CN106673939A - System and method for preparing ethylene by coupling - Google Patents
System and method for preparing ethylene by coupling Download PDFInfo
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- CN106673939A CN106673939A CN201611147796.9A CN201611147796A CN106673939A CN 106673939 A CN106673939 A CN 106673939A CN 201611147796 A CN201611147796 A CN 201611147796A CN 106673939 A CN106673939 A CN 106673939A
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- hydrogen
- acetylene
- calcium carbide
- coal
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- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 title claims abstract description 43
- 238000000034 method Methods 0.000 title claims abstract description 25
- 230000008878 coupling Effects 0.000 title claims abstract description 9
- 238000010168 coupling process Methods 0.000 title claims abstract description 9
- 238000005859 coupling reaction Methods 0.000 title claims abstract description 9
- 239000005977 Ethylene Substances 0.000 title abstract 5
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims abstract description 93
- 229910052739 hydrogen Inorganic materials 0.000 claims abstract description 93
- 239000001257 hydrogen Substances 0.000 claims abstract description 93
- HSFWRNGVRCDJHI-UHFFFAOYSA-N alpha-acetylene Natural products C#C HSFWRNGVRCDJHI-UHFFFAOYSA-N 0.000 claims abstract description 71
- 125000002534 ethynyl group Chemical group [H]C#C* 0.000 claims abstract description 68
- 238000002309 gasification Methods 0.000 claims abstract description 66
- 239000003245 coal Substances 0.000 claims abstract description 53
- 239000003034 coal gas Substances 0.000 claims abstract description 37
- 238000005984 hydrogenation reaction Methods 0.000 claims abstract description 37
- 239000003054 catalyst Substances 0.000 claims abstract description 24
- 238000004519 manufacturing process Methods 0.000 claims abstract description 23
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Chemical compound O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 18
- 238000000926 separation method Methods 0.000 claims abstract description 11
- 238000002360 preparation method Methods 0.000 claims abstract description 9
- 239000000843 powder Substances 0.000 claims abstract description 4
- 239000005997 Calcium carbide Substances 0.000 claims description 87
- CLZWAWBPWVRRGI-UHFFFAOYSA-N tert-butyl 2-[2-[2-[2-[bis[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]amino]-5-bromophenoxy]ethoxy]-4-methyl-n-[2-[(2-methylpropan-2-yl)oxy]-2-oxoethyl]anilino]acetate Chemical compound CC1=CC=C(N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)C(OCCOC=2C(=CC=C(Br)C=2)N(CC(=O)OC(C)(C)C)CC(=O)OC(C)(C)C)=C1 CLZWAWBPWVRRGI-UHFFFAOYSA-N 0.000 claims description 87
- 239000007788 liquid Substances 0.000 claims description 37
- 239000002245 particle Substances 0.000 claims description 32
- 239000007789 gas Substances 0.000 claims description 29
- 239000000571 coke Substances 0.000 claims description 20
- 239000004575 stone Substances 0.000 claims description 12
- 238000006243 chemical reaction Methods 0.000 claims description 11
- 239000002817 coal dust Substances 0.000 claims description 8
- 238000003723 Smelting Methods 0.000 claims description 6
- 230000005611 electricity Effects 0.000 claims description 2
- 230000008569 process Effects 0.000 abstract description 5
- 238000000605 extraction Methods 0.000 abstract 3
- 238000005516 engineering process Methods 0.000 description 9
- 239000002956 ash Substances 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 230000008859 change Effects 0.000 description 4
- 150000001336 alkenes Chemical class 0.000 description 3
- 239000002994 raw material Substances 0.000 description 3
- 230000026676 system process Effects 0.000 description 3
- 230000003197 catalytic effect Effects 0.000 description 2
- 239000003795 chemical substances by application Substances 0.000 description 2
- 238000001514 detection method Methods 0.000 description 2
- 239000003063 flame retardant Substances 0.000 description 2
- 238000009413 insulation Methods 0.000 description 2
- 238000012946 outsourcing Methods 0.000 description 2
- 235000002918 Fraxinus excelsior Nutrition 0.000 description 1
- 235000019738 Limestone Nutrition 0.000 description 1
- 241001417490 Sillaginidae Species 0.000 description 1
- 241001062472 Stokellia anisodon Species 0.000 description 1
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 1
- GLLAXJZCLLRSKC-UHFFFAOYSA-N acetylene ethene Chemical compound C=C.C=C.C#C GLLAXJZCLLRSKC-UHFFFAOYSA-N 0.000 description 1
- AMXBISSOONGENB-UHFFFAOYSA-N acetylene;ethene Chemical group C=C.C#C AMXBISSOONGENB-UHFFFAOYSA-N 0.000 description 1
