CN206519141U - Shell and tube paste state bed reactor and reaction system - Google Patents
Shell and tube paste state bed reactor and reaction system Download PDFInfo
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- CN206519141U CN206519141U CN201720062686.6U CN201720062686U CN206519141U CN 206519141 U CN206519141 U CN 206519141U CN 201720062686 U CN201720062686 U CN 201720062686U CN 206519141 U CN206519141 U CN 206519141U
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- shell
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Abstract
The utility model is related to a kind of shell and tube paste state bed reactor and reaction system.The shell and tube paste state bed reactor, the reactor of ethene is prepared for high concentration acetylene, it includes tactic air inlet section, tubulation distribution section and expanding reach, also include epimere and the area of hypomere tubulation UNICOM for connecting the tubulation distribution section, wherein, gas access is provided with the air inlet section, for reacting gas to be passed through into shell and tube paste state bed reactor；Tubulation distribution section is provided with multiple tubulations, reacted for reacting gas in tubulation distribution section to prepare ethene, multiple tubulations are provided with area of epimere tubulation UNICOM and area of hypomere tubulation UNICOM, the filter that is provided at both ends with area of epimere tubulation UNICOM, and gas vent is provided with the top of expanding reach.The design in area of tubulation UNICOM in shell and tube paste state bed reactor described in the utility model, ensure that the liquid level in each tubulation is homogeneous, it is to avoid gas short circuit, the setting of wherein epimere UNICOM area's filter can ensure the replacing and regeneration of solvent.
Description
Technical field
The utility model is related to chemical field, and ethene field is prepared especially with high concentration acetylene, and in particular to a kind of
The reaction system of shell and tube paste state bed reactor and the application paste state bed reactor.
Background technology
Ethene is a kind of important basic material in modern industry, is also one of maximum chemicals of world wide production, it is produced
Product are widely used in the fields such as national economy, people's lives, national defence, are " mothers of organic synthesis ".In face of the shortage of petroleum resources
Soaring with international oil price, raw material sources turn into the bottleneck of development ethylene industry, are also asking of must being solved in face of people of pendulum
Topic.Therefore, research and develop a kind of new source and process prepares ethene and substitutes the new technology of preparing that oil is raw material, energy
Enough dependences alleviated to oil.
In coal chemical technology, pass through Non-catalytic partial oxygen by calcium carbide technique or by raw material of natural gas by raw material of coal
Chemical industry skill produces acetylene, it has also become maturation process.Using acetylene as raw material, in the presence of selective hydrocatalyst, by adding
Hydrogen process obtains ethylene product, can further expand Coal Chemical Industry Route.Therefore, the new technology and skill of producing ethylene with acetylene hydrogenation are developed
Art, has broad application prospects.
Low concentration acetylene gas and solid phase catalyzing hydrogen addition technology is highly developed in the oil industry, is mainly used in removing in ethene
Acetylene impurities, the reactor used is fixed bed reactors, and solid-phase catalyst is loaded in the reactor and carries out gas-solid phase reaction.But
Because ethyne reactive is high, hydrogenation reaction thermal discharge is big, even there is a small amount of acetylene in cracking gas, traditional gas is solid phase fixed bed
There are still green oil generating amount is big, catalyst cycle period is short, reactor easily serious problems such as " temperature runaway " for hydrogenation reactor.
The appearance of traditional paste state bed reactor solves above mentioned problem to a certain extent, because its is simple in construction, it is easy to
Heat is moved, the ethylene product of generation is widely used, therefore, carrying out high concentration selective hydrogenation of acetylene using paste state bed reactor turns into
One important alkene production line processed.But traditional paste state bed reactor is when acetylene prepares ethene, gas-liquid-solid three-phase is mixed
Close uneven, reaction raw materials time of contact is short, and bed temperature is uniform in reactor, and temperature is difficult to control.
Utility model content
To overcome above mentioned problem, the utility model provides a kind of shell and tube paste state bed reactor and reaction system so that
Inside reactor temperature is uniform, increases the impurity component in reaction raw materials time of contact, reduction reaction product, is conveniently replaceable molten
Agent, improves production efficiency.System described in the utility model has green oil removal unit, greatly reduces green oil to catalyst
The influence of activity realizes the smooth long term running of device.
