CN109999732A - A kind of heat-transfering device of F-T synthesis paste state bed reactor - Google Patents
A kind of heat-transfering device of F-T synthesis paste state bed reactor Download PDFInfo
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- CN109999732A CN109999732A CN201810012901.0A CN201810012901A CN109999732A CN 109999732 A CN109999732 A CN 109999732A CN 201810012901 A CN201810012901 A CN 201810012901A CN 109999732 A CN109999732 A CN 109999732A
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- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 58
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 56
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 70
- 230000009467 reduction Effects 0.000 claims abstract description 49
- 238000006243 chemical reaction Methods 0.000 description 18
- 230000003020 moisturizing effect Effects 0.000 description 12
- 239000007788 liquid Substances 0.000 description 8
- 239000003054 catalyst Substances 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 238000006392 deoxygenation reaction Methods 0.000 description 5
- 238000000034 method Methods 0.000 description 4
- 230000008901 benefit Effects 0.000 description 3
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 229910052760 oxygen Inorganic materials 0.000 description 2
- 239000001301 oxygen Substances 0.000 description 2
- 230000008569 process Effects 0.000 description 2
- 238000005245 sintering Methods 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 230000009466 transformation Effects 0.000 description 2
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 1
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 235000006508 Nelumbo nucifera Nutrition 0.000 description 1
- 240000002853 Nelumbo nucifera Species 0.000 description 1
- 235000006510 Nelumbo pentapetala Nutrition 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- 150000001336 alkenes Chemical class 0.000 description 1
- 150000004945 aromatic hydrocarbons Chemical class 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000006227 byproduct Substances 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
- 230000007423 decrease Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000010612 desalination reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 230000005611 electricity Effects 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000002779 inactivation Effects 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 239000012188 paraffin wax Substances 0.000 description 1
- 239000000047 product Substances 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003746 solid phase reaction Methods 0.000 description 1
- 238000006467 substitution reaction Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
- 238000009834 vaporization Methods 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000001993 wax Substances 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/1836—Heating and cooling the reactor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
- B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
- B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
- B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
- C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
- C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
- C10G2/34—Apparatus, reactors
- C10G2/342—Apparatus, reactors with moving solid catalysts
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00008—Controlling the process
- B01J2208/00017—Controlling the temperature
- B01J2208/00106—Controlling the temperature by indirect heat exchange
- B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
- B01J2208/00132—Tubes
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Combustion & Propulsion (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
A kind of heat-transfering device of F-T synthesis paste state bed reactor, it include: the upper section drum and lower section drum being connect with synthesis reactor, the reduction drum being connect with reduction reactor, wherein the upper section drum and the lower section drum pass through pipeline respectively and are connected with synthesis small pump, recirculated water in the upper section drum and the lower section drum passes through upper section drum water circulating pump respectively and lower section drum water circulating pump is pumped into the heat exchanging pipe in the synthesis reactor, the reduction drum is connected by pipeline with reduction small pump, recirculated water in the reduction drum is pumped into the heat exchanging pipe in the reduction reactor by restoring drum water circulating pump, the outlet conduit of the reduction small pump is connected with the outlet conduit of the synthesis small pump by connecting pipe, valve is provided on the connecting pipe.Heat-transfering device of the invention solves the problems, such as synthesis turbine-driven boiler feed pump without effectively standby pump, when certain boiler feedwater failure of pump, when needing to overhaul, is not required to load down.
Description
Technical field
The present invention relates to chemical industry synthesis fields, and in particular to a kind of heat-transfering device of F-T synthesis paste state bed reactor.
Background technique
F-T synthetic reaction is strong exothermal reaction, and reaction heat is removed mainly by the vaporization of circulation deaerated water, so guaranteeing to remove
The abundance and normal circulation of oxygen water are that heat is smoothly moved out premise.The deaerated water of synthesis drum is that the deaerated water in oxygen-eliminating device is logical
Crossing in boiler presses feed pump to provide by boosting.If boiler water pump designed capacity deficiency certainly will will affect the confession of deaerated water
It answers, leads to the dry pot of drum, reactor heat cannot be removed in time, and reactor batch temperature goes up, and cause reactor temperature runaway, it will
Catalyst micropore carbon distribution is caused to inactivate, sintering of catalyst inactivation or even Fischer-Tropsch reaction Fe-series catalyst can form bulk when serious
And it can not take out to cause completely to stop and re-replace catalyst.