- 238000007259 addition reaction Methods 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 239000003077 lignite Substances 0.000 description 1
- 239000006028 limestone Substances 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000002893 slag Substances 0.000 description 1
- 229910052717 sulfur Inorganic materials 0.000 description 1
- 239000011593 sulfur Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/08—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds
- C07C5/09—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Catalysts (AREA)
Abstract
The invention discloses a system and method for preparing ethylene by coupling. The system comprises a gasification furnace, a coal gas separation hydrogen extraction device and a hydrogenation reactor, wherein the gasification furnace comprises a coal powder inlet, a water vapor inlet and a hydrogen-rich coal gas outlet; the coal gas separation hydrogen extraction device comprises a hydrogen-rich coal gas inlet and a hydrogen outlet; the hydrogen-rich coal gas inlet is connected with the hydrogen-rich coal gas outlet of the gasification furnace; the hydrogenation reactor comprises a hydrogen inlet, a hydrogenation catalyst inlet, an acetylene inlet and an ethylene outlet; and the hydrogen inlet is connected with the hydrogen outlet of the coal gas separation hydrogen extraction device. By coupling coal gasification and the ethylene preparation technique, the hydrogen generated by coal gasification in the coal gas and acetylene are subjected to hydrogenation reaction to prepare the ethylene, thereby lowering the production cost. The process route of the overall system is very simple.
Description
Technical field
Present invention relates generally to the preparation technology of ethene, and in particular to a kind of coupling prepares the system and method for ethene.
Background technology
At present in calcium carbide production technology, calcium carbide flows out furnace of calcium carbide extremely in furnace of calcium carbide by more than 2000 DEG C of liquid carbide liquid
Calcium carbide crucible, is then cooled to room temperature in its natural state, it is impossible to utilize acetylene stones sensible heat, causes the significant wastage of the energy.
In addition, it is necessary to there is addition reaction with acetylene for substantial amounts of hydrogen outward during by carbide acetylene production ethene
Generation ethene, hydrogen source turns into the key restriction factors of acetylene downstream production, finds cheap hydrogen source and its production technology and calcium carbide smelting
Refining, carbide acetylene ethene are coupled as current study hotspot problem.
The content of the invention
It is an object of the invention to provide a kind of new technology by the technology coupling such as coal gasification and ethene preparation.
Present invention firstly provides the system that a kind of coupling prepares ethene, the system includes that gasification furnace, coal gas are separated and carries
Hydrogen production device and hydrogenation reactor；
The gasification furnace includes the outlet of coal powder entrance, steam entry and hydrogen-rich gas；
The coal gas separates and carries hydrogen production device and include hydrogen-rich gas entrance and hydrogen outlet, the hydrogen-rich gas entrance with it is described
The hydrogen-rich gas outlet of gasification furnace is connected；
The hydrogenation reactor includes the outlet of hydrogen inlet, hydrogenation catalyst entrance, acetylene entrance and ethene, the hydrogen
Entrance separated with the coal gas carry hydrogen production device hydrogen outlet be connected.
In one embodiment of the invention, the system also includes furnace of calcium carbide, acetylene stones sensible heat recover and acetylene hair
Raw device；
The furnace of calcium carbide includes the outlet of semi-coke entrance, CaO entrances and liquid calcium carbide；
The acetylene stones sensible heat recover includes the outlet of liquid calcium carbide entrance, water inlet, steam outlet and calcium carbide, the liquid
State calcium carbide entrance is connected with the liquid calcium carbide outlet of the furnace of calcium carbide, and the steam outlet enters with the vapor of the gasification furnace
Mouth is connected；
The acetylene generator includes the outlet of calcium carbide entrance, water inlet and acetylene, and the calcium carbide entrance is aobvious with the calcium carbide
The calcium carbide outlet of heat regenerator is connected, and the acetylene outlet is connected with the acetylene entrance of the hydrogenation reactor.
In one embodiment of the invention, the gasification furnace also includes gasifying catalyst entrance.
