CN106433736A - Direct coal hydrogenation reaction device and method - Google Patents
Direct coal hydrogenation reaction device and method Download PDFInfo
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- CN106433736A CN106433736A CN201610858504.6A CN201610858504A CN106433736A CN 106433736 A CN106433736 A CN 106433736A CN 201610858504 A CN201610858504 A CN 201610858504A CN 106433736 A CN106433736 A CN 106433736A
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- coal
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- hydrogenation reaction
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/002—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal in combination with oil conversion- or refining processes
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/06—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by destructive hydrogenation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/02—Gasoline
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention relates to a direct coal hydrogenation reaction device and method. The device is characterized by comprising a vaporizing chamber, a fluidization pyrolysis chamber and a separation chamber which are communicated in sequence; the vaporizing chamber is a hot-wall reactor, and the top of the vaporizing chamber is provided with a vaporizing nozzle for performing charging inside the vaporizing chamber, an inlet of the lower portion of the fluidization pyrolysis chamber is connected with an outlet in the lower portion of the vaporizing chamber through a pipeline; a coal dust nozzle for adding coal dust into the fluidization pyrolysis chamber is arranged on the side wall of the fluidization pyrolysis chamber; an outlet of the upper portion of the fluidization pyrolysis chamber is connected with the separation chamber through a pipeline; a gas phase outlet is formed in the top of the separation chamber, and a solid phase outlet is formed in the bottom of the separation chamber. On the relatively-mild reaction condition, coal dust can be directly catalyzed and hydrogenated, separation and upgrading are performed to obtain liquid chemical product oil and other chemicals such as gasoline, diesel and aviation kerosene; no extra hydrogen source needs to be provided, the oil yield is high, and the device is environmentally friendly.
Description
Technical field
The present invention relates to a kind of chemical industry equipment and reaction method, refer specifically to a kind of coal direct hydrogenation reaction unit and reaction side
Method.
Background technology
Coal direct hydrogenation technical process mainly include the broken of coal and drying, coal slurry preparation, hydrogenation liquefaction, separation of solid and liquid,
The parts such as gas purification, fluid product fractionation and refined and hydrogen manufacturing.Main flow is：At high temperature under high pressure, high concentration coal slurry
In coal be pyrolyzed, be hydrogenated with catalyst action and decomposed, eventually become stable fluid molecule.Liquefaction process
In, coal slurry that coal, catalyst and recycle oil are made, feeding reactor is mixed with prepared hydrogen.In liquefying reactor, coal
There is pyrolytic reaction first, generate free radical " fragment ", unstable free radical " fragment " again with hydrogen in catalyst existence condition
Lower combination, forms the molecular weight primary hydrogenation products more much lower than coal.Go out reactor product constitute sufficiently complex, including gas,
Liquid, solid three-phase.The main component of gas phase is hydrogen, separates Posterior circle Returning reactor and again participates in reaction；Solid phase is unreacted
Coal, mineral matter and catalyst；Liquid phase is then the fraction such as light oil (raw gasoline), middle oil oil and heavy oil.Liquid phase fraction oil is through upgrading
Processing (such as hydrofinishing, be hydrocracked and reform) obtains the products such as qualified gasoline, diesel oil and aviation kerosine.The liquid of heavy
Gu slurry is through separately obtaining heavy oil and residue further, heavy oil is used for coal slurry as circulating solvent to be prepared.
In existing direct coal liquefaction technology, reactor reaction pressure is up to 17MPa-30Mpa, and hydrogen consumption is up to 6%-
10%, flow process is complicated, and cost of investment is high.Not only to supplement in technical process in a large number new hydrogen in addition it is also necessary to hydrogen supply dissolvent made by recycle oil,
Plant capacity reduces, and the product composition going out liquefying reactor is complicated, and solid-liquid two-phase laminated flow is difficult, and oil productivity is low.
Content of the invention
The technical problem to be solved is that the present situation for prior art provides a kind of reaction condition gentle and hydrogen
The coal direct hydrogenation reaction unit that consumption is little, oil productivity is high.