Shell and tube paste state bed reactor described in the utility model, the reactor of ethene is prepared for high concentration acetylene.Institute
Stating shell and tube paste state bed reactor includes tactic air inlet section, tubulation distribution section and expanding reach, in addition to connects the row
The epimere of pipe distribution section and area of hypomere tubulation UNICOM, wherein,
The bottom of the air inlet section is provided with gas access, for reacting gas to be passed through into the shell and tube slurry reactor
Device；
The tubulation distribution section is provided with multiple tubulations, occurs for the reacting gas in tubulation distribution section anti-
Should, prepare upper position in the middle part of ethene, the multiple tubulation and be provided with area of epimere tubulation UNICOM, area of the epimere tubulation UNICOM
It is provided at both ends with filter；The multiple tubulation bottom is provided with area of hypomere tubulation UNICOM, the one of area of the hypomere tubulation UNICOM
End is provided with discharge port；
Gas vent is provided with the top of the expanding reach.
Further, the region between the multiple tubulations and tubulation of the shell and tube paste state bed reactor constitutes shell side, institute
State and heat transferring medium is provided with shell side.
Further, the lower side of the tubulation distribution section is provided with heat transferring medium entrance, and upper side, which is provided with, changes
Thermal medium outlet, for heat transferring medium to be entered into the shell side from the heat transferring medium entrance, then is exported from the heat transferring medium
Discharge.
Further, the multiple tubulation bottom is provided with gas distributor, and stomata is distributed with thereon.
Further, the lower side of the expanding reach is provided with colvent inlet, and area of hypomere tubulation UNICOM side is set
Discharge port is equipped with, for solvent to be entered into the multiple tubulation from the colvent inlet, then is discharged from the discharge port.
Specifically, the upper end of the expanding reach is provided with metal demister.
Reaction system described in the utility model, for preparing ethene using acetylene.The reaction system includes above-mentioned
Shell and tube paste state bed reactor, condenser, gas-liquid separator, catalyst preparation tank and green oil removal unit, wherein,
The shell and tube paste state bed reactor has gas access, gas vent, colvent inlet, discharge port, heat transferring medium
Entrance, heat transferring medium outlet and
It is arranged at the filter at area of epimere tubulation UNICOM two ends；
The condenser has high-temperature product gas entrance and mixed gas outlet, the high-temperature product gas entrance and the tubulation
The gas vent of formula paste state bed reactor is connected；
The gas-liquid separator has gaseous mixture entrance, ethene outlet and solvent export mouth, the gaseous mixture entrance and institute
The mixed gas outlet for stating condenser is connected；
The catalyst preparation tank is connected with the colvent inlet of the shell and tube paste state bed reactor；
The green oil removal unit is connected with the filter of the shell and tube paste state bed reactor, for receiving the filtering
The solvent of device filtering.
Further, the green oil removal unit includes solvent tank and solvent reclamation device, wherein, the solvent tank
Exported with green oil entrance and green oil, the green oil entrance is connected with the filter of the shell and tube paste state bed reactor；
There is the solvent reclamation device de-oiling entrance to be exported with de-oiling, and the de-oiling entrance is green with the solvent tank
Oil export is connected, and the de-oiling outlet is connected with the colvent inlet of the shell and tube paste state bed reactor.
Further, the system also includes thermal medium storage tank and pump, wherein,
One end of the thermal medium storage tank and the heat transferring medium outlet of the shell and tube paste state bed reactor；
One end of the pump is connected with the other end of the thermal medium storage tank, and the other end of the pump is starched with the shell and tube
The heat transferring medium entrance connection of state bed reactor.
Further, the system also includes temperature conditioning unit, and it is arranged on the shell and tube paste state bed reactor and institute
State between pump, for controlling the heat exchange medium temperature into the shell and tube paste state bed reactor, the temperature conditioning unit is included simultaneously
The heater set, cooler and heat transferring medium is arranged to bypass.
The beneficial effects of the utility model：
The design in area of tubulation UNICOM, ensure that each tubulation in shell and tube paste state bed reactor described in the utility model
In liquid level it is homogeneous, it is to avoid gas short circuit, the equipment of filter therein can reduce the impurity component in reaction product.In addition,
Each tubulation is a small slurry bed system in shell and tube paste state bed reactor, because the diameter of each tubulation is smaller, high
Degree is of a relatively high, and it is more uniform that gas-liquid-solid three-phase can be mixed, and adds time of contact, improves gas-liquid flow field distribution, drop
Low enlarge-effect so that it is more abundant that reaction can be carried out.