Additionally, present invention also offers a kind of method that utilization said system prepares ethene, comprising the following steps：
Coal gasification：Coal dust and vapor are sent into the gasification furnace via the coal entrance and the steam entry respectively
In, the coal gasification, obtains hydrogen-rich gas at a temperature of T1；
Coal gas is separated：The hydrogen-rich gas is sent into during the coal gas separation carries hydrogen production device and is separated, obtain hydrogen；
It is prepared by ethene：At a temperature of T2, by acetylene, hydrogenation catalyst and the hydrogen respectively via the acetylene entrance,
Hydrogenation catalyst entrance and the hydrogen inlet are sent into the hydrogenation reactor, and the acetylene and hydrogen reaction generate second
Alkene.
In one embodiment of the invention, methods described is further comprising the steps of：
Calcium carbide is smelted：At a temperature of T3, carried out smelting preparation liquid calcium carbide with semi-coke and CaO；
Exposure degree：With the liquid calcium carbide and water indirect heat exchange, solid-state calcium carbide and vapor are obtained, by the vapor
In sending into the gasification furnace；
It is prepared by acetylene：Acetylene is prepared with solid-state calcium carbide, by the acetylene feeding hydrogenation reactor.
In one embodiment of the invention, in the coal gasification step, go back and be passed through gas toward the gasification furnace
Change catalyst, the coal dust is 25 with the mass ratio of the gasifying catalyst:1-15:1.
In one embodiment of the invention, the gasifying catalyst for powdery CaO, the powdery CaO particle diameter≤
0.2mm, preferable particle size≤0.1mm.
In one embodiment of the invention, the particle diameter≤0.5mm of the coal, preferable particle size≤0.1mm.The coal
Moisture≤8wt%.Pit ash content≤the 15wt%.Volatile matter content >=the 30wt% of the coal.
In one embodiment of the invention, the T1 is 1200-2000 DEG C.The T2 is 150-250 DEG C.
In one embodiment of the invention, the particle diameter≤30mm of the semi-coke, preferable particle size≤25mm.The semi-coke
Moisture≤2wt%.Particle diameter≤the 30mm of the CaO, preferable particle size≤25mm.The T3 is 1900-2200 DEG C, and its is excellent
Elect 2050 DEG C as.
The present invention couples coal gasification with ethene preparation technology, is entered with acetylene using the hydrogen in the coal gas that coal gasification is produced
Row hydrogenation reaction, prepares ethene, reduces production cost.Whole system process route is very simple.
Additionally, the application has also reclaimed the sensible heat of carbide liquid, dramatically reduce loss, saved the energy.
Brief description of the drawings
Fig. 1 prepares the structural representation of the system of ethene for a kind of coupling in the embodiment of the present invention；
Fig. 2 prepares the process chart of ethene for a kind of utilization said system in the embodiment of the present invention.
Specific embodiment
Below in conjunction with drawings and Examples, specific embodiment of the invention is described in more details, so as to energy
Enough more fully understand the solution of the present invention and the advantage of its various aspects.However, specific embodiments described below and reality
It is only descriptive purpose to apply example, rather than limitation of the present invention.
With reference to Fig. 1, the system for preparing ethene of present invention offer includes that gasification furnace 1, coal gas is separated and carries hydrogen production device 2, hydrogenation
Reactor 3, furnace of calcium carbide 4, acetylene stones sensible heat recover 5 and acetylene generator 6.
Gasification furnace 1 includes the outlet of coal powder entrance 101, steam entry, gasifying catalyst entrance and hydrogen-rich gas.Gasification furnace
1 is preferably airflow bed gasification furnace.
Coal gas separation carries hydrogen production device 2 includes hydrogen-rich gas entrance, hydrogen outlet and gas exit, hydrogen-rich gas entrance and gas
The hydrogen-rich gas outlet for changing stove 1 is connected.
Hydrogenation reactor 3 includes hydrogen inlet, hydrogenation catalyst entrance 301, acetylene entrance and ethene outlet 302, hydrogen
Entrance separated with coal gas carry hydrogen production device 2 hydrogen outlet be connected.
Furnace of calcium carbide 4 includes semi-coke entrance 401, the outlet of CaO entrances 402, calcium carbide furnace gas and the outlet of liquid calcium carbide.