Another technical problem to be solved by this invention is that the present situation for prior art provides a kind of reaction condition temperature
With and hydrogen consumption is little, oil productivity is high coal direct hydrogenation reaction method.
The present invention solves the technical scheme that adopted of above-mentioned technical problem：This coal direct hydrogenation reaction unit, its feature
It is including being sequentially connected logical gasifying type, fluidisation pyrolysis chamber and separation chamber；
Described vaporizer is hot wall reactor, and its top is provided with for the gasification nozzle to the indoor charging of described gasification；
The lower entrances of described fluidisation pyrolysis chamber connect the lower part outlet of described vaporizer by pipeline；Described fluidisation pyrolysis
The side wall of room is provided with for the coal nozzle to the indoor coal powder of described fluidisation pyrolysis；The upper outlet of described fluidisation pyrolysis chamber
Described separation chamber is connected by pipeline；
The top of described separation chamber is provided with gaseous phase outlet, and the bottom of described separation chamber is provided with solid-phase outlet.
The bottom of fluidisation decomposition chamber is provided with air distribution plate；The outlet of described coal nozzle is towards described air distribution plate.
Described gasification nozzle includes body, and body is sequentially provided with fuel channel, oxygen channel, steam channel from inside to outside
With the first cooling duct；Interlayer between fuel channel and oxygen channel adopts high-abrasive material to prepare.
Using above-mentioned coal direct hydrogenation reaction unit coal direct hydrogenation reaction method it is characterised in that include following steps
Suddenly：
Fuel, oxygen and water vapour enter described vaporizer from described gasification nozzle, in 1000～1700 DEG C, 1～9MPa
Under reacted, generate with CO+H2HTHP synthesis gas for main composition；
Temperature is 1000～1700 DEG C, pressure is the synthesis gas of 3～9MPa together with the coal dust from described coal nozzle
Enter described fluidisation pyrolysis chamber, carry out coal hydrogenation reaction under 600～1500 DEG C, 3～9MPa, generate oil gas and cinder；
Oil gas and cinder enter described separation chamber from described fluidisation pyrolysis chamber and carry out gas solid separation, and the oil gas after separating is from institute
State gaseous phase outlet and drain into downstream, the cinder separating is discharged from described solid-phase outlet；
Described fuel is non-solid fuel；
In described synthesis gas, hydrogen content and the mass ratio of butt coal dust are 4～10%；
Described gasification interior material flow is 0.3～0.5m/s；
The indoor goods fluid speed 0.1～1.5m/s of described fluidisation pyrolysis.
Described fuel is preferably natural gas；The volume ratio of described fuel, oxygen and water vapour is 1：0.6～0.78：0.1～
0.3.
Compared with prior art, coal direct hydrogenation reaction unit provided by the present invention and reaction method can be in temperature relatively
By direct for coal dust catalytic hydrogenation under the reaction condition of sum, then obtain gasoline, diesel oil, aviation kerosine etc. through separating with upgrading processing
Liquiefied product oil and other chemicals；It is not required to be additionally provided hydrogen source, and oil yield is high, environmental friendliness.
Brief description
Fig. 1 is embodiment of the present invention schematic diagram；
Fig. 2 is the cross-sectional schematic of gasification nozzle in the embodiment of the present invention；
Fig. 3 is the partial enlarged drawing of A in Fig. 1.
Specific embodiment
Below in conjunction with accompanying drawing embodiment, the present invention is described in further detail.
As shown in Figure 1 to Figure 3, this coal direct hydrogenation reaction unit includes being sequentially connected logical gasifying type 1, fluidisation pyrolysis chamber
2 and separation chamber 3.
