CN209696864U - Synthesis reaction system with porous type central tube - Google Patents
Synthesis reaction system with porous type central tube Download PDFInfo
- Publication number
- CN209696864U CN209696864U CN201920261361.XU CN201920261361U CN209696864U CN 209696864 U CN209696864 U CN 209696864U CN 201920261361 U CN201920261361 U CN 201920261361U CN 209696864 U CN209696864 U CN 209696864U
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- Prior art keywords
- central tube
- synthesis
- porous type
- casing
- reaction system
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- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 95
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims abstract description 138
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 63
- 238000006243 chemical reaction Methods 0.000 claims abstract description 57
- 239000003054 catalyst Substances 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
- 230000006835 compression Effects 0.000 claims description 18
- 238000007906 compression Methods 0.000 claims description 18
- 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 3
- 239000002245 particle Substances 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 55
- 125000001741 organic sulfur group Chemical group 0.000 description 6
- 238000010438 heat treatment Methods 0.000 description 5
- 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
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- 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
- 238000006555 catalytic reaction Methods 0.000 description 2
- 230000001413 cellular 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
- 238000000746 purification Methods 0.000 description 2
- 239000012495 reaction gas Substances 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
- 239000003795 chemical substances by application Substances 0.000 description 1
- 239000008246 gaseous mixture Substances 0.000 description 1
- 230000036031 hyperthermia Effects 0.000 description 1
- 238000000034 method Methods 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
- 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
- 230000001360 synchronised effect Effects 0.000 description 1
- 230000002194 synthesizing effect Effects 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
Abstract
The utility model 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, the utility model synthetic reaction device production capacity of methanol 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.
Description
Technical field
The utility model relates to a kind of synthesis reaction systems with porous type central tube, belong to methanol 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
In, system production load is maintained at 105% operation, due to the limitation of pressure difference in synthetic tower so that system production load be difficult to after
It is continuous to improve.
Utility model content
The purpose of the utility model is to provide a kind of synthesis reaction systems with porous type central tube, can improve
The pressure difference of synthetic reaction device improves system production load, improves methanol production amount.
In order to solve the above technical problems, the utility model adopts the following technical solutions: a kind of have porous type central tube
Synthesis reaction system, including synthetic reaction device, heat-exchange device, water cooling plant, equipment for separating methanol, cycle pressure device
And oil separating device, synthetic reaction device are connect with heat-exchange device, heat-exchange device is connect with water cooling plant, water cooling plant with
Equipment for separating methanol connection, equipment for separating methanol are connect with cycle pressure device, and cycle pressure device is connect with oil separating device,
Oil separating device is connect with synthetic reaction device；Purified syngas enters synthetic reaction device, in synthetic reaction device
Methanol synthesis reaction is carried out in reactor enclosure body, the pyroreaction gas that methanol synthesis reaction generates enters heat-exchange device, high temperature
Reaction gas exchanges heat in heat-exchange device with low-temperature mixed gas, enters water cooling dress with the gas after the heat exchange of low-temperature mixed gas
It sets, is cooled down in water cooling plant and be condensed out the gas-liquid mixture of first alcohol and water to be condensed out methanol and enter methanol point
Crude carbinol is isolated from device, crude carbinol is then delivered to distillation system and produces refined methanol.It is separated in equipment for separating methanol
The unreacting gas of crude carbinol and water out, a part, which enters after cycle pressure device, is again introduced into synthesis instead by oil separating device
Device is answered, to recycle, a part is as periodic off-gases by being arranged between equipment for separating methanol and cycle pressure device
Exhaust 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 the utility model central tube are more reasonable, can be effectively reduced synthetic reaction device
Resistance drop, improve synthetic reaction device synthesizing methanol ability, improve the yield of methanol-fueled CLC.