Acetylene stones sensible heat recover 5 includes the outlet of liquid calcium carbide entrance, water inlet 501, steam outlet and calcium carbide, liquid electricity
Stone entrance is connected with the liquid calcium carbide outlet of furnace of calcium carbide 4, and steam outlet is connected with the steam entry of gasification furnace 1.Calcium carbide shows
The heat exchange mode of heat regenerator 5 is indirect heat exchange.
Acetylene generator 6 include calcium carbide entrance, water inlet 601, carbide slag outlet 602 and acetylene outlet, calcium carbide entrance with
The calcium carbide outlet of the acetylene stones sensible heat recover 5 is connected, and acetylene outlet is connected with the acetylene entrance of hydrogenation reactor 3.
Wherein, furnace of calcium carbide 4, acetylene stones sensible heat recover 5 and acetylene generator 6 are not the device that system must have, and are used for
The acetylene for preparing ethene can be prepared by calcium carbide, also can directly outsourcing；Can be by between water and liquid calcium carbide as the vapor of gasifying agent
Connect heat exchange to be obtained, can also be prepared by other modes.
Fig. 2 is the mode that a kind of utilization said system of the invention prepares ethene, and the method comprises the following steps：
Calcium carbide is smelted：At a temperature of T3, carried out smelting preparation liquid calcium carbide with semi-coke and CaO；
Exposure degree：With the liquid calcium carbide and water indirect heat exchange, solid-state calcium carbide and vapor are obtained, by the vapor
In sending into the gasification furnace；
It is prepared by acetylene：Acetylene is prepared with solid-state calcium carbide, by the acetylene feeding hydrogenation reactor.
Coal gasification：Coal dust and vapor are sent into the gasification furnace via the coal entrance and the steam entry respectively
In, the coal gasification, obtains hydrogen-rich gas at a temperature of T1；
Coal gas is separated：The hydrogen-rich gas is sent into during the coal gas separation carries hydrogen production device and is separated, obtain hydrogen；
It is prepared by ethene：At a temperature of T2, by acetylene, hydrogenation catalyst and the hydrogen respectively via the acetylene entrance,
Hydrogenation catalyst entrance and the hydrogen inlet are sent into the hydrogenation reactor, and the acetylene and hydrogen reaction generate second
Alkene.
Mass ratio≤0.96 of the catalyst when present invention uses vapor as coal gasification, vapor and coal, preferably matter
Amount ratio≤0.80.Vapor is that water is prepared with high temperature carbide liquid indirect heat exchange, has reclaimed the sensible heat of carbide liquid, very big journey
Spend ground reduce loss, save the energy.In above-mentioned technique be used for prepare ethene acetylene can directly outsourcing, as coal gas agent
Vapor can also be prepared by other modes.
The present invention couples coal gasification with ethene preparation technology, is entered with acetylene using the hydrogen in the coal gas that coal gasification is produced
Row hydrogenation reaction, prepares ethene, reduces production cost.Whole system process route is very simple.
Additionally, all of equipment of the invention insulation, it is closed and fire-retardant under conditions of work, material sets at each
Conveying between standby also insulation and it is fire-retardant under conditions of carry out, it is abundant to make use of the high temperature that gasification and calcium carbide are smelted to show
Heat, significantly reduces loss, has saved the energy.
In gasification of coal, also, to improve the effect of coal gasification, hydrogen in coal gas can be increased toward catalyst is passed through in gasification furnace 1
The content of gas.CaO has preferable catalytic action in coal gasification course, and has good sulfur fixation performance concurrently, is improving coal gas
While the reaction rate of change, the clean conversion of coal can be realized.
Found by substantial amounts of experiment, when the addition of powdery CaO is the 1/25-1/15 of the quality of coal, its catalytic effect
It is best.
The particle diameter of coal is smaller, moisture is fewer, and the effect of gasification is better.In the application, the particle diameter of coal preferably≤
0.5mm, preferably, particle diameter is best≤0.1mm.Similarly, the moisture of coal less, content of ashes less, volatile matter content
More, the effect of its gasification is also better.In the application, the moisture of coal preferably≤8wt%, pit ash content preferably≤
15wt%, the volatile matter content of coal is preferably >=30%.
The application smelts calcium carbide using semi-coke and lime stone, and the effect of the smaller smelting of its particle diameter is better.The particle diameter of semi-coke is excellent
Choosing≤30mm, preferable particle size preferably≤25mm.The particle diameter of CaO preferably≤30mm, preferable particle size preferably≤25mm.Semi-coke and CaO
Mass ratio be 0.55-0.70, preferably 0.63.
