CN109772233A - Synthesis reaction system and methane synthesizing method with porous type central tube - Google Patents
Synthesis reaction system and methane synthesizing method with porous type central tube Download PDFInfo
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- CN109772233A CN109772233A CN201910152755.6A CN201910152755A CN109772233A CN 109772233 A CN109772233 A CN 109772233A CN 201910152755 A CN201910152755 A CN 201910152755A CN 109772233 A CN109772233 A CN 109772233A
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- central tube
- synthesis
- porous type
- reaction system
- casing
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- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 105
- 238000000034 method Methods 0.000 title claims abstract description 10
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 12
- 230000002194 synthesizing effect Effects 0.000 title claims description 7
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 148
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 71
- 238000006243 chemical reaction Methods 0.000 claims abstract description 63
- 239000003054 catalyst Substances 0.000 claims abstract description 25
- 230000006835 compression Effects 0.000 claims abstract description 18
- 238000007906 compression Methods 0.000 claims abstract description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 37
- 238000001816 cooling Methods 0.000 claims description 20
- 239000007788 liquid Substances 0.000 claims description 17
- 238000000926 separation method Methods 0.000 claims description 5
- 238000004519 manufacturing process Methods 0.000 abstract description 8
- 238000005265 energy consumption Methods 0.000 abstract description 4
- 239000002245 particle Substances 0.000 abstract description 2
- 230000001360 synchronised effect Effects 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 58
- 125000001741 organic sulfur group Chemical group 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 5
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 description 4
- XLOMVQKBTHCTTD-UHFFFAOYSA-N Zinc monoxide Chemical compound [Zn]=O XLOMVQKBTHCTTD-UHFFFAOYSA-N 0.000 description 4
- 238000000746 purification Methods 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 239000000203 mixture Substances 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 230000000737 periodic effect Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000011787 zinc oxide Substances 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- 206010020843 Hyperthermia Diseases 0.000 description 1
- 230000000903 blocking effect Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000001413 cellular effect Effects 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 230000036031 hyperthermia Effects 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 229910052573 porcelain Inorganic materials 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000012495 reaction gas Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000009991 scouring Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/52—Improvements relating to the production of bulk chemicals using catalysts, e.g. selective catalysts
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The invention discloses a kind of synthesis reaction systems with porous type central tube, synthetic reaction device includes reactor shell, central tube and synthesis casing are provided in reactor enclosure body, central tube and synthesis casing coaxial arrangement, the identical micropore of multiple diameters is provided on the tube wall of central tube, it synthesizes and is provided with multiple apertures on the tube wall of casing, the diameter of aperture is greater than the diameter of the micropore, synthesizes and is provided with gap between casing and reactor shell.Compared with prior art, synthetic reaction device production capacity of methanol of the present invention is high, synthesis gas radial centripetal is flowed by central tube built in synthetic reaction device, runner is shorter, and pressure drop is reduced, and increases air speed, improve methanol output, catalyst elements area uses catalyst particle, improves the utilization rate of catalyst inner surface, saves energy consumption.0.1MPa is had dropped using the methanol synthesis reaction system entirety pressure drop of the method for the present invention, so that compression set energy consumption is also synchronous to be reduced.
Description
Technical field
It is raw to belong to methanol for the present invention relates to a kind of synthesis reaction system and methane synthesizing method with porous type central tube
Production field.
Background technique
Methanol is a kind of good clean fuel of combustibility, can be directly used as motor vehicle fuel, can also make with gasoline blend
With, while methanol is also a kind of important Organic Chemicals, is the staple product of one chemical industry of carbon.
At present in methanol production system, system production load is maintained at 105% operation, due to the limit of pressure difference in synthetic tower
System, so that system production load is difficult to continue to improve.
Summary of the invention
The object of the present invention is to provide a kind of synthesis reaction system with porous type central tube and methanol-fueled CLC sides
Method can improve the pressure difference of synthetic reaction device, improve system production load, improve methanol production amount.