Compared with prior art, the utility model synthetic reaction device production capacity of methanol is high, passes through synthetic reaction device
Built-in central tube makes synthesis gas pass through the micropore radial direction centripetal flow opened up, and central tube wall thickness is 10mm~15mm, opens up micro-
The runner that hole is formed is shorter, and pressure drop is reduced, and increases air speed, improves methanol output, catalyst elements area is urged using little particle
Agent improves the utilization rate of catalyst inner surface, saves energy consumption；
Number of aperture and perforated area on the utility model central tube is more reasonable, and the pressure difference of central tube is stably controlled
Between 30~40kpa, the resistance drop of synthetic reaction device is made to have reached most ideal range, the refined methanol wink of Tthe utility model system
When yield can reach 275t/h；By increasing the number of openings of central tube, increasing perforated area, make the utility model synthetic reaction
Pressure difference between the air inlet and steam (vapor) outlet of device can be down to 30kPa or so；The bed in synthetic reaction device catalyst unit area
Temperature Distribution is relatively uniform (since resistance drop declines, to be considered as through the tolerance of per volume of catalyst to a certain extent
Appropriate to increase, catalyst bed dead point is reduced, and bed temperature distribution can be relatively uniform), localized hyperthermia's hot spot is effectively controlled；
Tthe utility model system produce load is up to 116%.The utility model synthesis reaction system entirety pressure drop has dropped 0.1MPa, from
And compression set energy consumption also synchronous reduction.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of the synthetic reaction device of the utility model；
Fig. 2 is the work flow diagram of the system of the utility model.
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.
The utility model is further described with reference to the accompanying drawings and detailed description.
Specific embodiment
The embodiments of the present invention 1: a kind of synthesis reaction system with porous type central tube, including synthetic reaction dress
Set 201, heat-exchange device 202, water cooling plant 203, equipment for separating methanol 204, cycle pressure device 205 and oil separating device
206, synthetic reaction device 201 is connect with heat-exchange device 202, and heat-exchange device 202 is connect with water cooling plant 203, water cooling dress
It sets 203 to connect with equipment for separating methanol 204, equipment for separating methanol 204 is connect with cycle pressure device 205, cycle pressure device
205 connect with oil separating device 206, and oil separating device 206 is connect with synthetic reaction device 201；Wherein, synthetic reaction device
201 include reactor shell 4, and central tube 401 and synthesis casing 402, central tube 401 and synthesis are provided in reactor shell 4
Casing 402 is coaxially disposed, in order to which the synthesis gas after purified treatment radially flows to catalyst unit area 403, on the tube wall of central tube 401
It is provided with the identical micropore 4011 of multiple diameters, synthesizes and be provided with multiple apertures 4021 on the tube wall of casing 402 (such as Fig. 1 institute
Show), the diameter of aperture 4021 is greater than the diameter of micropore 4011, synthesizes and is provided with gap between casing 402 and reactor shell 4
404.Catalyst unit area 403 is provided between synthesis casing 402 and central tube 401.Micropore 4011 on 401 tube wall of gas central tube
Diameter is 1.8mm.Spacing on 401 tube wall of central tube between two neighboring micropore is 10mm.In order to reduce the pressure difference of central tube,
180000 round micropores are offered on the tube wall of central tube 401, the perforated area on central tube 401 is 550000mm2.It closes
Reaction temperature at reaction unit 201 is 180 DEG C, reaction pressure 5.0MPa.
The embodiments of the present invention 2: a kind of synthesis reaction system with porous type central tube, including synthetic reaction dress
Set 201, heat-exchange device 202, water cooling plant 203, equipment for separating methanol 204, cycle pressure device 205 and oil separating device
206, synthetic reaction device 201 is connect with heat-exchange device 202, and heat-exchange device 202 is connect with water cooling plant 203, water cooling dress
It sets 203 to connect with equipment for separating methanol 204, equipment for separating methanol 204 is connect with cycle pressure device 205, cycle pressure device
205 connect with oil separating device 206, and oil separating device 206 is connect with synthetic reaction device 201；Wherein, synthetic reaction device
201 include reactor shell 4, and central tube 401 and synthesis casing 402, central tube 401 and synthesis are provided in reactor shell 4
Casing 402 is coaxially disposed, and the identical micropore 4011 of multiple diameters is provided on the tube wall of central tube 401, synthesizes the pipe of casing 402
Multiple apertures 4021 are provided on wall, the diameter of aperture 4021 is greater than the diameter of micropore 4011, synthesizes casing 402 and reactor enclosure
Gap 404 is provided between body 4.4011 diameter of micropore on 401 tube wall of central tube is 2mm.Adjacent two on 401 tube wall of central tube
Spacing between a micropore is 12mm.200000 round micropores are provided on the tube wall of central tube 401.On central tube 401
Perforated area is 0000mm2。
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；Gas-liquid separator 101 is connect with compression set 102, compression set 102 and purifying, preheating
Device 103 connects, and purifying, preheating device 103 is connect with purified synthesis gas slot 105, and boiler water increasing pump 104 is arranged in purifying, preheating device
On branch line 106 between 103 and purified synthesis gas slot 105.Catalysis is provided between synthesis casing 402 and central tube 401
Cellular zone 403.The reaction temperature of synthetic reaction device 201 is 250 DEG C, reaction pressure 10MPa.