In addition, deaerated water is insufficient, reactor overtemperature may cause heat exchanging pipe built in paste state bed reactor and deform,
It even damages, is equivalent to reactor and scraps without can be carried out Chemical Manufacture；May cause screen pipe built in paste state bed reactor by
To high temperature influence and damage, if filtering pipe network burns out liquid wax and cannot extract out in time, the operation of less serious case's device load down, severe one without
Method, which comes into operation, directly results in parking replacement.And screen pipe production cost is big, fabrication cycle and replacing construction are all long, gives company's band
Carry out serious financial consequences.
In short, the deaerated water that F-T reactor moves heat is insufficient, synthesis system will face halt production or F-T reaction system
System can only be run at low load, cannot achieve at full capacity or heavy-duty service.
Currently, the F-T synthesis reactor system run, the problem that deaerated water insufficient supply causes temperature of reactor high are equal
It is that unstripped gas air inflow is reduced by load down to solve.F-T synthesis reactor system includes two F-T reactors, respectively there is one
Drum heat-tranferring system is covered, is supplied water by two Medium pressure boiler feeding water pumps to synthesis drum, is removed for reactor reaction heat.
The temperature of synthesis reactor is recycled by the water of upper-lower section water circulating pump and removes reaction heat, and reaction heat becomes water
Steam, the synthesis boiler replenishing water pump when liquid level of steam drum is low through oxygen-eliminating device carry out moisturizing, and the temperature of reduction reactor passes through also
The water circulation of former water circulating pump removes reaction heat, and water is become steam by reaction heat, passes through oxygen-eliminating device when liquid level of steam drum is low
It restores boiler replenishing water pump and carries out moisturizing.The moisturizing that two reactors move hot vapour packet is that individual small pump carries out moisturizing.
Since Medium pressure boiler feeding water pump is without standby pump, it is insufficient that there is deaerated water when high load capacity, may cause reactor
Temperature runaway and cannot achieve synthesis reaction system high load capacity (excess load) operation the drawbacks of；There is no stand-by pump, once operation pump occurs
Failure, liquid level of steam drum decline, can not moisturizing carry out move heat, synthesis system by load down production even parking process.
Although can realize standby pump by transformation turbine-driven boiler feed pump, transformation difficulty is big, investment is big, while steam-operating
Coming into operation for boiler feed pump is also uncertain.Boiler feed pump is driven in addition it can increasing new electricity to realize, but is existed
The disadvantages such as system is huge, and design cycle, procurement cycle, construction period are long, and investment is big.
Summary of the invention
In order to solve boiler feed pump without standby pump, deaerated water supply is insufficient after boiler feed pump jumps vehicle, and heat of reaction is moved
It does not go out, heat is assembled in reactor, the problem of causing reactor temperature runaway, and the invention proposes a kind of F-T to synthesize slurry bed system
The heat-transfering device of reactor.
The heat-transfering device of F-T synthesis paste state bed reactor proposed by the present invention includes: the upper section connecting with synthesis reactor
Drum and lower section drum, the reduction drum being connect with reduction reactor,
Wherein the upper section drum and the lower section drum pass through pipeline respectively and are connected with synthesis small pump, the upper section vapour
Recirculated water in packet and the lower section drum passes through upper section drum water circulating pump respectively and lower section drum water circulating pump be pumped into it is described
Heat exchanging pipe in synthesis reactor, the steam that the synthesis reactor top generates enter the upper section drum by pipeline,
The steam that the synthesis reactor lower part generates enters the lower section drum by pipeline,
The reduction drum is connected by pipeline with reduction small pump, and the recirculated water in the reduction drum passes through reduction vapour
Packet loop water pump is pumped into the heat exchanging pipe in the reduction reactor, the steam generated in the reduction reactor by pipeline into
Enter the reduction drum,
The outlet conduit of the reduction small pump is connected with the outlet conduit of the synthesis small pump by connecting pipe, institute
It states and is provided with valve on connecting pipe.