In order to solve the above technical problems, the present invention adopts the following technical scheme that: a kind of conjunction with porous type central tube
At reaction system, including synthetic reaction device, heat-exchange device, water cooling plant, equipment for separating methanol, cycle pressure device and oil
Separator, synthetic reaction device are connect with heat-exchange device, and heat-exchange device is connect with water cooling plant, water cooling plant and methanol
Separator connection, equipment for separating methanol are connect with cycle pressure device, and cycle pressure device is connect with oil separating device, oil
It is connect from device with synthetic reaction device；Purified syngas enters synthetic reaction device, in the reaction of synthetic reaction device
Methanol synthesis reaction is carried out in device shell, the pyroreaction gas that methanol synthesis reaction generates enters heat-exchange device, pyroreaction
Gas exchanges heat in heat-exchange device with low-temperature mixed gas, enters water cooling plant with the gas after the heat exchange of low-temperature mixed gas,
It is cooled down in water cooling plant and is condensed out the gas-liquid mixture of first alcohol and water to be condensed out methanol and enters equipment for separating methanol
Crude carbinol is isolated, crude carbinol is then delivered to distillation system and produces refined methanol.Thick first is isolated in equipment for separating methanol
The unreacting gas of alcohol and water, a part, which enters after cycle pressure device, is again introduced into synthetic reaction dress by oil separating device
It sets, to recycle, a part passes through the exhaust being arranged between equipment for separating methanol and cycle pressure device as periodic off-gases
Pipe discharge.
Synthetic reaction device includes reactor shell, and central tube and synthesis casing, central tube are provided in reactor enclosure body
It is coaxially disposed with synthesis casing, is provided with the identical micropore of multiple diameters on the tube wall of central tube, synthesizes and set on the tube wall of casing
Multiple apertures are equipped with, the diameter of aperture is greater than the diameter of the micropore, synthesizes and is provided with gap between casing and reactor shell.
Synthesis casing tube wall on be arranged foraminate purpose be will be net by the methanol-fueled CLC in central tube wall thickness channel, porcelain ball bed
Change gas and diffuses into catalyst bed generation chemical reaction and heat release；Foraminate synthesis casing, which is arranged, can be used as stainless steel wire
Inertia magnetic ball is fixed on central tube and column for the inertia magnetic ball between fixed center pipe outer wall and synthetic catalyst by net
Catalyst unit area between tube bank.The size of micropore is more smaller than aperture, and micropore is the key point for controlling resistance drop, aperture
Can guarantee that inertia magnetic ball cannot pass through casing and catalyst mixed influence reaction effect by airflow scouring, but also have every
The effect of the micropore sintered blocking of Thermal protection central tube.
In a kind of synthesis reaction system with porous type central tube above-mentioned, further include gas-liquid separator, compression set,
Purifying, preheating device, boiler water increasing pump and purified synthesis gas slot；The gas-liquid separator is connect with compression set, compression set with
The connection of purifying, preheating device, purifying, preheating device are connect with purified synthesis gas slot, and the boiler water increasing pump is arranged in purifying, preheating device
On branch line between purified synthesis gas slot；Synthesis gas enters gas-liquid separator and carries out gas-liquid separation, through gas-liquid separation
Synthesis gas enters compression set compression and is pressurized to 7.91MPaG, and purified synthesis gas preheater is for heating through compressing pressurized conjunction
At gas, boiler is added into the synthesis gas after heating by boiler water booster pump before synthesis gas enters purified synthesis gas slot
Then the synthesis gas for removing organic sulfur is passed through synthesis again to decompose micro organic sulfur remaining in the synthesis gas after heating by water
In gas purification tank, organic sulfur is eliminated to remove using the Zinc oxide catalytic containing alumina loaded in purified synthesis gas slot
Micro inorganic sulfur in synthesis gas makes the sulfur content after purifying in synthesis gas be less than 50ppb.
In a kind of synthesis reaction system with porous type central tube above-mentioned, set between synthesis casing and the central tube
It is equipped with catalyst unit area.
In a kind of synthesis reaction system with porous type central tube above-mentioned, the bottom of the reactor shell is provided with
Air inlet is provided with steam (vapor) outlet at the top of reactor shell, is provided with first outlet and second on the side wall of reactor shell
Outlet.Steam (vapor) outlet is for being discharged reaction hot steam.
