CN209702624U - The parallel methanol synthesis reaction system of double-reactor - Google Patents
The parallel methanol synthesis reaction system of double-reactor Download PDFInfo
- Publication number
- CN209702624U CN209702624U CN201920261344.6U CN201920261344U CN209702624U CN 209702624 U CN209702624 U CN 209702624U CN 201920261344 U CN201920261344 U CN 201920261344U CN 209702624 U CN209702624 U CN 209702624U
- Authority
- CN
- China
- Prior art keywords
- synthesis
- reactor
- connect
- separator
- gas
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 title claims abstract description 171
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 160
- 230000015572 biosynthetic process Effects 0.000 claims abstract description 136
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 24
- 230000006835 compression Effects 0.000 claims description 17
- 238000007906 compression Methods 0.000 claims description 17
- 239000007788 liquid Substances 0.000 claims description 17
- 239000003054 catalyst Substances 0.000 claims description 6
- 238000004519 manufacturing process Methods 0.000 abstract description 7
- 238000010276 construction Methods 0.000 abstract description 2
- 239000007789 gas Substances 0.000 description 60
- 238000000926 separation method Methods 0.000 description 9
- 238000001816 cooling Methods 0.000 description 6
- 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
- 238000006243 chemical reaction Methods 0.000 description 4
- 229910052717 sulfur Inorganic materials 0.000 description 4
- 239000011593 sulfur Substances 0.000 description 4
- 238000004821 distillation Methods 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
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-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
- 230000000994 depressogenic effect Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 239000000446 fuel Substances 0.000 description 2
- 239000008246 gaseous mixture 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
- 238000010685 alcohol synthesis reaction Methods 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
- 230000004907 flux Effects 0.000 description 1
- 238000001727 in vivo Methods 0.000 description 1
- 238000000034 method Methods 0.000 description 1
- 239000012466 permeate Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
The utility model discloses a kind of parallel methanol synthesis reaction systems of double-reactor, including the first synthesis reactor, the second synthesis reactor, circulator compressor and oil separating device, first synthesis reactor is connect with the first separator, second synthesis reactor is connect with the second separator, first separator and the second separator are connect with the air inlet of circulator compressor, circulator compressor is connect with oil separating device, and oil separating device is connect with the first synthesis reactor and the second synthesis reactor respectively.The parallel methanol synthesis reaction system of this double-reactor of the utility model, there is no structure limitation between first synthesis reactor and the second synthesis reactor, it is capable of handling the virgin gas of the same scale of construction, therefore the outlet temperature and pressure drop of the first synthesis reactor or the second synthesis reactor are not in the problem of rapidly raising by way of increasing virgin gas, it will not influence production, can be improved methanol production amount.
Description
Technical field
The utility model relates to a kind of parallel methanol synthesis reaction systems of double-reactor, 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.
Methanol-fueled CLC segment structure (as shown in Figure 2), the essence of the methanol-fueled CLC segment structure in existing methanol production system
Two groups of methanol synthesis reactors of series connection are illustrated in figure 3, the fresh tolerance into first group of methanol synthesis reactor is
414102Nm3/ h, the fresh tolerance into second group of methanol synthesis reactor are 103526Nm3/h.Due to entering second group of methanol
The virgin gas of synthesis reactor from first group of methanol synthesis reactor circulating air, thus enter second group of methanol-fueled CLC it is anti-
The fresh tolerance of device is answered to be lower than the circulating flow rate into first group of methanol synthesis reactor.If being mentioned by way of increasing virgin gas
When high methanol yield, due to the structure limitation of two groups of methanol synthesis reactor tandem connections, first group of methanol synthesis reactor
Outlet temperature and pressure drop can rapidly increase, cause system that can not produce.
Utility model content
The purpose of the utility model is to provide one kind, and the double of methanol output can be improved by way of increasing virgin gas
The parallel methanol synthesis reaction system of reactor.
In order to solve the above technical problems, the utility model adopts the following technical solutions: a kind of parallel first of double-reactor
Alcohol synthesis reaction system, including the first synthesis reactor, the second synthesis reactor, circulator compressor and oil separating device, the
One synthesis reactor is connect with the first separator, and the second synthesis reactor is connect with the second separator, the first separator and second
Separator is connect with the air inlet of circulator compressor, and circulator compressor is connect with oil separating device, oil separating device point
It is not connect with the first synthesis reactor and the second synthesis reactor.