Temperature T1 during coal gasification is preferably 1200 DEG C -2000 DEG C.Prepare temperature T2 preferably 150-250 during ethene
℃.The temperature T3 that smelting prepares calcium carbide is preferably 1900 DEG C -2200 DEG C, and preferably, T3 is preferably 2050 DEG C.Temperature is too low, coal
The effect for gasify, preparing ethene and smelt calcium carbide is bad；Temperature is too high, wastes the energy.If T2 is too high, it is impossible to be obtained high-grade
Ethene.
Additionally, the pressure that the operating pressure of gasification furnace 1 can be allowed by any gasification furnace.
Below with reference to specific embodiment, the present invention will be described.Institute's taking technique condition value is in following embodiments
Exemplary, its desirable number range is as shown in foregoing summary.Detection method used by following embodiments is one's own profession
The conventional detection method of industry.
Embodiment 1
The present embodiment prepares acetylene using the process route shown in the system and Fig. 2 shown in Fig. 1, specific as follows：
Prepare raw material：Dross coal is crushed, the coal dust of particle diameter≤0.5mm is chosen, then is dried to moisture and is
8wt%；This pit ash content is 7wt%, volatile matter content is 30wt%.CaO is crushed, chooses particle diameter≤30mm's respectively
The powdery CaO of CaO and particle diameter≤0.2mm.Semi-coke is crushed, the semi-coke of particle diameter≤30mm is chosen.
Calcium carbide is smelted：Take 550kg semi-cokes feeding furnace of calcium carbide 4 in, then inside add 1000kg CaO, at 1900 DEG C
Smelt and prepare liquid calcium carbide.
Exposure degree：Exchanged heat with liquid calcium carbide and water, obtain solid-state calcium carbide and vapor.
It is prepared by acetylene：Take 950kg solid-states calcium carbide and prepare acetylene with 1400kg water reactions.
Coal gasification：In taking 1000kg coal dusts feeding gasification furnace 1, then toward adding 40kg powderies CaO and 960kg in gasification furnace 1
Vapor, coal gasification is carried out at 2000 DEG C, obtains hydrogen-rich gas.
Coal gas is separated：Separated during hydrogen-rich gas feeding coal gas separation is carried into hydrogen production device 2, obtained hydrogen.
It is prepared by ethene：By 305m2Acetylene, 4.5kg hydrogenation catalysts and 310m2In hydrogen feeding hydrogenation reactor 3,250
At DEG C, acetylene and hydrogen reaction generate ethene.
Product and the temperature of liquid calcium carbide outlet are see table 1.
Embodiment 2
The present embodiment prepares acetylene using the process route shown in the system and Fig. 2 shown in Fig. 1, specific as follows：
Prepare raw material：By brown coal crushing, the coal dust of particle diameter≤0.1mm is chosen, then be dried to moisture and be
5wt%；This pit ash content is 15wt%, volatile matter content is 35wt%.CaO is crushed, particle diameter≤25mm is chosen respectively
CaO and particle diameter≤0.1mm powdery CaO.Semi-coke is crushed, the semi-coke of particle diameter≤25mm is chosen.
Calcium carbide is smelted：Take 700kg semi-cokes feeding furnace of calcium carbide 4 in, then inside add 1000kg CaO, at 2050 DEG C
Smelt and prepare liquid calcium carbide.
Exposure degree：Exchanged heat with liquid calcium carbide and water, obtain solid-state calcium carbide and vapor.
It is prepared by acetylene：Take 1014kg solid-states calcium carbide and prepare acetylene with 1500kg water reactions.
Coal gasification：In taking 1000kg coal dusts feeding gasification furnace 1, then toward adding 67kg powderies CaO and 800kg in gasification furnace 1
Vapor, coal gasification is carried out at 1200 DEG C, obtains hydrogen-rich gas.
Coal gas is separated：Separated during hydrogen-rich gas feeding coal gas separation is carried into hydrogen production device 2, obtained hydrogen.
It is prepared by ethene：By 311m2Acetylene, 4.7kg hydrogenation catalysts and 315m2In hydrogen feeding hydrogenation reactor 3,150
At DEG C, acetylene and hydrogen reaction generate ethene.
Product and the temperature of liquid calcium carbide outlet are see table 1.