The embodiments of the present invention 3: a kind of synthesis reaction system with porous type central tube, including synthetic reaction dress
Set 201, heat-exchange device 202, water cooling plant 203, equipment for separating methanol 204, cycle pressure device 205 and oil separating device
206, synthetic reaction device 201 is connect with heat-exchange device 202, and heat-exchange device 202 is connect with water cooling plant 203, water cooling dress
It sets 203 to connect with equipment for separating methanol 204, equipment for separating methanol 204 is connect with cycle pressure device 205, cycle pressure device
205 connect with oil separating device 206, and oil separating device 206 is connect with synthetic reaction device 201；Wherein, synthetic reaction device
201 include reactor shell 4, and central tube 401 and synthesis casing 402, central tube 401 and synthesis are provided in reactor shell 4
Casing 402 is coaxially disposed, and the identical micropore 4011 of multiple diameters is provided on the tube wall of central tube 401, synthesizes the pipe of casing 402
Multiple apertures 4021 are provided on wall, the diameter of aperture 4021 is greater than the diameter of micropore 4011, synthesizes casing 402 and reactor enclosure
Gap 404 is provided between body 4.The bottom of reactor shell 4 is provided with air inlet 405, and the top of reactor shell 4 is provided with
Steam (vapor) outlet 3 is provided with first outlet 1 and second outlet 2 on the side wall of reactor shell 4.
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；Gas-liquid separator 101 is connect with compression set 102, compression set 102 and purifying, preheating
Device 103 connects, and purifying, preheating device 103 is connect with purified synthesis gas slot 105, and boiler water increasing pump 104 is arranged in purifying, preheating device
On branch line 106 between 103 and purified synthesis gas slot 105.Catalysis is provided between synthesis casing 402 and central tube 401
Cellular zone 403.4011 diameter of micropore on 401 tube wall of central tube is 2.4mm.On 401 tube wall of central tube two neighboring micropore it
Between spacing be 14mm.220000 round micropores are provided on the tube wall of central tube 401.Perforated area on central tube 401
For 680000mm2.The reaction temperature of synthetic reaction device 201 is 330 DEG C, reaction pressure 12.0MPa.
Working principle of the utility model is: synthesis gas (synthesis gas be washed from low-temp methanol the fresh synthesis gas of unit with
The gaseous mixture of the per-meate side hydrogen rich gas of film recovery unit) enter the progress gas-liquid separation of gas-liquid separator 101, the conjunction through gas-liquid separation
Enter the compression of compression set 102 at gas and be pressurized to 7.91MPaG, then passes through synthesizer purifying, preheating device 103 for pressurized conjunction
150 DEG C are heated at gas, passes through the boiler water booster pump boiler that spray flow is 2.08t/h into the synthesis gas after pressurization heating
Then water is again led to the synthesis gas for removing organic sulfur with decomposing micro organic sulfur remaining in the synthesis gas after pressurization heating
Enter in purified synthesis gas slot 105, is removed using the Zinc oxide catalytic containing alumina loaded in purified synthesis gas slot 105
In addition to inorganic sulfur micro in the synthesis gas of organic sulfur, the sulfur content after purifying in synthesis gas is made to 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 (9)
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.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920261361.XU CN209696864U (en) | 2019-02-28 | 2019-02-28 | Synthesis reaction system with porous type central tube |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920261361.XU CN209696864U (en) | 2019-02-28 | 2019-02-28 | Synthesis reaction system with porous type central tube |
Publications (1)
| Publication Number | Publication Date |
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| CN209696864U true CN209696864U (en) | 2019-11-29 |
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ID=68642916
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109772233A (en) * | 2019-02-28 | 2019-05-21 | 中煤陕西榆林能源化工有限公司 | Synthesis reaction system and methane synthesizing method with porous type central tube |
-
2019
- 2019-02-28 CN CN201920261361.XU patent/CN209696864U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109772233A (en) * | 2019-02-28 | 2019-05-21 | 中煤陕西榆林能源化工有限公司 | Synthesis reaction system and methane synthesizing method with porous type central tube |
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