In the parallel methanol synthesis reaction system of a kind of double-reactor above-mentioned, first synthesis reactor and second is closed
It include reactor shell, central tube and synthesis casing at reactor, the central tube and synthesis casing are arranged in reactor enclosure
In vivo, the central tube and synthesis casing coaxial arrangement.
In the parallel methanol synthesis reaction system of a kind of double-reactor 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, and the synthesis gas through gas-liquid separation enters compression set compression and increases
It is depressed into 7.91MPaG, purified synthesis gas preheater enters synthesis gas in synthesis gas for heating through compressing pressurized synthesis gas
Pass through boiler water booster pump before purification tank and boiler water is added into the synthesis gas after heating, to decompose in the synthesis gas after heating
The synthesis gas for removing organic sulfur, is then passed through in purified synthesis gas slot again, utilizes purified synthesis gas by remaining micro organic sulfur
The Zinc oxide catalytic containing alumina that loads in slot removes inorganic sulfur micro in the synthesis gas for eliminate organic sulfur, makes net
Sulfur content after change in synthesis gas is less than 50ppb.
In the parallel methanol synthesis reaction system of a kind of double-reactor above-mentioned, set between synthesis casing and the central tube
It is equipped with catalyst unit area.
In the parallel methanol synthesis reaction system of a kind of double-reactor above-mentioned, it is provided at the top of the reactor shell
Steam (vapor) outlet is provided with first outlet and second outlet on the side wall of the reactor shell.
When system is run, virgin gas enters the first synthesis reactor, virgin gas by the air inlet of synthetic reaction device into
Enter central tube, catalyst unit area is entered by the identical micropore radial direction radiant flux of diameters multiple on central tube tube wall, in the first synthesis
The catalyst unit area of reactor carries out methanol synthesis reaction.The pyroreaction gas that methanol synthesis reaction generates sequentially enters setting and exists
Heat-exchange device and water cooling plant between first synthesis reactor and the first separator, pyroreaction gas is in heat-exchange device
It exchanges heat with low-temperature mixed gas, enters water cooling plant with the gas after the heat exchange of low-temperature mixed gas, carried out in water cooling plant cold
But cool down to be condensed out methanol, the gas-liquid mixture for being condensed out first alcohol and water enters the first separator, isolates crude carbinol, then
Crude carbinol is delivered to distillation system and produces refined methanol.The unreacting gas of crude carbinol and water is isolated in the first separator,
A part, which enters after circulator compressor, is again introduced into the first synthesis reactor or the second synthesis reactor by oil separating device,
To recycle, a part passes through the exhaust pipe row being arranged between the first separator and circulator compressor as periodic off-gases
Out.
Similarly, virgin gas enters the second synthesis reactor, carries out methanol in the reactor enclosure body of the second synthesis reactor
Synthetic reaction, the pyroreaction gas that methanol synthesis reaction generates, which sequentially enters, to be arranged in the second synthesis reactor and the second separator
Between heat-exchange device and water cooling plant, pyroreaction gas exchanges heat in heat-exchange device with low-temperature mixed gas, and low
Gas after warm gaseous mixture heat exchange enters water cooling plant, is cooled down in water cooling plant to be condensed out methanol, is condensed out
The gas-liquid mixture of first alcohol and water enters the second separator, isolates crude carbinol, crude carbinol is then delivered to distillation system system
Take refined methanol.The unreacting gas of crude carbinol and water is isolated in the second separator, after a part enters circulator compressor
It is again introduced into the second synthesis reactor or the first synthesis reactor by oil separating device, to recycle, a part is used as and speeds
It deflates through the exhaust pipe discharge being arranged between the second separator and circulator compressor.
Compared with prior art, the parallel methanol synthesis reaction system of this double-reactor of the utility model, the first synthesis
There is no structure limitation between reactor and the second synthesis reactor, be capable of handling the virgin gas of the same scale of construction, therefore passes through increase
The first synthesis reactor of mode of virgin gas or the outlet temperature of the second synthesis reactor and pressure drop are not in rapidly raised
Problem will not influence production, can be improved methanol production amount.The parallel methanol synthesis reaction of this double-reactor of the utility model
The refined methanol instant productivity of system can reach 275t/h.
Detailed description of the invention
Fig. 1 is the structural schematic diagram of Tthe utility model system；
Fig. 2 is methanol-fueled CLC segment structure figure in existing methanol production system；
Fig. 3 is the structure diagram of Fig. 2.