Micro-pore diameter in a kind of synthesis reaction system with porous type central tube above-mentioned, on the central tube tube wall
For 1.8mm~2.4mm.
It is two neighboring micro- on the central tube tube wall in a kind of synthesis reaction system with porous type central tube above-mentioned
Spacing between hole is 10mm~14mm.
In a kind of synthesis reaction system with porous type central tube above-mentioned, it is provided on the tube wall of the central tube
180000~220000 round micropores.In order to control centre's pipe resistance drop within 30KPa, micropore quantity can at most be set
It is set to 220000.
In a kind of synthesis reaction system with porous type central tube above-mentioned, the perforated area on the central tube is
550000mm2~680000mm2.In order to control centre's pipe resistance drop within 30KPa, perforated area is limited in
550000mm2~680000mm2Within.
In a kind of synthesis reaction system with porous type central tube above-mentioned, the reaction temperature of the synthetic reaction device
For 180 DEG C~330 DEG C, reaction pressure be 5.0MPa~12.0MPa.
The number of openings and perforated area of central tube of the present invention are more reasonable, can be effectively reduced the resistance of synthetic reaction device
Power drop, improves the ability of synthetic reaction device synthesizing methanol, improves the yield of methanol-fueled CLC.
A kind of methane synthesizing method enters central tube by the air inlet of synthetic reaction device including synthesis gas, in
The identical micropore radial direction radiant flux of multiple diameters enters catalyst unit area on heart tube wall, and it is anti-to carry out methanol-fueled CLC in catalyst unit area
It answers.
Compared with prior art, synthetic reaction device production capacity of methanol of the present invention is high, by built in synthetic reaction device
Central tube so that synthesis gas is passed through the micropore radial direction centripetal flow that opens up, central tube wall thickness is 10mm~15mm, opens up micropore shape
At runner it is shorter, pressure drop is reduced, and increases air speed, improves methanol output, and catalyst elements area uses catalyst particle,
The utilization rate for improving catalyst inner surface, saves energy consumption；
Number of aperture and perforated area on central tube of the present invention is more reasonable, and the pressure difference of central tube is stably controlled 30~
Between 40kpa, the resistance drop of synthetic reaction device is set to have reached most ideal range, the refined methanol instant productivity of present system can
Reach 275t/h；By increasing the number of openings of central tube, increasing perforated area, make the air inlet of synthetic reaction device of the present invention
Pressure difference between steam (vapor) outlet can be down to 30kPa or so；The bed temperature distribution in synthetic reaction device catalyst unit area is opposite
Uniformly (since resistance drop declines, it is considered as suitably increasing to a certain extent by the tolerance of per volume of catalyst, is catalyzed
Agent bed dead point is reduced, and bed temperature distribution can be relatively uniform), localized hyperthermia's hot spot is effectively controlled.Present system is raw
Load is produced up to 116%.
0.1MPa is had dropped using the methanol synthesis reaction system entirety pressure drop of the method for the present invention, thus compression set energy consumption
Also synchronous to reduce.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of synthetic reaction device of the invention；
Fig. 2 is the work flow diagram of system of the invention.
Appended drawing reference: 1- first outlet, 101- gas-liquid separator, 102- compression set, 103- purifying, preheating device, 104- pots
Furnace water increasing pump, 105- purified synthesis gas slot, 106- branch line, 2- second outlet, 201- synthetic reaction device, 202- heat are handed over
Changing device, 203- water cooling plant, 204- equipment for separating methanol, 205- cycle pressure device, 206- oil separating device, 3- steam go out
Mouthful, 4- reactor shell, 401- central tube, 402- synthesis casing, 403- catalyst unit area, the gap 404-, 405- air inlet,
4011- micropore, 4021- aperture.
The present invention is further illustrated with reference to the accompanying drawings and detailed description.
