CN207641442U - Calandria type fixed bed reactor for strong exothermal reaction - Google Patents
Calandria type fixed bed reactor for strong exothermal reaction Download PDFInfo
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Abstract
A kind of calandria type fixed bed reactor for strong exothermal reaction, it includes reactor shell（5）, upper cover（2）, low head（8）, upper perforated plate（3）, lower perforated plate（7）, feed inlet（1）, discharge port（9）, cooling medium inlet（10）, cooling media outlet（4）, it is characterized in that being fixed on upper perforated plate（3）And lower perforated plate（7）Between several tubulations（6）, tubulation（6）Diameter from top to bottom gradually subtracts big or gradually decreasees from top to bottom, and axial in reactor shell along tubulation (6)（5）Several axial temperature-measuring ports of spaced set.The advantages of the utility model has the heat-transfer effect of tube side and shell side good, and the radial and axial temperature gradient of reactor is small, and bed utilization rate is high, and production capacity is largely increased.
Description
Technical field
The utility model is related to a kind of calandria type fixed bed reactors for strong exothermal reaction.
Background technology
Fixed bed reactors have a wide range of applications in chemical industry and petroleum industry.Preparing gasoline by methanol, methanol system
The reaction process such as propylene, steam reformation, methanol-fueled CLC, F- T synthesis usually carry out all in fixed bed reactors.These processes
All it is strongly exothermic process, controlling reaction temperature is the key that maintain higher reaction conversion ratio and selectivity, raw in reaction process
At heat needs removed from bed in time, thus reactor type selecting, design and monitoring it is most important to these processes.
Calandria type fixed bed reactor is by more reaction tube parallel connections, and loading catalyst is reacted in pipe, cooling to be situated between
Matter flows outside pipe to be carried out moving heat, and calandria type fixed bed reactor is relative to common fixed bed reactors heat transfer area bigger, more
The reaction process for adding suitable thermal discharge big.However, the big chemical reaction of some thermal discharges is under inappropriate process condition, still
Temperature control phenomenon is easy tod produce, consequence is often catastrophic.
When design and operation carry out strong exothermal reaction in shell-and-tube reactor, it is to need to examine to avoid temperature control phenomenon
One of critical issue of worry.The rate and efficiency of reactor will be severely limited, and reaction process condition, which must control, to be prevented
There is hot(test)-spot temperature, generate temperature control phenomenon, influence the activity of catalyst and in the range of the service life, especially in reactor cylinder
In the case of body is relatively large in diameter, reactor hot spot radial temperature difference can increase rapidly.Therefore new and effective heat exchanging pipe reactor is designed,
Bed hot spot is reduced, stable reaction warm area is widened, to improving production capacity, the reaction efficiency of calandria type fixed bed reactor, into
One step is energy saving, important in inhibiting of increasing economic efficiency.
Temperature control between calandria type fixed bed reactor tube bank depends on being evenly distributed for the heat carrier flowed between pipe
Degree, therefore how to ensure that full and uniform heat between pipe is transmitted, it solves cooling medium and is flowed between calandria type fixed bed reactor pipe
Heat transfer problem caused by unevenness is that calandria type fixed bed reactor needs the key technology solved.
Every reaction tube is used sleeve structure by patent CN 1736574A, and loading catalyst is formed and urged in shell clearance
Agent bed, cooling medium flow through inner tube tube side and reactor shell side simultaneously, increase the heat exchange area of calandria type fixed bed reaction,
Shorten heat-transfer path simultaneously so that reaction temperature axis is radially uniform.This method is true to increase heat transfer area by increasing tube bank
In fact can augmentation of heat transfer effect, but the difficulty in terms of processing can be brought, and largely effect on effective loadings of catalyst.
Patent US 3801634, JP53-30688B and JP (are adopted in catalyst bed inert particle segmentation dilute catalyst
With different dilution ratios), to control catalytic activity and reaction rate, eliminate hot spot.On the one hand this method increases catalyst
Bed height, reduces the production capacity of whole device, on the other hand causes entire catalyst bed in physical arrangement and chemical property
It is different so that there is apparent discontinuous and wild effect in mass-and heat-transfer.
Invention content
What the utility model aim was to provide a kind of uneven distribution that can overcome bed temperature is suitable for strong exothermal reaction
Calandria type fixed bed reactor.