Preferably, the synthesis small pump is used to deaerated water being pumped into the upper section drum and the lower section drum.
Preferably, the reduction small pump is used to deaerated water being pumped into the reduction drum.
Preferably, the steam in the upper section drum and the lower section drum is discharged into the first steam pipe network.
Preferably, the steam in the reduction drum is discharged into the second steam pipe network.
Preferably, the synthesis small pump and the reduction small pump are connected with oxygen-eliminating device, the oxygen-eliminating device and desalination
Pipe network is connected with third steam pipe network.
Preferably, valve is respectively arranged between the upper section drum and the lower section drum and the synthesis small pump.
Compared with prior art, heat-transfering device of the invention will restore small pump as the standby pump of synthesis small pump, make anti-
Answer in device heat production and move thermal balance, keep reactor temperature constant and controllable, prevent inside reactor heat exchanging pipe damage and
The safety accidents such as internal accelerator overtemperature sintering solve the problems, such as synthesis turbine-driven boiler feed pump without effectively standby pump, when certain
Boiler feedwater failure of pump, when needing to overhaul, device is not required to load down.
Detailed description of the invention
Fig. 1 is the schematic diagram for the heat-transfering device that F-T of the present invention synthesizes paste state bed reactor.
Description of symbols:
1- synthesis reactor；2- upper section drum；3- lower section drum；4- reduction reactor；5- restores drum；6- synthesizes moisturizing
Pump；7- upper section drum water circulating pump；8- lower section drum water circulating pump；9- restores small pump；10- restores drum water circulating pump；11-
Oxygen-eliminating device.
Specific embodiment
To make the objectives, technical solutions, and advantages of the present invention clearer, below in conjunction with specific embodiment, and reference
Attached drawing, the present invention is described in further detail.
F-T synthesis is with a certain proportion of H2It is raw material with CO, under the action of catalyst, generates linear paraffin, alkene, lacks
Measure the reaction of the liquid hydrocarbon products such as aromatic hydrocarbons and byproduct water and carbon dioxide.Paste state bed reactor is that gas is passed through in the form of being bubbled
It is suspended with the slurry layer of solid fine grain, to realize the reactor of gas-liquid solid phase reaction process.
The heat-transfering device of F-T synthesis paste state bed reactor of the invention includes: the upper section drum connecting with synthesis reactor 1
2 and lower section drum 3, the reduction drum 5 that connect with reduction reactor 4, wherein upper section drum 2 and lower section drum 3 pass through pipe respectively
Road is connected with synthesis small pump 6, and synthesis small pump 6 is used to deaerated water being pumped into upper section drum 2 and lower section drum 3, upper section drum 2
Pass through upper section drum water circulating pump 7 respectively with the recirculated water in lower section drum 3 and lower section drum water circulating pump 8 is pumped into synthetic reaction
Heat exchanging pipe in device 1, the steam that 1 top of synthesis reactor generates enter upper section drum 2 by pipeline, under synthesis reactor 1
The steam that portion generates enters lower section drum 3 by pipeline, and reduction drum 5 is connected by pipeline with reduction small pump 9, restores moisturizing
Pump 9 restores the recirculated water in drum 5 and is pumped into also by restoring drum water circulating pump 10 for deaerated water to be pumped into reduction drum 5
Heat exchanging pipe in former reactor 4, the steam generated in reduction reactor 4 enter reduction drum 5 by pipeline, restore small pump
9 outlet conduit is connected with the outlet conduit of synthesis small pump 6 by connecting pipe, and valve is provided on connecting pipe.
Steam in upper section drum 2 and lower section drum 3 is discharged into steam pipe network from top, and the pressure of steam pipe network can be
2.8MPa.Steam in reduction drum 5 is discharged into another steam pipe network from top, and the pressure of steam pipe network can be 1.0MPa.