Specific embodiment
The embodiment of the present invention 1: a kind of synthesis reaction system with porous type central tube, including synthetic reaction device
201, heat-exchange device 202, water cooling plant 203, equipment for separating methanol 204, cycle pressure device 205 and oil separating device 206,
The synthetic reaction device 201 is connect with heat-exchange device 202, and the heat-exchange device 202 is connect with water cooling plant 203, institute
Water cooling plant 203 to be stated to connect with equipment for separating methanol 204, the equipment for separating methanol 204 is connect with cycle pressure device 205,
The cycle pressure device 205 is connect with oil separating device 206, and oil separating device 206 is connect with synthetic reaction device 201；Its
In, synthetic reaction device 201 includes reactor shell 4, and central tube 401 and synthesis casing are provided in the reactor shell 4
402, the central tube 401 is coaxially disposed with synthesis casing 402, in order to which the synthesis gas after purified treatment radially flows to catalyst unit
Area 403 is provided with the identical micropore 4011 of multiple diameters on the tube wall of central tube 401, synthesizes and is provided on the tube wall of casing 402
Multiple apertures 4021 (as shown in Figure 1), the diameter of aperture 4021 are greater than the diameter of micropore 4011, synthesize casing 402 and reactor
Gap 404 is provided between shell 4.Catalyst unit area 403 is provided between synthesis casing 402 and central tube 401.Gas central tube
4011 diameter of micropore on 401 tube walls is 1.8mm.Spacing on 401 tube wall of central tube between two neighboring micropore is 10mm.For
The pressure difference for reducing central tube offers 180000 round micropores, opening on central tube 401 on the tube wall of central tube 401
Hole area is 550000mm2.The reaction temperature of synthetic reaction device 201 is 180 DEG C, reaction pressure 5.0MPa.
The embodiment of the present invention 2: a kind of synthesis reaction system with porous type central tube, including synthetic reaction device
201, heat-exchange device 202, water cooling plant 203, equipment for separating methanol 204, cycle pressure device 205 and oil separating device 206,
The synthetic reaction device 201 is connect with heat-exchange device 202, and the heat-exchange device 202 is connect with water cooling plant 203, institute
Water cooling plant 203 to be stated to connect with equipment for separating methanol 204, the equipment for separating methanol 204 is connect with cycle pressure device 205,
The cycle pressure device 205 is connect with oil separating device 206, and the oil separating device 206 connects with synthetic reaction device 201
It connects；Wherein, synthetic reaction device 201 includes reactor shell 4, and central tube 401 and synthesis are provided in the reactor shell 4
Casing 402, the central tube 401 are coaxially disposed with synthesis casing 402, are provided on the tube wall of the central tube 401 multiple straight
The identical micropore 4011 of diameter, it is described synthesis casing 402 tube wall on be provided with multiple apertures 4021, the diameter of the aperture 4021
Greater than the diameter of the micropore 4011, gap 404 is provided between the synthesis casing 402 and reactor shell 4.Central tube
4011 diameter of micropore on 401 tube walls is 2mm.Spacing on 401 tube wall of central tube between two neighboring micropore is 12mm.Center
200000 round micropores are provided on the tube wall of pipe 401.Perforated area on central tube 401 is 6800000mm2。
Further, which further includes gas-liquid separator 101, compression set 102, purifying, preheating device 103, boiler water increasing
Add pump 104 and purified synthesis gas slot 105；The gas-liquid separator 101 is connect with compression set 102, compression set 102 and purification
Preheater 103 connects, and purifying, preheating device 103 is connect with purified synthesis gas slot 105, and the boiler water increasing pump 104 is arranged net
Change on the branch line 106 between preheater 103 and purified synthesis gas slot 105.It is set between synthesis casing 402 and central tube 401
It is equipped with catalyst unit area 403.The reaction temperature of synthetic reaction device 201 is 250 DEG C, reaction pressure 10MPa.