The utility model is that the relationship of heat release and bed temperature based on chemical reaction is nonlinear, and is applied to move heat
The cooling law of process is linear, and the two combines so that nonlinear Distribution, tool is presented in the bed temperature in fixed bed reactors
Body shows as epimere in bed and is susceptible to " hot spot " temperature and polymorphic behavior.It is anti-by different sections according to exothermic reaction characteristics
It answers device loaded catalyst different, and keeps catalyst bed physical arrangement, the consistency of chemical property so that shell-and-tube reactor
In exothermic heat of reaction and bed temperature be in nonlinear Distribution, the final homogeneity for realizing bed temperature temperature.
The utility model is the calandria type fixed bed reactor for strong exothermal reaction, it includes reactor shell, upper envelope
Head, upper perforated plate, lower perforated plate, feed inlet, discharge port, cools down medium inlet, cooling media outlet, it is characterized in that solid at low head
Several tubulations being scheduled between upper perforated plate and lower perforated plate, tubulation diameter from top to bottom gradually subtract big or from top to bottom gradually subtract
It is small, and along axial several the axial temperature-measuring ports in reactor shell spaced set of reaction tube.
As described above, temperature-measuring port is 4-6.
As described above, tubulation diameter from top to bottom gradually increases, top end diameter：Bottom diameter=0.65-0.95：1.
As described above, reactor tubulation diameter gradually decreasees from top to bottom, top end diameter/bottom diameter=1.1-1.5：1.
As described above, reactor tubulation bottom diameter 28-48mm.
As described above, reactor tubulation length 3-12m.
As described above, reactor shell internal diameter is 1.5-4.8m.
As described above, lower perforated plate is equipped with 500-10000 root tubulations on reactor.
As described above, cooling medium can select one kind of air-cooled, oil cooling, water cooling etc..
Reactor as described above be applied to F- T synthesis, preparing gasoline by methanol, methanol propylene, steam reformation, methanol-fueled CLC,
The reactions such as benzene oxygen cis-butenedioic anhydride.
The utility model compared with prior art, has the following advantages：The heat-transfer effect of tube side and shell side is good, reactor diameter
To small with axial-temperature gradient, bed utilization rate is high, and production capacity is largely increased, strongly exothermic anti-especially suitable for F- T synthesis etc.
It answers.
Description of the drawings
Fig. 1 is the structural representation that tubulation diameter gradually decreasees from top to bottom in the utility model calandria type fixed bed reactor
Figure.
Fig. 2 is tubulation diameter gradually increased structural representation from top to bottom in the utility model calandria type fixed bed reactor
Figure.
As shown in the figure：1- feed inlets, 2- upper covers, 3- upper perforated plates, 4- coolings media outlet, 5- reactor shells, 6- are anti-
Answer tubulation, 7- lower perforated plates, 8- low heads, 9- discharge ports, 10- coolings medium inlet, 11- first axis thermometer hole, the second axis of 12-
To thermometer hole, 13- third axial directions thermometer hole, the axial thermometer holes of 14- the 4th, the axial thermometer holes of 15- the 5th.
Specific implementation mode
The utility model reactor is illustrated with reference to embodiment, but is not limited to the present embodiment.
Below by taking strong exothermal reaction Fischer-Tropsch synthesis as an example, the utility model reactor is illustrated.
Embodiment 1
The utility model is calandria type fixed bed reactor suitable for strong exothermal reaction, including reactor shell (5), on
End socket (2), upper perforated plate (3), lower perforated plate (7), feed inlet (1), discharge port (9), cools down medium inlet (10), is cold low head (8)
But media outlet (4) and it is fixed on the tubulation (6) of ordered arrangement between upper perforated plate (3), lower perforated plate (7)；Along reaction tube axis
To 5 axial temperature-measuring ports are arranged in reactor shell (5) successively from the top to the bottom, the spacing between temperature-measuring port is equal, axial
Temperature measuring point 1 is located in first axis temperature-measuring port 11, axial temperature measuring point 2 is located in the second axial temperature-measuring port 12, axial temperature measuring point 3
In third axial direction temperature-measuring port 13, axial temperature measuring point 4 is located in the 4th axial temperature-measuring port 14, axial temperature measuring point 5 is located at the 5th axis
Into temperature-measuring port 15.
