1), dme is through the effect of catalyst for cracking, at first can be decomposed into formaldehyde and hydrogen, formaldehyde is under the effect of cracking and catalyzing, can further decompose, be decomposed into carbon monoxide and hydrogen, therefore, the main component of the synthetic gas after scission reaction is carbon monoxide and hydrogen, also has a small amount of unreacted dme; After this, synthetic gas enters in the well heater 6, in well heater inside synthetic gas is quickly heated up to 350-550 ℃, is preferably 500 ℃, synthetic gas after the heating is delivered to the reactor inlet mouth 41 in reactor 4, transfer to the reactor inner chamber, be provided with methanation catalyst 7 in the reactor inner chamber, methanation reaction takes place in synthetic gas under the effect of methanation catalyst 7, in the present embodiment, methanation catalyst is nickel-base catalyst, and its temperature of reaction is 230-450 ℃, is preferably 350 ℃; Reaction pressure is 0.05-0.2Mpa, is preferably 0.1Mpa; Air speed is 500-25000h
-1, be preferably 7500h
-1The reaction equation of this methanation reaction is:
2CO+3H
2——→CH
4+H
2+CO (3)；
In reaction formula (3), synthetic gas is that carbon monoxide and hydrogen are under catalyzer and certain conditions, methanation reaction has taken place, after methanation reaction is finished, the main component that generates gas is methane, also have a spot of hydrogen and carbon monoxide, and the unreacted dme of trace, the gas of gained is the rich hydrogen propellant combination of methane, 42 discharges from the reactor air outlet of the rich hydrogen propellant combination of methane, this reactor air outlet 42 is connected to combustion chamber 8, has namely finished dimethyl ether conversion substitute natural gas industrial combustion method.
In the above-described embodiments, we carry out record to the correlation parameter of two kinds of different heat-supplying modes of emulsification coal tar and dimethyl ether conversion substitute natural gas, table 1 between the record result:
| Capacity of boiler | Calorific value | Consumption | |
| Emulsification coal tar | 1315.6kg/h | 33854Kj/kg | 107.03kg/h |
| The dimethyl ether conversion substitute natural gas | 1315.6kg/h | 46000Kj/kg | 78.77kg/h |
Table 1
As can be seen from Table 1, when capacity of boiler is identical, the calorific value of dimethyl ether conversion substitute natural gas is 46000Kj/kg, suitable with the calorific value of liquefied petroleum gas (LPG) (LPG), the calorific value of emulsification coal tar has only 33854Kj/kg, have only the dimethyl ether conversion substitute natural gas calorific value 74%, and the consumption of emulsification coal tar is bigger than the consumption of dimethyl ether conversion substitute natural gas, therefore, use dimethyl ether conversion substitute natural gas industrial combustion method more economical, energy-conservation.
With reference to shown in Figure 2, be second embodiment of the present invention, in the present embodiment, the dme liquefied gas storage is in tank body 1, the interchanger 8 of after reducing valve 2 decompression, flowing through, utilize and reflect in the methanator 9 that liberated heat tentatively heats dme, after the preliminary heating, dme is sent in the boiler 5 and heats, and Heating temperature is more than 350 ℃, be preferably 400 ℃, after heating was finished, dme transferred in the cracking reactor 10, is provided with catalyst for cracking 11 in the cracking reactor 10, under the katalysis of catalyst for cracking 11, dme is decomposed into carbon monoxide and hydrogen, and after scission reaction was finished, carbon monoxide and hydrogen were sent in the methanator 9, be provided with methanation catalyst 7 in this methanator 9, in the present embodiment, methanation catalyst 7 is nickel-base catalyst, and carbon monoxide and hydrogen under the effect of nickel-base catalyst methanation reaction take place, its temperature of reaction is 230-450 ℃, is preferably 350 ℃; Reaction pressure is 0.05-0.2Mpa, is preferably 0.1Mpa; Air speed is 500-25000h
-1, be preferably 7500h
-1After methanation reaction is finished, the main component that generates gas is methane, also have a spot of hydrogen and carbon monoxide, and the unreacted dme of trace, the gas of gained is the rich hydrogen propellant combination of methane, and the rich hydrogen propellant combination of methane enters in the gas-holder 12 after cooling off by interchanger 8, namely finished dimethyl ether conversion substitute natural gas industrial combustion method, gas-holder is used for boiler is carried out heat supply.