Appended drawing reference: the first synthesis reactor of 1-, the second synthesis reactor of 2-, 3- circulator compressor, 4- oil separation dress
It sets, the first separator of 5-, the second separator of 6-, 11- gas-liquid separator, 12- compression set, 13- purifying, preheating device, 14- boiler
Water increasing pump, 15- purified synthesis gas slot, 16- branch line, first group of methanol synthesis reactor of 17-, second group of methanol of 18- close
At reactor.
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 parallel methanol synthesis reaction system of double-reactor, including the first synthesis are anti-
Answer device 1, the second synthesis reactor 2, circulator compressor 3 and oil separating device 4, first synthesis reactor 1 and first point
It is connected from device 5, second synthesis reactor 2 is connect with the second separator 6, first separator 5 and the second separator 6
It is connect with the air inlet of circulator compressor 3, the circulator compressor 3 is connect with oil separating device 4, the oil separation dress
4 are set to connect with the first synthesis reactor 1 and the second synthesis reactor 2 respectively.
The embodiments of the present invention 2: a kind of parallel methanol synthesis reaction system of double-reactor, including the first synthesis are anti-
Answer device 1, the second synthesis reactor 2, circulator compressor 3 and oil separating device 4, first synthesis reactor 1 and first point
It is connected from device 5, second synthesis reactor 2 is connect with the second separator 6, first separator 5 and the second separator 6
It is connect with the air inlet of circulator compressor 3, the circulator compressor 3 is connect with oil separating device 4, the oil separation dress
4 are set to connect with the first synthesis reactor 1 and the second synthesis reactor 2 respectively.First synthesis reactor 1 and the second synthesis reactor
2 include reactor shell, central tube and synthesis casing, and the central tube and synthesis casing are arranged in reactor enclosure body, institute
State central tube and synthesis casing coaxial arrangement.The identical micropore 801 of multiple diameters is provided on the tube wall of central tube.Central tube
The diameter of micropore 801 is 1.8mm on wall；Spacing on the central tube tube wall between two neighboring micropore 801 is 10mm.Center
180000 round micropores 801 are provided on the tube wall of pipe.Perforated area on central tube is 550000mm2。
The embodiments of the present invention 3: a kind of parallel methanol synthesis reaction system of double-reactor, including the first synthesis are anti-
Answer device 1, the second synthesis reactor 2, circulator compressor 3 and oil separating device 4, first synthesis reactor 1 and first point
It is connected from device 5, second synthesis reactor 2 is connect with the second separator 6, first separator 5 and the second separator 6
It is connect with the air inlet of circulator compressor 3, the circulator compressor 3 is connect with oil separating device 4, the oil separation dress
4 are set to connect with the first synthesis reactor 1 and the second synthesis reactor 2 respectively.First synthesis reactor 1 and the second synthetic reaction
Device 2 includes reactor shell, central tube and synthesis casing, and the central tube and synthesis casing are arranged in reactor enclosure body,
The central tube and synthesis casing coaxial arrangement.The identical micropore 801 of multiple diameters is provided on the tube wall of central tube.Further include
Gas-liquid separator 11, compression set 12, purifying, preheating device 13, boiler water increasing pump 14 and purified synthesis gas slot 15；The gas-liquid
Separator 11 is connect with compression set 12, and compression set 12 is connect with purifying, preheating device 13, and purifying, preheating device 13 and synthesis gas are net
Change slot 15 to connect, the branch line between purifying, preheating device 13 and purified synthesis gas slot 15 is arranged in the boiler water increasing pump 14
On 16.Catalyst unit area 11 is provided between synthesis casing and central tube.Steam (vapor) outlet is provided at the top of reactor shell, institute
It states and is provided with first outlet and second outlet on the side wall of reactor shell.The diameter of micropore 801 is 2mm on central tube tube wall；
Spacing on the central tube tube wall between two neighboring micropore 801 is 14mm.220000 are provided on the tube wall of central tube
Round micropore 801.Perforated area on central tube is 680000mm2。
The embodiments of the present invention 4: a kind of parallel methanol synthesis reaction system of double-reactor, including the first synthesis are anti-
Answer device 1, the second synthesis reactor 2, circulator compressor 3 and oil separating device 4, first synthesis reactor 1 and first point
It is connected from device 5, second synthesis reactor 2 is connect with the second separator 6, first separator 5 and the second separator 6