5 internal diameter of the reactor shell is 3.4m, and upper lower perforated plate is equipped with 4800 tubulations, and 6 diameter of reactor tubulation is by upper
To lower gradual increase, top end diameter/bottom diameter=0.85：1,6 bottom diameter 38mm of reactor tubulation, reactor tubulation 6 are grown
Spend 12m.
Fischer-Tropsch synthesis, after activation of catalyst, fresh synthesis gas and circulating air are carried out using the utility model reactor
Enter in reactor 5 from feed inlet 1 after mixing, enters the tubulation 6 equipped with catalyst by upper perforated plate 3, it is anti-to carry out F- T synthesis
It answers；Cooling medium (water cooling) enters from cooling entrance 10, is discharged from coolant outlet 4；All reaction products, including circulatory mediator and
The complete gas of unreacted, is discharged via the discharge port 9 of reactor, and the synthesis that reaction generates is separated by oil gas water separator
Water, remaining product are cut by rectifying column rectifying and are detached, and respectively obtain light components, centre evaporates and heavy component, residue one
On-condensible gas is divided to be discharged out-of-bounds as periodic off-gases, another part on-condensible gas reenters reactor as circulating air.
The reactor filling Co based Fischer-Tropsch synthesis catalyst (being prepared according to the method for patent CN 102962066A), also
Old terms is 500 DEG C, 1.2MPa, 2500h-1(v/v), constant temperature 12h；Reaction condition is：220 DEG C, 2.4MPa, 1200h-1(v/
V), H2/ CO (mol)=1.7.The major temperature parameter and catalyst performance of reactor are shown in Table 1.
Embodiment 2
Reactor as described in Example 1 and reaction process flow, 5 internal diameter of reactor shell are 3.6m, up and down
Tube sheet is equipped with 4000 tubulations 6, and 6 diameter of reactor tubulation from top to bottom gradually increases, top end diameter/bottom diameter=0.75：
1,6 bottom diameter 44mm × 2mm of reactor tubulation, 6 length 9m of reactor tubulation.
The reactor filling Co based Fischer-Tropsch synthesis catalyst (being prepared according to the method for patent CN 102962077B), also
Old terms is：450 DEG C, 1.0MPa, 1000h-1(v/v), constant temperature 10h；Reaction condition is：210 DEG C, 2.5MPa, 1100h-1(v/
V), H2/ CO (mol)=1.8.The major temperature parameter and catalyst performance of reactor are shown in Table 1.
Embodiment 3
Reactor as described in Example 1 and reaction process flow, the reactor shell (5) internal diameter are 1.5m, on
Lower perforated plate is equipped with 500 tubulations, and 6 diameter of reactor tubulation from top to bottom gradually increases, top end diameter/bottom diameter=0.65：
1,6 bottom diameter 48mm × 2mm of reactor tubulation, 6 length 3m of reactor tubulation.
The reactor filling Co based Fischer-Tropsch synthesis catalyst (being prepared according to the method for patent CN 105032425A), also
Old terms is：350 DEG C, 0.1MPa, constant temperature 10h, 1500h-1(v/v), using hydrogen in nitrogen, H2Content is 15% (v/v).React item
Part is：230 DEG C, 3.0MPa, 2500h-1(v/v), H2/ CO (mol)=2.2.The major temperature parameter and catalyst performance of reactor
1 can be shown in Table.
Embodiment 4
Reactor as described in Example 1 and reaction process flow, 5 internal diameter of reactor shell are 4.0m, up and down
Tube sheet is equipped with 5000 tubulations, and 6 diameter of reactor tubulation gradually decreasees from top to bottom, top end diameter/bottom diameter=1.25：1,
6 bottom diameter 33.5mm × 2mm of reactor tubulation, 6 length 7.5m of reactor tubulation.
The reactor filling Co based Fischer-Tropsch synthesis catalyst (being prepared according to the method for patent CN 103977801A), also
Old terms：It 400 DEG C, 1.0Mpa, 5h, restores in hydrogen, volume space velocity 1500h-1；Reaction condition is：H2The molar ratio of/CO is
2, reaction temperature is 220 DEG C, pressure 2.0Mpa, volume space velocity 1000h-1.The major temperature parameter and catalyst of reactor
Performance is shown in Table 1.