The embodiment of the present invention 3: a kind of synthesis reaction system with porous type central tube, including synthetic reaction device
201, heat-exchange device 202, water cooling plant 203, equipment for separating methanol 204, cycle pressure device 205 and oil separating device 206,
The synthetic reaction device 201 is connect with heat-exchange device 202, and the heat-exchange device 202 is connect with water cooling plant 203, institute
Water cooling plant 203 to be stated to connect with equipment for separating methanol 204, the equipment for separating methanol 204 is connect with cycle pressure device 205,
The cycle pressure device 205 is connect with oil separating device 206, and the oil separating device 206 connects with synthetic reaction device 201
It connects；Wherein, synthetic reaction device 201 includes reactor shell 4, and central tube 401 and synthesis are provided in the reactor shell 4
Casing 402, the central tube 401 are coaxially disposed with synthesis casing 402, are provided on the tube wall of the central tube 401 multiple straight
The identical micropore 4011 of diameter, it is described synthesis casing 402 tube wall on be provided with multiple apertures 4021, the diameter of the aperture 4021
Greater than the diameter of the micropore 4011, gap 404 is provided between the synthesis casing 402 and reactor shell 4.Reactor enclosure
The bottom of body 4 is provided with air inlet 405, and the top of the reactor shell 4 is provided with steam (vapor) outlet 3, the reactor shell 4
Side wall on be provided with first outlet 1 and second outlet 2.
Further, which further includes gas-liquid separator 101, compression set 102, purifying, preheating device 103, boiler water increasing
Add pump 104 and purified synthesis gas slot 105；The gas-liquid separator 101 is connect with compression set 102, compression set 102 and purification
Preheater 103 connects, and purifying, preheating device 103 is connect with purified synthesis gas slot 105, and the boiler water increasing pump 104 is arranged net
Change on the branch line 106 between preheater 103 and purified synthesis gas slot 105.It is set between synthesis casing 402 and central tube 401
It is equipped with catalyst unit area 403.4011 diameter of micropore on 401 tube wall of central tube is 2.4mm.Adjacent two on 401 tube wall of central tube
Spacing between a micropore is 14mm.220000 round micropores are provided on the tube wall of central tube 401.On central tube 401
Perforated area is 680000mm2.The reaction temperature of synthetic reaction device 201 is 330 DEG C, reaction pressure 12.0MPa.
The embodiment of the present invention 4: a kind of methane synthesizing method passes through the air inlet of synthetic reaction device 201 including synthesis gas
Mouth 405 is being catalyzed into central tube 401 by the micropore radial inflow catalyst unit area 403 being arranged on 401 tube wall of central tube
Cellular zone 403 carries out methanol synthesis reaction.
The working principle of the invention:
(synthesis gas is the per-meate side hydrogen-rich that the fresh synthesis gas and film recovery unit of unit are washed from low-temp methanol to synthesis gas
The gaseous mixture of gas) enter the progress gas-liquid separation of gas-liquid separator 101, the synthesis gas through gas-liquid separation enters the pressure of compression set 102
Contracting is pressurized to 7.91MPaG, and pressurized synthesis gas is then heated to 150 DEG C by synthesizer purifying, preheating device 103, is passed through
The boiler water booster pump boiler water that spray flow is 2.08t/h into the synthesis gas after pressurization heating, after decomposing pressurization heating
Synthesis gas in remaining micro organic sulfur, then the synthesis gas for removing organic sulfur is passed through in purified synthesis gas slot 105 again,
It is removed in the synthesis gas for eliminating organic sulfur using the Zinc oxide catalytic containing alumina loaded in purified synthesis gas slot 105
Micro inorganic sulfur makes the sulfur content after purifying in synthesis gas be less than 50ppb.
Through the synthesis gas (synthesis gas includes carbon monoxide, carbon dioxide and hydrogen after purification) of above-mentioned purified treatment a part
Into synthetic reaction device 201, methanol synthesis reaction, the height that methanol synthesis reaction generates are carried out in synthetic reaction device 201
Warm reaction gas enters heat-exchange device 202, and pyroreaction gas exchanges heat in heat-exchange device 202 with low-temperature mixed gas, with
Gas after the heat exchange of low-temperature mixed gas enters water cooling plant 203, is cooled down in water cooling plant 203 to be condensed out first
Alcohol, the gas-liquid mixture for being condensed out first alcohol and water enter equipment for separating methanol 204 and isolate crude carbinol, then convey crude carbinol
Refined methanol is produced to distillation system.Isolate the unreacting gas of crude carbinol and water in equipment for separating methanol 204, a part into
Enter and synthetic reaction device 201 is again introduced by oil separating device 206 after cycle pressure device 205, to recycle, another portion
It is allocated as passing through the exhaust pipe being arranged between equipment for separating methanol 204 and cycle pressure device 205 discharge for periodic off-gases.