Embodiment 3
The present embodiment prepares acetylene using the process route shown in the system and Fig. 2 shown in Fig. 1, specific as follows：
Prepare raw material：Jet coal is crushed, the coal dust of particle diameter≤0.3mm is chosen, then is dried to moisture and is
6wt%；This pit ash content is 10wt%, volatile matter content is 32wt%.CaO is crushed, particle diameter≤20mm is chosen respectively
CaO and particle diameter≤0.08mm powdery CaO.Semi-coke is crushed, the semi-coke of particle diameter≤20mm is chosen.
Calcium carbide is smelted：Take 630kg semi-cokes feeding furnace of calcium carbide 4 in, then inside add 1000kg CaO, at 2200 DEG C
Smelt and prepare liquid calcium carbide.
Exposure degree：Exchanged heat with liquid calcium carbide and water, obtain solid-state calcium carbide and vapor.
It is prepared by acetylene：Take 997kg solid-states calcium carbide and prepare acetylene with 1480kg water reactions.
Coal gasification：In taking 1000kg coal dusts feeding gasification furnace 1, then toward adding 50kg powderies CaO and 600kg in gasification furnace 1
Vapor, coal gasification is carried out at 1600 DEG C, obtains hydrogen-rich gas.
Coal gas is separated：Separated during hydrogen-rich gas feeding coal gas separation is carried into hydrogen production device 2, obtained hydrogen.
It is prepared by ethene：By 315m2Acetylene, 4.5kg hydrogenation catalysts and 320m2In hydrogen feeding hydrogenation reactor 3,200
At DEG C, acetylene and hydrogen reaction generate ethene.
Product and the temperature of liquid calcium carbide outlet are see table 1.
Each embodiment product of table 1 and the temperature of liquid calcium carbide outlet
| Embodiment 1 | Embodiment 2 | Embodiment 3 | |
| Coal gas/m3 | 2297 | 2352 | 2346 |
| Hydrogen/m3 | 1378 | 1413 | 1408 |
| Calcium carbide/kg | 950 | 1014 | 997 |
| Vapor //kg | 960 | 800 | 600 |
| Ethene/m3 | 294 | 299 | 302 |
| The outlet of liquid calcium carbide/DEG C | 1763 | 1975 | 2086 |
As it can be seen from table 1 the comparision contents of hydrogen are more in the obtained coal gas of the present invention, can be completely used for preparing second
Alkene.Further, since make use of the sensible heat of liquid calcium carbide, loss is greatly reduced, saved the energy.
To sum up, the present invention coal gasification couple with ethene preparation technology, using coal gasification generation coal gas in hydrogen and
Acetylene carries out hydrogenation reaction, prepares ethene, reduces production cost.Whole system process route is very simple.
Additionally, the application has also reclaimed the sensible heat of carbide liquid, dramatically reduce loss, saved the energy.
Finally it should be noted that：Obviously, above-described embodiment is only intended to clearly illustrate example of the present invention, and simultaneously
The non-restriction to implementation method.For those of ordinary skill in the field, can also do on the basis of the above description
Go out the change or variation of other multi-forms.There is no need and unable to be exhaustive to all of implementation method.And thus drawn
Obvious change that Shen goes out or among changing still in protection scope of the present invention.
Claims (10)
1. the system that a kind of coupling prepares ethene, it is characterised in that the system include gasification furnace, coal gas separate carry hydrogen production device and
Hydrogenation reactor；
The gasification furnace includes the outlet of coal powder entrance, steam entry and hydrogen-rich gas；
The coal gas separation carries hydrogen production device includes hydrogen-rich gas entrance and hydrogen outlet, the hydrogen-rich gas entrance and the gasification
The hydrogen-rich gas outlet of stove is connected；
The hydrogenation reactor includes the outlet of hydrogen inlet, hydrogenation catalyst entrance, acetylene entrance and ethene, the hydrogen inlet
Separated with the coal gas carry hydrogen production device hydrogen outlet be connected.
2. system according to claim 1, it is characterised in that the system also includes furnace of calcium carbide, acetylene stones sensible heat recover
And acetylene generator；
The furnace of calcium carbide includes the outlet of semi-coke entrance, CaO entrances and liquid calcium carbide；
The acetylene stones sensible heat recover includes the outlet of liquid calcium carbide entrance, water inlet, steam outlet and calcium carbide, the liquid electricity
The liquid calcium carbide outlet of stone entrance and the furnace of calcium carbide is connected, the steam entry phase of the steam outlet and the gasification furnace
Even；
The acetylene generator includes the outlet of calcium carbide entrance, water inlet and acetylene, and the calcium carbide entrance is returned with the acetylene stones sensible heat
The calcium carbide outlet for receiving device is connected, and the acetylene outlet is connected with the acetylene entrance of the hydrogenation reactor.