Synthesis small pump 6 and reduction small pump 9 are connected with oxygen-eliminating device 11, oxygen-eliminating device 11 and desalted water pipe network and steam pipe
Net is connected, and the pressure of steam pipe network can be 0.5MPa, and desalted water pipe network is 11 moisturizing of oxygen-eliminating device, and steam pipe network is used for deoxygenation
Device 11 carries out heating deoxygenation.
Valve is respectively arranged between upper section drum 2 and lower section drum 3 and synthesis small pump 6.
The temperature of synthesis reactor 1 is recycled by the water of upper-lower section water circulating pump and removes reaction heat, and reaction heat becomes water
At steam, when liquid level of steam drum reduces, moisturizing is carried out by the synthesis boiler replenishing water pump of oxygen-eliminating device, the temperature of reduction reactor is logical
The water circulation for crossing reduction water circulating pump removes reaction heat, and water is become steam by reaction heat, when liquid level of steam drum reduces, by removing
The reduction boiler replenishing water pump of oxygen device carries out moisturizing.It is that individual small pump is mended that two reactors, which move the moisturizing of hot vapour packet,
Water.Connecting pipe can be opened when synthesizing small pump 6 and breaking down, moisturizing is carried out by reduction small pump 9, it thus can be with
The normal operation for guaranteeing synthesis reactor 1, reaches maximization of economic benefit.
The present invention will be used for F-T catalyst reduction system and provide the deoxygenation pump outlet tube line of deaerated water to synthetic reaction system
The Medium pressure boiler feeding water pump outlet line that system supplies water increases a cross-line, can be by going back original system boiler feed pump to synthesis vapour
Packet supplies water and (it is larger to go back original system boiler feed pump design margin, two to open one standby, and goes back original system intermittently operated), it is ensured that synthesis
Reaction system deoxygenation water consumption is sufficient, solves the problems, such as that synthesis system deoxygenation water consumption is insufficient with this, realizes that synthesis system is completely negative
Lotus and overload operation increase economic benefit for enterprise.
Particular embodiments described above has carried out further in detail the purpose of the present invention, technical scheme and beneficial effects
Describe in detail bright, it should be understood that the above is only a specific embodiment of the present invention, is not intended to restrict the invention, it is all
Within the spirit and principles in the present invention, any modification, equivalent substitution, improvement and etc. done should be included in protection of the invention
Within the scope of.
Claims (7)
1. a kind of heat-transfering device of F-T synthesis paste state bed reactor, comprising: the upper section drum and lower section being connect with synthesis reactor
Drum, the reduction drum being connect with reduction reactor,
Wherein the upper section drum and the lower section drum pass through respectively pipeline with synthesis small pump be connected, the upper section drum with
Recirculated water in the lower section drum passes through upper section drum water circulating pump respectively and lower section drum water circulating pump is pumped into the synthesis
Heat exchanging pipe in reactor, the steam that the synthesis reactor top generates enters the upper section drum by pipeline, described
The steam that synthesis reactor lower part generates enters the lower section drum by pipeline,
The reduction drum is connected by pipeline with reduction small pump, and the recirculated water in the reduction drum is followed by restoring drum
Ring water pump is pumped into the heat exchanging pipe in the reduction reactor, and the steam generated in the reduction reactor enters institute by pipeline
Reduction drum is stated,
The outlet conduit of the reduction small pump is connected with the outlet conduit of the synthesis small pump by connecting pipe, the company
Valve is provided on threading a pipe.
2. heat-transfering device as described in claim 1, which is characterized in that the synthesis small pump is used to for deaerated water being pumped into described
Upper section drum and the lower section drum.
3. heat-transfering device as described in claim 1, which is characterized in that the reduction small pump is used to for deaerated water being pumped into described
Restore drum.
4. heat-transfering device as described in claim 1, which is characterized in that the steam in the upper section drum and the lower section drum
It is discharged into the first steam pipe network.