Wherein, the synthesis gas of purified processing enters central tube 401 from the air inlet 405 of 201 bottom of synthetic reaction device,
The equally distributed micropore of institute enters catalyst unit area 403 from the tube wall surrounding of central tube 401, and methanol synthesis reaction occurs.
Claims (10)
1. a kind of synthesis reaction system with porous type central tube, which is characterized in that including synthetic reaction device (201), heat
Switch (202), water cooling plant (203), equipment for separating methanol (204), cycle pressure device (205) and oil separating device
(206), the synthetic reaction device (201) connect with heat-exchange device (202), and the heat-exchange device (202) and water cooling fill
Set (203) connection, the water cooling plant (203) connect with equipment for separating methanol (204), the equipment for separating methanol (204) and
Cycle pressure device (205) connection, the cycle pressure device (205) connect with oil separating device (206), the oil separation dress
(206) are set to connect with synthetic reaction device (201)；
The synthetic reaction device (201) includes reactor shell (4), is provided with central tube in the reactor shell (4)
(401) it is coaxially disposed with synthesis casing (402), the central tube (401) and synthesis casing (402), the central tube (401)
It is provided with the identical micropore of multiple diameters (4011) on tube wall, is provided with multiple apertures on the tube wall of synthesis casing (402)
(4021), the diameter of the aperture (4021) is greater than the diameter of the micropore (4011), the synthesis casing (402) and reactor
Gap (404) are provided between shell (4).
2. a kind of synthesis reaction system with porous type central tube according to claim 1, which is characterized in that further include
Gas-liquid separator (101), compression set (102), purifying, preheating device (103), boiler water increasing pump (104) and purified synthesis gas slot
(105)；The gas-liquid separator (101) connect with compression set (102), and compression set (102) and purifying, preheating device (103) are even
It connects, purifying, preheating device (103) is connect with purified synthesis gas slot (105), and the boiler water increasing pump (104) is arranged in purifying, preheating
On branch line (106) between device (103) and purified synthesis gas slot (105).
3. a kind of synthesis reaction system with porous type central tube according to claim 1, which is characterized in that the conjunction
Catalyst unit area (403) are provided between packaged tube (402) and central tube (401).
4. a kind of synthesis reaction system with porous type central tube according to claim 1, which is characterized in that described anti-
It answers the bottom of device shell (4) to be provided with air inlet (405), is provided with steam (vapor) outlet (3) at the top of the reactor shell (4),
First outlet (1) and second outlet (2) are provided on the side wall of the reactor shell (4).
5. a kind of synthesis reaction system with porous type central tube according to claim 1, which is characterized in that in described
Micropore (4011) diameter on heart pipe (401) tube wall is 1.8mm~2.4mm.
6. a kind of synthesis reaction system with porous type central tube according to claim 1, which is characterized in that in described
Spacing on heart pipe (401) tube wall between two neighboring micropore is 10mm~14mm.
7. a kind of synthesis reaction system with porous type central tube according to claim 1, which is characterized in that in described
180000~220000 round micropores are provided on the tube wall of heart pipe (401).
8. a kind of synthesis reaction system with porous type central tube according to claim 1, which is characterized in that in described
Perforated area on heart pipe (401) is 550000mm2~680000mm2。
9. a kind of synthesis reaction system with porous type central tube according to claim 1, which is characterized in that the conjunction
Reaction temperature at reaction unit (201) is 180 DEG C~330 DEG C, reaction pressure is 5.0MPa~12.0MPa.
10. using a kind of methane synthesizing method of system described in any claim in claim 1~9, which is characterized in that packet
It includes synthesis gas and central tube (401) is entered by the air inlet (405) of synthetic reaction device (201), pass through central tube (401) tube wall
The micropore radial inflow catalyst unit area (403) of upper setting carries out methanol synthesis reaction in catalyst unit area (403).
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| CN201910152755.6A CN109772233A (en) | 2019-02-28 | 2019-02-28 | Synthesis reaction system and methane synthesizing method with porous type central tube |
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| CN201910152755.6A CN109772233A (en) | 2019-02-28 | 2019-02-28 | Synthesis reaction system and methane synthesizing method with porous type central tube |
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