In the above-described embodiments, we carry out record to the correlation parameter of two kinds of different heat-supplying modes of No. 250 heavy oil and dimethyl ether conversion substitute natural gas, table 2 between the record result:
| Capacity of boiler | Calorific value | Consumption | |
| No. 250 heavy oil | 916kg/h | 34146Kj/kg | 70.01kg/h |
| The dimethyl ether conversion substitute natural gas | 916kg/h | 46000Kj/kg | 52.0kg/h |
Table 2
As can be seen from Table 1, when capacity of boiler is identical, the calorific value of dimethyl ether conversion substitute natural gas is 46000Kj/kg, suitable with the calorific value of liquefied petroleum gas (LPG) (LPG), the calorific value of No. 250 heavy oil has only 34146Kj/kg, have only the dimethyl ether conversion substitute natural gas calorific value 74%, the fuel cost of No. 250 heavy oil that consume is 70.01Kg/h*5.5 unit/Kg=385.055 unit/h, the dme that consumes fuel cost be 52.0Kg/h*5.5 unit/Kg=286 unit/h, one day fuel cost can be saved 2377.32 yuan, and the fuel cost in 1 year can be saved 710,000 yuan, therefore, use dimethyl ether conversion substitute natural gas combustion method to can save energy fund, more economical.
Described above only is preferred embodiment of the present invention, and above-mentioned specific embodiment is not limitation of the present invention.In technological thought category of the present invention, various distortion and modification can appear, and the retouching that all those of ordinary skill in the art make according to above description, revise or be equal to replacement, all belong to the scope that the present invention protects.
Claims (10)
1. dimethyl ether conversion substitute natural gas industrial combustion method, it is characterized in that: it may further comprise the steps:
A), the dme liquefied gas through the decompression after carry out preheating, preheating temperature is greater than 350 ℃.
B), carry in well heater through the gas of dimethyl ether after the preheating, in well heater gas of dimethyl ether is quickly heated up to 350-550 ℃, the gas of dimethyl ether after heating transfers in the cracking reactor.
C), be provided with catalyst for cracking in the cracking reactor, under the effect of catalyst for cracking scission reaction takes place through the gas of dimethyl ether after the heater heats, the gas that the reaction back generates is called synthetic gas, its main component is carbon monoxide and hydrogen, after reaction is finished, synthetic gas is transferred in the methanator.
D), be provided with methanation catalyst in the methanator, methanation reaction takes place in the synthetic gas above-mentioned steps c) under the effect of methanation catalyst, the main component that the reaction back generates gas is methane, the reaction conditions of described methanation reaction is: temperature of reaction 230-450 ℃, reaction pressure 0.05-0.2Mpa, air speed 500-25000h
-1
E), after methanation reaction finishes, namely finished the process of dme conversion substitute natural gas, subsequently, burnt in gas transmission to the combustion chamber that produces in the step d).
2. a kind of dimethyl ether conversion substitute natural gas industrial combustion method according to claim 1, it is characterized in that: in the described step a), the heat that gas of dimethyl ether carries out preheating comes from the heat that the methanation reaction of used heat that boiler smoke produces or step d) produces.
3. a kind of dimethyl ether conversion substitute natural gas industrial combustion method according to claim 1, it is characterized in that: in the described step b), carry in well heater through the gas of dimethyl ether after the preheating, in well heater gas of dimethyl ether is quickly heated up to 500 ℃, the gas of dimethyl ether after heating transfers in the reactor.