5. heat-transfering device as described in claim 1, which is characterized in that the steam in the reduction drum is discharged into the second steam pipe
Net.
6. heat-transfering device as described in claim 1, which is characterized in that the synthesis small pump and the reduction small pump with
Oxygen-eliminating device is connected, and the oxygen-eliminating device is connected with desalted water pipe network and third steam pipe network.
7. heat-transfering device as described in claim 1, which is characterized in that the upper section drum and the lower section drum and the conjunction
At being respectively arranged with valve between small pump.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810012901.0A CN109999732B (en) | 2018-01-05 | 2018-01-05 | Heat transfer device of F-T synthesis slurry bed reactor |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201810012901.0A CN109999732B (en) | 2018-01-05 | 2018-01-05 | Heat transfer device of F-T synthesis slurry bed reactor |
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| Publication Number | Publication Date |
|---|---|
| CN109999732A true CN109999732A (en) | 2019-07-12 |
| CN109999732B CN109999732B (en) | 2024-04-23 |
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ID=67164696
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810012901.0A Active CN109999732B (en) | 2018-01-05 | 2018-01-05 | Heat transfer device of F-T synthesis slurry bed reactor |
Country Status (1)
| Country | Link |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110591763A (en) * | 2019-09-10 | 2019-12-20 | 南京延长反应技术研究院有限公司 | Intelligent enhanced control system and process for coal indirect liquefaction |
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|---|---|---|---|---|
| CN101480592A (en) * | 2008-01-12 | 2009-07-15 | 杭州林达化工技术工程有限公司 | Fixed bed composite reaction equipment |
| US20130116348A1 (en) * | 2010-07-09 | 2013-05-09 | Shenhua Group Corporation Limited | Fischer-tropsch synthesis process and system |
| CN202995359U (en) * | 2012-11-09 | 2013-06-12 | 内蒙古伊泰煤制油有限责任公司 | Slurry bed reactor parking interlocking system |
| CN103386280A (en) * | 2012-05-08 | 2013-11-13 | 中国石油化工集团公司 | Naturally circulated heat removal method and system for slurry-bed reactor of Fische-Tropsch synthesis |
| CN203591777U (en) * | 2013-11-21 | 2014-05-14 | 内蒙古伊泰煤制油有限责任公司 | Rapid cooling system for heat exchanging tube nest in Fischer-Tropsch synthesis reactor |
| CN208098032U (en) * | 2018-01-05 | 2018-11-16 | 内蒙古伊泰煤基新材料研究院有限公司 | A kind of heat-transfering device of F-T synthesis paste state bed reactor |
-
2018
- 2018-01-05 CN CN201810012901.0A patent/CN109999732B/en active Active
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101480592A (en) * | 2008-01-12 | 2009-07-15 | 杭州林达化工技术工程有限公司 | Fixed bed composite reaction equipment |
| US20130116348A1 (en) * | 2010-07-09 | 2013-05-09 | Shenhua Group Corporation Limited | Fischer-tropsch synthesis process and system |
| CN103386280A (en) * | 2012-05-08 | 2013-11-13 | 中国石油化工集团公司 | Naturally circulated heat removal method and system for slurry-bed reactor of Fische-Tropsch synthesis |
| CN202995359U (en) * | 2012-11-09 | 2013-06-12 | 内蒙古伊泰煤制油有限责任公司 | Slurry bed reactor parking interlocking system |
| CN203591777U (en) * | 2013-11-21 | 2014-05-14 | 内蒙古伊泰煤制油有限责任公司 | Rapid cooling system for heat exchanging tube nest in Fischer-Tropsch synthesis reactor |
| CN208098032U (en) * | 2018-01-05 | 2018-11-16 | 内蒙古伊泰煤基新材料研究院有限公司 | A kind of heat-transfering device of F-T synthesis paste state bed reactor |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN110591763A (en) * | 2019-09-10 | 2019-12-20 | 南京延长反应技术研究院有限公司 | Intelligent enhanced control system and process for coal indirect liquefaction |
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| CN109999732B (en) | 2024-04-23 |
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