In addition, system described in the utility model, with green oil removal unit, greatly reduces green oil and catalyst is lived
The influence of property realizes the smooth long term running of device.System described in the utility model can be realized to system solvent temperature
Accurate control, keeps the temperature of solvent to stablize relatively, so as to ensure that the even running of whole system；Furthermore, it is molten using liquid phase
The sensible heat of agent, heat-sinking capability is significantly improved, and can be quickly moved out the heat that selective hydrogenation of acetylene generation ethene is produced, reduction reaction
The temperature of bed, improves the conversion ratio of acetylene and the selectivity of ethene.
It is anti-that system described in the utility model solves the fixed bed in preparing ethylene by selective hydrogenation of acetylene reaction well
Answer that green oil generating amount in device is big, catalyst cycle period is short, reactor easily " temperature runaway " the problem of, due to catalyst in fluid bed
Mutual sharp impacts between particle, cause the difficulty of loss, the dedusting of catalyst and due to the corrasion of solid particle, exchange heat structure
The problem of serious wear of part and reactor.
Brief description of the drawings
Fig. 1 is the structural representation of shell and tube paste state bed reactor described in the utility model.
Fig. 2 is the structural representation of reaction system described in the utility model.
Embodiment
Below in conjunction with drawings and examples, embodiment of the present utility model is described in more details, with
Just it better understood when the advantage of scheme of the present utility model and its various aspects.However, specific implementations described below side
Formula and embodiment are only the purposes of explanation, rather than to limitation of the present utility model.
As shown in figure 1, shell and tube paste state bed reactor 1 described in the utility model, ethene is prepared for high concentration acetylene
Reactor.The shell and tube paste state bed reactor 1, by air inlet section, tubulation distribution section and expanding reach, is gone back including tactic
Epimere and area of hypomere tubulation UNICOM 111,108 including connecting the tubulation distribution section.
As shown in figure 1, the air inlet section is arranged in the bottom of the shell and tube paste state bed reactor 1, the air inlet section
Gas access 101 is provided with, for reacting gas to be passed through into the shell and tube paste state bed reactor 1.
As shown in figure 1, the tubulation distribution section is arranged on the top of the air inlet section, the tubulation distribution section is provided with many
Individual tubulation 106, reacts in tubulation distribution section for the reacting gas, prepares ethene, the multiple tubulation 106
Middle part is provided with area of epimere tubulation UNICOM 111, and area of the epimere tubulation UNICOM 111 is provided at both ends with filter；Multiple tubulations
106 bottoms are provided with area of hypomere tubulation UNICOM 108, and the one end in area of the hypomere tubulation UNICOM 108 is discharge port.Generally in epimere
Area of tubulation UNICOM is provided at both ends with two accurate filters, and main purpose is for filtering out solvent, in not parking situation
Under, change and regenerative response solvent.
Wherein, alternatively, a diameter of 30~100mm of tubulation 106, centre-to-centre spacing is 1~5 times of caliber, it is preferable that hole
Between centre-to-centre spacing be 1.5 times.Alternatively, a diameter of 3~8mm of stomata, centre-to-centre spacing is 1~5 times of caliber, it is preferable that Kong Jian
Centre-to-centre spacing be 1.5~3 times.
It is provided with as shown in figure 1, the expanding reach is arranged at the top of the top that the tubulation is distributed section, the expanding reach
Gas vent 105, the product for exporting reaction, wherein the impurity such as solvent, catalyst may be contained.
As shown in figure 1, the region between the multiple tubulation 106 and tubulation 106 constitutes and is provided with shell side, the shell side
Heat transferring medium.The tube side of tubulation 106 of tubulation distribution section is the main place that paste state bed reactor 1 reacts, and its shell side is that heat exchange is situated between
Matter, is that tubulation 106 provides heat.
As shown in figure 1, the lower side of the tubulation distribution section is provided with heat transferring medium entrance 102, upper side is set
There is heat transferring medium to export 103, heat transferring medium enters the shell side from the heat transferring medium entrance 102, then from the heat transferring medium
Discharge outlet 103.
As shown in figure 1, the multiple bottom of tubulation 106 is provided with gas distributor 107, stomata is distributed with thereon, it is ensured that
Reacting gas can enter in tubulation from all directions so that gas is evenly distributed.
As shown in figure 1, the lower side of the expanding reach is provided with colvent inlet 104, area of the hypomere tubulation UNICOM 108
Side is provided with discharge port 109, and solvent enters the multiple tubulation 106 from the colvent inlet 104, then from the discharge port
109 discharges.
As shown in figure 1, the upper end of reactor is expanding reach, its main function is to reduce the gas of reacted ethylene gas
Speed；The upper end of expanding reach is provided with metal demister 110, its main function is by a part of solvent carried secretly in gas analysis
Go out, return in reactor.As shown in Fig. 2 reaction system described in the utility model, for preparing ethene using acetylene.