4. a kind of dme according to claim 1 is changed substitute natural gas industrial combustion method, it is characterized in that: in the described step c), scission reaction takes place in gas of dimethyl ether under the effect of catalyst for cracking, the intermediate product that generates is formaldehyde, scission reaction further takes place in formaldehyde, generates carbon monoxide and hydrogen.
5. a kind of dimethyl ether conversion substitute natural gas industrial combustion method according to claim 1, it is characterized in that: in the described step d), employed methanation catalyst is nickel-base catalyst.
6. a kind of dme according to claim 1 is changed substitute natural gas industrial combustion method, and it is characterized in that: in the described step d), the temperature of reaction that methanation reaction takes place under the effect of methanation catalyst synthetic gas is 280-400 ℃.
7. a kind of dme according to claim 1 is changed substitute natural gas industrial combustion method, and it is characterized in that: in the described step d), the temperature of reaction that methanation reaction takes place under the effect of methanation catalyst synthetic gas is 350 ℃.
8. a kind of dme according to claim 1 is changed substitute natural gas industrial combustion method, and it is characterized in that: in the described step d), the reaction pressure that methanation reaction takes place under the effect of methanation catalyst synthetic gas is 0.1Mpa.
9. a kind of dme according to claim 1 is changed substitute natural gas industrial combustion method, and it is characterized in that: in the described step d), the air speed that methanation reaction takes place under the effect of methanation catalyst synthetic gas is 5000-10000h
-1
10. a kind of dme according to claim 1 is changed substitute natural gas industrial combustion method, and it is characterized in that: in the described step d), the air speed that methanation reaction takes place under the effect of methanation catalyst synthetic gas is 7500h
-1
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Citations (6)
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| CN1642891A (en) * | 2002-02-20 | 2005-07-20 | 加利福尼亚大学董事会 | Process and catalyst for production of formaldehyde from dimethyl ether |
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| CN1981122A (en) * | 2004-06-30 | 2007-06-13 | 杰富意控股株式会社 | Waste heat recovery apparatus, waste heat recovery system, and method of recovering waste heat |
| CN101042261A (en) * | 2006-03-22 | 2007-09-26 | 中国科学院工程热物理研究所 | Method and apparatus for converting solar energy into fuel chemical energy |
| CN101745401A (en) * | 2009-12-07 | 2010-06-23 | 中国科学院山西煤炭化学研究所 | Load type sulfur-tolerant methanation catalyst and preparation method and application thereof |
| CN102060667A (en) * | 2010-11-23 | 2011-05-18 | 吉林众鑫化工集团有限公司 | Method for gas-phase solvent-free catalysis-free synthesis of 3-methyl-3-butenyl-1-alcohol |
-
2012
- 2012-01-05 CN CN2012100019051A patent/CN103194285A/en active Pending
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1642891A (en) * | 2002-02-20 | 2005-07-20 | 加利福尼亚大学董事会 | Process and catalyst for production of formaldehyde from dimethyl ether |
| CN1931428A (en) * | 2002-02-20 | 2007-03-21 | 加利福尼亚大学董事会 | Process and catalyst for production of formaldehyde from dimethyl ether |
| CN1981122A (en) * | 2004-06-30 | 2007-06-13 | 杰富意控股株式会社 | Waste heat recovery apparatus, waste heat recovery system, and method of recovering waste heat |
| CN1830757A (en) * | 2005-03-07 | 2006-09-13 | 中国科学院工程热物理研究所 | Method and device for transforming solar energy into fuel chemical energy |
| CN101042261A (en) * | 2006-03-22 | 2007-09-26 | 中国科学院工程热物理研究所 | Method and apparatus for converting solar energy into fuel chemical energy |
| CN101745401A (en) * | 2009-12-07 | 2010-06-23 | 中国科学院山西煤炭化学研究所 | Load type sulfur-tolerant methanation catalyst and preparation method and application thereof |
| CN102060667A (en) * | 2010-11-23 | 2011-05-18 | 吉林众鑫化工集团有限公司 | Method for gas-phase solvent-free catalysis-free synthesis of 3-methyl-3-butenyl-1-alcohol |
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Application publication date: 20130710 |