3. system according to claim 1, it is characterised in that the gasification furnace also includes gasifying catalyst entrance.
4. the method that a kind of described systems of one of utilization claim 1-3 prepare ethene, comprises the following steps：
Coal gasification：During coal dust and vapor sent into the gasification furnace via the coal entrance and the steam entry respectively,
The coal gasification, obtains hydrogen-rich gas at a temperature of T1；
Coal gas is separated：The hydrogen-rich gas is sent into during the coal gas separation carries hydrogen production device and is separated, obtain hydrogen；
It is prepared by ethene：At a temperature of T2, by acetylene, hydrogenation catalyst and the hydrogen respectively via the acetylene entrance, hydrogenation
Catalyst inlet and the hydrogen inlet are sent into the hydrogenation reactor, and the acetylene and hydrogen reaction generate ethene.
5. method according to claim 4, it is characterised in that methods described is further comprising the steps of：
Calcium carbide is smelted：At a temperature of T3, carried out smelting preparation liquid calcium carbide with semi-coke and CaO；
Exposure degree：Exchanged heat with the liquid calcium carbide and water, obtain solid-state calcium carbide and vapor, vapor feeding is described
In gasification furnace；
It is prepared by acetylene：Acetylene is prepared with solid-state calcium carbide, by the acetylene feeding hydrogenation reactor.
6. method according to claim 4, it is characterised in that in the coal gasification step, also toward in the gasification furnace
Gasifying catalyst is passed through, the coal dust is 25 with the mass ratio of the gasifying catalyst:1-15:1.
7. method according to claim 6, it is characterised in that the gasifying catalyst is powdery CaO, the powdery CaO
Particle diameter≤0.2mm, preferable particle size≤0.1mm.
8. method according to claim 4, it is characterised in that the particle diameter≤0.5mm of the coal, preferable particle size≤0.1mm.
9. method according to claim 4, it is characterised in that the T1 is 1200-2000 DEG C；The T2 is 150-250
℃。
10. method according to claim 5, it is characterised in that the T3 is 1900-2200 DEG C, and it is preferably 2050 DEG C.
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| CN201611147796.9A CN106673939A (en) | 2016-12-13 | 2016-12-13 | System and method for preparing ethylene by coupling |
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| Application Number | Priority Date | Filing Date | Title |
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| CN201611147796.9A CN106673939A (en) | 2016-12-13 | 2016-12-13 | System and method for preparing ethylene by coupling |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5699428A (en) * | 1980-01-12 | 1981-08-10 | Natl Res Inst For Metals | Preparation of acetylene and ethylene form solid carbon using hydrogen plasma |
| CN102676232A (en) * | 2012-05-17 | 2012-09-19 | 山东万丰煤化工设备制造有限公司 | Method for preparing pulverized coal into hydrogen gas |
| CN103992200A (en) * | 2014-05-20 | 2014-08-20 | 榆林科大高新能源研究院有限公司 | Process method for obtaining acetylene gas from semi-coke via calcium carbide and further producing ethylene by hydrogenation |
| CN104803819A (en) * | 2015-05-15 | 2015-07-29 | 北京神雾环境能源科技集团股份有限公司 | Method and system for producing ethylene by utilizing pulverized coal |
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2016
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5699428A (en) * | 1980-01-12 | 1981-08-10 | Natl Res Inst For Metals | Preparation of acetylene and ethylene form solid carbon using hydrogen plasma |
| CN102676232A (en) * | 2012-05-17 | 2012-09-19 | 山东万丰煤化工设备制造有限公司 | Method for preparing pulverized coal into hydrogen gas |
| CN103992200A (en) * | 2014-05-20 | 2014-08-20 | 榆林科大高新能源研究院有限公司 | Process method for obtaining acetylene gas from semi-coke via calcium carbide and further producing ethylene by hydrogenation |
| CN104803819A (en) * | 2015-05-15 | 2015-07-29 | 北京神雾环境能源科技集团股份有限公司 | Method and system for producing ethylene by utilizing pulverized coal |
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