Wherein vaporizer 1 is hot wall 11 structure of reactor, inner lining refractory block 12；, its top is provided with for indoor to gasification
The gasification nozzle 4 of charging；
The lower entrances of fluidisation pyrolysis chamber 2 connect the lower part outlet of vaporizer 1 by pipeline；The side wall of fluidisation pyrolysis chamber 2
It is provided with for the coal nozzle 5 to coal powder in fluidisation pyrolysis chamber 2；The upper outlet of fluidisation pyrolysis chamber 2 is connected by pipeline
Separation chamber 3；
The top of separation chamber 3 is provided with gaseous phase outlet 31, and the bottom of separation chamber 3 is provided with solid-phase outlet 32.
The bottom of fluidisation decomposition chamber 2 is provided with air distribution plate 6；The outlet of coal nozzle 5 is towards air distribution plate 6.
Air distribution plate 6 is the gas distributor of conventional perforated plate construction.
Gasification nozzle 4 includes body, body is sequentially provided with from inside to outside fuel channel 42, oxygen channel 43, steam lead to
Road 44 and the first cooling duct 45；Interlayer 46 between fuel channel 42 and oxygen channel 43 adopts high-abrasive material to prepare.
Using coal direct hydrogenation reaction unit coal direct hydrogenation reaction method it is characterised in that comprising the steps：
Fuel, oxygen and water vapour enter described vaporizer 1 from described gasification nozzle 4, carry out anti-under 1350 DEG C, 4MPa
Should, generate with CO+H2HTHP synthesis gas for main composition；
Temperature is 1350 DEG C, pressure is the HTHP synthesis gas of 4MPa together with the coal dust from described coal nozzle 5
Enter described fluidisation pyrolysis chamber 2, carry out coal hydrogenation reaction under 1100 DEG C, 3.9MPa, generate oil gas and cinder；
Oil gas and cinder enter described separation chamber 3 from described fluidisation pyrolysis chamber 2 and carry out gas solid separation, the oil gas after separating from
Described gaseous phase outlet 31 drains into downstream, and the cinder separating is discharged from described solid-phase outlet 32；
Wherein, described fuel is selected from natural gas；The proportioning (volume ratio) of described fuel, oxygen and water vapour is 1：0.67：
0.14；Fuel can also be the non-solid fuel such as liquefied petroleum gas, synthesis gas, oil gas.
The amount of described institute hydrogen producing and the mass ratio of dry pulverized coal are 5.5%；
Described gasification interior material flow is 0.36m/s；
Described fluidisation pyrolysis interior goods fluid speed 0.8m/s.
The present embodiment is compared with the method for coal liquefaction in prior art, the results are shown in Table 1.
Table 1
| Coal direct liquefaction | Indirect coal liquefaction | Coal destructive distillation | Embodiment | |
| Project water consume | 2.5 ton/ton mark coals | 2.75 ton/ton mark coals | 0.15t/t feed coal | 0.15t/t feed coal |
| CO2 discharges | 5～6 ton/ton oil products | 5 ton/ton oil products | --- | 0.05 ton/ton oil product |
| Hydrogen consumes | Device for producing hydrogen | Device for producing hydrogen | ----- | It is not required to added hydrogen |
Claims (5)
1. a kind of coal direct hydrogenation reaction unit is it is characterised in that include being sequentially connected logical gasifying type (1), fluidisation pyrolysis chamber
And separation chamber (3) (2)；
Described vaporizer (1) is hot wall reactor, and its top is provided with for the gasification nozzle (4) to the indoor charging of described gasification；
The lower entrances of described fluidisation pyrolysis chamber (2) connect the lower part outlet of described vaporizer (1) by pipeline；Described fluidisation heat
The side wall of solution room (2) is provided with for the coal nozzle (5) to the interior coal powder of described fluidisation pyrolysis chamber (2)；Described fluidisation pyrolysis
The upper outlet of room (2) connects described separation chamber (3) by pipeline；
The top of described separation chamber (3) is provided with gaseous phase outlet (31), and the bottom of described separation chamber (3) is provided with solid-phase outlet (32).