Embodiment 5
Reactor as described in Example 1 and reaction process flow, 5 internal diameter of reactor shell are 2.4m, up and down
Tube sheet is equipped with 2000 tubulations, and 6 diameter of reactor tubulation from top to bottom gradually increases, top end diameter/bottom diameter=0.75：1.
6 bottom diameter 40mm × 2mm of reactor tubulation.6 length 6m of reactor tubulation.
The reactor filling Co based Fischer-Tropsch synthesis catalyst (being prepared according to the method for patent CN 104841434B), also
Old terms is：400 DEG C, 1.0MPa, GHSV=1500h-1, constant temperature 8h, using hydrogen reduction gas, H in nitrogen2Content is 5% (v/v)；
Reaction condition is：235 DEG C, 2.0Mpa, GHSV=2500h-1, H2/ CO (v/v)=1.8.It the major temperature parameter of reactor and urges
Agent performance is shown in Table 1.
Table 1
Claims (8)
1. a kind of calandria type fixed bed reactor for strong exothermal reaction, it includes reactor shell（5）, upper cover（2）, under
End socket（8）, upper perforated plate（3）, lower perforated plate（7）, feed inlet（1）, discharge port（9）, cooling medium inlet（10）, cooling media outlet
（4）, it is characterized in that being fixed on upper perforated plate（3）And lower perforated plate（7）Between several tubulations（6）, tubulation（6）Diameter by up to
Gradually subtract down big or gradually decrease from top to bottom, and is axial in reactor shell along tubulation (6)（5）Several axis of spaced set
To temperature-measuring port.
2. a kind of calandria type fixed bed reactor for strong exothermal reaction as described in claim 1, it is characterised in that described
Temperature-measuring port is 4-6.
3. a kind of calandria type fixed bed reactor for strong exothermal reaction as described in claim 1, it is characterised in that described
Tubulation (6) diameter from top to bottom gradually increases, top end diameter：Bottom diameter=0.65-0.95：1.
4. a kind of calandria type fixed bed reactor for strong exothermal reaction as described in claim 1, it is characterised in that described
Tubulation (6) diameter gradually decreasees from top to bottom, top end diameter/bottom diameter=1.1-1.5：1.
5. a kind of calandria type fixed bed reactor for strong exothermal reaction as described in claim 1, it is characterised in that described
Tubulation (6) bottom diameter 28-48mm.
6. a kind of calandria type fixed bed reactor for strong exothermal reaction as described in claim 1, it is characterised in that described
Tubulation (6) length 3-12m.
7. a kind of calandria type fixed bed reactor for strong exothermal reaction as described in claim 1, it is characterised in that described
Reactor shell（5）Internal diameter is 1.5-4.8m.
8. a kind of calandria type fixed bed reactor for strong exothermal reaction as described in claim 1, it is characterised in that described
Tubulation (6) is 500-10000 roots.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201721694673.7U CN207641442U (en) | 2017-12-08 | 2017-12-08 | Calandria type fixed bed reactor for strong exothermal reaction |
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| CN201721694673.7U CN207641442U (en) | 2017-12-08 | 2017-12-08 | Calandria type fixed bed reactor for strong exothermal reaction |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108970550A (en) * | 2018-09-25 | 2018-12-11 | 鲁盈 | Methanol derivatives bed gradient orients temperature control reaction unit and its reaction method |
| CN114425278A (en) * | 2020-10-15 | 2022-05-03 | 中国石油化工股份有限公司 | Device and method for producing low-carbon olefin and application |
-
2017
- 2017-12-08 CN CN201721694673.7U patent/CN207641442U/en active Active
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN108970550A (en) * | 2018-09-25 | 2018-12-11 | 鲁盈 | Methanol derivatives bed gradient orients temperature control reaction unit and its reaction method |
| CN108970550B (en) * | 2018-09-25 | 2023-12-01 | 鲁盈 | Gradient directional temperature control reaction device and reaction method for methanol deep processing bed |
| CN114425278A (en) * | 2020-10-15 | 2022-05-03 | 中国石油化工股份有限公司 | Device and method for producing low-carbon olefin and application |
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