It is connect with the air inlet of circulator compressor 3, the circulator compressor 3 is connect with oil separating device 4, the oil separation dress
4 are set to connect with the first synthesis reactor 1 and the second synthesis reactor 2 respectively.First synthesis reactor 1 and the second synthetic reaction
Device 2 includes reactor shell, central tube and synthesis casing, and the central tube and synthesis casing are arranged in reactor enclosure body,
The central tube and synthesis casing coaxial arrangement.The identical micropore 801 of multiple diameters is provided on the tube wall of central tube.Further include
Gas-liquid separator 11, compression set 12, purifying, preheating device 13, boiler water increasing pump 14 and purified synthesis gas slot 15；The gas-liquid
Separator 11 is connect with compression set 12, and compression set 12 is connect with purifying, preheating device 13, and purifying, preheating device 13 and synthesis gas are net
Change slot 15 to connect, the branch line between purifying, preheating device 13 and purified synthesis gas slot 15 is arranged in the boiler water increasing pump 14
On 16.Catalyst unit area 11 is provided between synthesis casing and central tube.Steam (vapor) outlet is provided at the top of reactor shell, institute
It states and is provided with first outlet and second outlet on the side wall of reactor shell.Two neighboring micropore 801 on the central tube tube wall
Between spacing be 15mm.200000 round micropores 801 are provided on the tube wall of central tube.Perforated area on central tube is
600000mm2。
Working principle of the utility model is:
(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 gas-liquid separator progress gas-liquid separation, the synthesis gas through gas-liquid separation enters the compression of compression set 12 and increases
It is depressed into 7.91MPaG, pressurized synthesis gas is then heated to 150 DEG C by synthesizer purifying, preheating device 13, passes through boiler
The water booster pump boiler water that spray flow is 2.08t/h into the synthesis gas after pressurization heating, to decompose the conjunction after pressurization heating
At micro organic sulfur remaining in gas, then the synthesis gas for removing organic sulfur is passed through in purified synthesis gas slot 15 again, is utilized
The Zinc oxide catalytic containing alumina loaded in purified synthesis gas slot 15 is micro in the synthesis gas for eliminate organic sulfur to remove
Inorganic sulfur, generate sulfur content be less than 50ppb virgin gas (virgin gas includes carbon monoxide, carbon dioxide and hydrogen).
Above-mentioned virgin gas is delivered to the first synthesis reactor 1 and/or the second synthesis reactor 2, it is anti-to carry out methanol-fueled CLC
It answers, and crude carbinol is isolated by the first separator 5 and/or the second separator 6, crude carbinol is then delivered to distillation system system
Take refined methanol.Isolate the unreacting gas of crude carbinol and water in the first separator 5 and/or the second separator 6, a part into
Enter and the first synthesis reactor 1 and/or the second synthesis reactor 2 be again introduced by oil separating device 4 after circulator compressor 3,
To recycle, another part is discharged as periodic off-gases.
Claims (5)
1. a kind of parallel methanol synthesis reaction system of double-reactor, which is characterized in that including the first synthesis reactor (1),
Two synthesis reactor (2), circulator compressor (3) and oil separating device (4), first synthesis reactor (1) with first point
It is connected from device (5), second synthesis reactor (2) connect with the second separator (6), first separator (5) and second
Separator (6) is connect with the air inlet of circulator compressor (3), and the circulator compressor (3) and oil separating device (4) are even
It connects, the oil separating device (4) connect with the first synthesis reactor (1) and the second synthesis reactor (2) respectively.
2. the parallel methanol synthesis reaction system of a kind of double-reactor according to claim 1, which is characterized in that described
One synthesis reactor (1) and the second synthesis reactor (2) include reactor shell, central tube and synthesis casing, the center
Pipe and synthesis casing are arranged in reactor enclosure body, the central tube and synthesis casing coaxial arrangement.
3. the parallel methanol synthesis reaction system of a kind of double-reactor according to claim 2, which is characterized in that further include
Gas-liquid separator (11), compression set (12), purifying, preheating device (13), boiler water increasing pump (14) and purified synthesis gas slot
(15)；The gas-liquid separator (11) connect with compression set (12), and compression set (12) is connect with purifying, preheating device (13), only
Change preheater (13) connect with purified synthesis gas slot (15), the boiler water increasing pump (14) be arranged in purifying, preheating device (13) and
On branch line (16) between purified synthesis gas slot (15).