2. coal direct hydrogenation reaction unit according to claim 1 is it is characterised in that the bottom of fluidisation decomposition chamber (2) is provided with
Air distribution plate (6)；The outlet of described coal nozzle (5) is towards described air distribution plate (6).
3. coal direct hydrogenation reaction unit according to claim 1 and 2 is it is characterised in that described gasification nozzle (4) includes
Body, body is sequentially provided with fuel channel (42), oxygen channel (43), steam channel (44) and the first cooling from inside to outside logical
Road (45)；Interlayer (46) between fuel channel (42) and oxygen channel (43) adopts high-abrasive material to prepare.
4. using the coal direct hydrogenation reaction of the coal direct hydrogenation reaction unit as described in claims 1 to 3 any claim
Method is it is characterised in that comprise the steps：
Fuel, oxygen and water vapour from described gasification nozzle (4) enter described vaporizer (1), 1000～1700 DEG C, 1～
Reacted under 9MPa, generated with CO+H2HTHP synthesis gas for main composition；
The synthesis gas that temperature is 1000～1700 DEG C, pressure is 3～9MPa is entered together with the coal dust from described coal nozzle (5)
Enter described fluidisation pyrolysis chamber (2), carry out coal hydrogenation reaction under 600～1500 DEG C, 3～9MPa, generate oil gas and cinder；
Oil gas and cinder enter described separation chamber (3) from described fluidisation pyrolysis chamber (2) and carry out gas solid separation, the oil gas after separating from
Described gaseous phase outlet (31) drains into downstream, and the cinder separating is discharged from described solid-phase outlet (32)；
Described fuel is non-solid fuel；
In described synthesis gas, hydrogen content and the mass ratio of butt coal dust are 4～10%；
Described gasification interior material flow is 0.3～0.5m/s；
Goods fluid speed 0.1～1.5m/s in described fluidisation pyrolysis chamber (2).
5. coal direct hydrogenation reaction method according to claim 4 is it is characterised in that described fuel is natural gas；
Wherein, the volume ratio of described fuel, oxygen and water vapour is 1：0.6～0.78：0.1～0.3.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610858504.6A CN106433736A (en) | 2016-09-28 | 2016-09-28 | Direct coal hydrogenation reaction device and method |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201610858504.6A CN106433736A (en) | 2016-09-28 | 2016-09-28 | Direct coal hydrogenation reaction device and method |
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Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102604683A (en) * | 2011-12-20 | 2012-07-25 | 新奥科技发展有限公司 | Method for co-production of synthetic gas and coal tar |
| CN103992824A (en) * | 2014-05-28 | 2014-08-20 | 哈尔滨工业大学 | Double-cyclone coal pyrolysis gasification step converting device and double-cyclone coal pyrolysis gasification step converting method |
| CN104593037A (en) * | 2014-12-19 | 2015-05-06 | 中美新能源技术研发（山西）有限公司 | Composite coal hydrogenation oil refining reactor and oil refining method |
| CN105733688A (en) * | 2016-04-25 | 2016-07-06 | 中美新能源技术研发（山西）有限公司 | Coal liquefaction and coal gasification reactor |
-
2016
- 2016-09-28 CN CN201610858504.6A patent/CN106433736A/en active Pending
Patent Citations (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102604683A (en) * | 2011-12-20 | 2012-07-25 | 新奥科技发展有限公司 | Method for co-production of synthetic gas and coal tar |
| CN103992824A (en) * | 2014-05-28 | 2014-08-20 | 哈尔滨工业大学 | Double-cyclone coal pyrolysis gasification step converting device and double-cyclone coal pyrolysis gasification step converting method |
| CN104593037A (en) * | 2014-12-19 | 2015-05-06 | 中美新能源技术研发（山西）有限公司 | Composite coal hydrogenation oil refining reactor and oil refining method |
| CN105733688A (en) * | 2016-04-25 | 2016-07-06 | 中美新能源技术研发（山西）有限公司 | Coal liquefaction and coal gasification reactor |
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Application publication date: 20170222 |