4. the parallel methanol synthesis reaction system of a kind of double-reactor according to claim 3, which is characterized in that the conjunction
Catalyst unit area is provided between packaged tube and central tube.
5. the parallel methanol synthesis reaction system of a kind of double-reactor according to claim 4, which is characterized in that described anti-
It answers and is provided with steam (vapor) outlet at the top of device shell, be provided with first outlet and second outlet on the side wall of the reactor shell.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920261344.6U CN209702624U (en) | 2019-02-28 | 2019-02-28 | The parallel methanol synthesis reaction system of double-reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201920261344.6U CN209702624U (en) | 2019-02-28 | 2019-02-28 | The parallel methanol synthesis reaction system of double-reactor |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN209702624U true CN209702624U (en) | 2019-11-29 |
Family
ID=68642879
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201920261344.6U Active CN209702624U (en) | 2019-02-28 | 2019-02-28 | The parallel methanol synthesis reaction system of double-reactor |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN209702624U (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109678659A (en) * | 2019-02-28 | 2019-04-26 | 中煤陕西榆林能源化工有限公司 | The parallel methanol synthesis reaction system of double-reactor |
-
2019
- 2019-02-28 CN CN201920261344.6U patent/CN209702624U/en active Active
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN109678659A (en) * | 2019-02-28 | 2019-04-26 | 中煤陕西榆林能源化工有限公司 | The parallel methanol synthesis reaction system of double-reactor |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US10017438B2 (en) | Method and device system for producing dimethyl oxalate through carbonylation of industrial synthesis gas and producing ethylene glycol through dimethyl oxalate hydrogenation | |
| CN102775274B (en) | System and method for preparing ethylene glycol through oxalate hydrogenation | |
| CN104138713A (en) | Method, device and reactor for recovery of sulfur from acidic gas | |
| CN102502901B (en) | Condensed fluid stripping method matched with CO transforming device | |
| CN209702624U (en) | The parallel methanol synthesis reaction system of double-reactor | |
| CN103708426A (en) | Device for producing hydrogen peroxide by adopting anthraquinone process | |
| CN203612954U (en) | Hydrogenation section system for hydrogen peroxide production with anthraquinone process | |
| CN109678659A (en) | The parallel methanol synthesis reaction system of double-reactor | |
| CN105582859B (en) | The method of catalytic ammoniation legal system ethanol amine | |
| RU2252209C1 (en) | Method for methanol production (variants) | |
| CN104152198B (en) | Methanation reaction process | |
| CN203699908U (en) | Anthraquinone process hydrogen peroxide production device | |
| CN205295183U (en) | Energy -saving ultra -large methanol synthesis device of production different brackets steam | |
| CN102963944B (en) | Stripping tower for CO conversion condensate | |
| CN106278844A (en) | A kind of reduce the device and method of consumption of raw materials during propenecarbonyl | |
| CN107789969A (en) | The processing method and device of a kind of sour gas | |
| CN105925301A (en) | Technique for preparing gasoline from methyl alcohol through combined bed | |
| CN106397121A (en) | A biogas-coke oven gas combined methanol production device | |
| CN209696864U (en) | Synthesis reaction system with porous type central tube | |
| CN201537408U (en) | Purification treatment tower for producing hydrogen with natural gas | |
| CN204385096U (en) | A kind of propylene product protection bed regeneration purge device | |
| CN203269817U (en) | Improved production device for preparing isobutene from isobutane through dehydrogenation | |
| CN203568999U (en) | Reaction separation system and device for preparing polyoxymethylene dimethyl ethers | |
| CN103664497A (en) | Method for producing styrene employing catalytic dehydrogenation of ethylbenzene | |
| CN202621125U (en) | High-pressure reaction unit |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| GR01 | Patent grant | ||
| GR01 | Patent grant | ||
| TR01 | Transfer of patent right | ||
| TR01 | Transfer of patent right |
Effective date of registration: 20240117 Address after: 719000 east of B1 Road, North Yuma Avenue, high tech Industrial Park, Yulin City, Shaanxi Province Patentee after: Middling coal Shaanxi Energy and Chemical Group Co.,Ltd. Address before: 719000 Mazaliang China Coal Group, Yuheng Industrial Park, Yulin City, Shaanxi Province Patentee before: CHINA COAL SHAANXI YULIN ENERGY & CHEMICAL CO.,LTD. |