The reaction system include above-mentioned shell and tube paste state bed reactor 1, condenser 2, gas-liquid separator 3, catalyst preparation tank 4 with
And green oil removal unit, the green oil removal unit includes solvent tank 9 and solvent reclamation device 10.
As shown in Fig. 2 the shell and tube paste state bed reactor 1 has gas access 101, gas vent 105, colvent inlet
104th, discharge port 109, heat transferring medium entrance 102, heat transferring medium outlet 103 and upper end area of UNICOM filter.
As shown in Fig. 2 the condenser 2 has high-temperature product gas entrance and mixed gas outlet, the high-temperature product gas enters
Mouth is connected with the gas vent of the shell and tube paste state bed reactor 1.
As shown in Fig. 2 the gas-liquid separator 3 has gaseous mixture entrance, ethene outlet and solvent export mouth, the mixing
Gas entrance is connected with the mixed gas outlet of the condenser 2.
The reaction product come out from the top of reactor 1, by the cooling of cooler, is subsequently passed gas-liquid separator 3, then pass through
Gas-liquid separation is crossed, product ethene is obtained, the solvent in gas is condensed out；The solvent condensed out can be pushed up by reactor 1
The colvent inlet 104 in portion is re-entered into reactor 1.
As shown in Fig. 2 the phase of colvent inlet 104 of the catalyst preparation tank 4 and the shell and tube paste state bed reactor 1
Even.
As shown in Fig. 2 the green oil removal unit is connected with the filter of the shell and tube paste state bed reactor, for connecing
Receive the solvent of the filter filtering.Specifically, as shown in Fig. 2 there is the solvent tank 9 green oil entrance to be exported with green oil,
The green oil entrance is connected with epimere UNICOM area's filter of the shell and tube paste state bed reactor 1.As shown in Fig. 2 described molten
There is agent regenerating unit 10 de-oiling entrance to be exported with de-oiling, and the green oil of the de-oiling entrance and the solvent tank 9 exports phase
Even, the de-oiling outlet is connected with the colvent inlet 104 of the shell and tube paste state bed reactor 1.
When find reaction efficiency decrease or solvent in there is yellow green color when, it should be due to side reaction generation
What green oil was caused.At this point it is possible to which a part of solvent in reactor 1 is filtered out from the accurate filter in reactor 1.
Solvent after filtering is entered in solvent tank 9, is then being passed into solvent reclamation device 10, is being passed through solvent reclamation device 10
Green oil is separated with solvent, solvent is re-entered into reactor 1 by the colvent inlet 104 at the top of reactor 1 again, and green oil is then
It can be preserved into green oil storage tank.
As shown in Fig. 2 the system also include thermal medium storage tank 4 and pump 5, wherein, one end of the thermal medium storage tank 4 with
The heat transferring medium outlet 103 of the shell and tube paste state bed reactor 1 is connected；One end of the pump 5 and the thermal medium storage tank 4
The other end is connected, and the other end of the pump 5 is connected with the heat transferring medium entrance 102 of the shell and tube paste state bed reactor 1.
As shown in Fig. 2 the system also includes temperature conditioning unit, it is arranged on the shell and tube paste state bed reactor 1 and institute
State between pump 5, the temperature conditioning unit includes heater 6, cooler 7 and bypassed with heat transferring medium.
Realize that acetylene prepares ethene by said system, generally first with nitrogen as source of the gas, whole system is entered into line replacement；
Then, the catalysts and solvents configured in catalyst preparation tank 8 are sent in shell and tube paste state bed reactor 1, then gradually
The heater 6 of unlatching temperature conditioning unit is gradually exchanged thermal medium and heated up；When the solvent temperature in reactor 1 reaches target temperature
And after system even running, shell and tube paste state bed reactor 1 will be passed through as the gaseous mixture of the acetylene of reacting gas and hydrogen
The gas access 101 of bottom is entered in reactor 1, and the operating pressure of reactor 1 is 0.15~0.45MPa, and temperature is 90~
180℃。
Reacting gas is entered in air inlet section, and tubulation is entered by the gas distributor 107 of each bottom of tubulation 106
In 106 reactors 1.Because the hole on gas distributor 107 is equally distributed, so reacting gas also evenly spreads to row therewith
Among the internal solvent of pipe 106.Section is distributed in tubulation, each tubulation 106 is paste state bed reactor 1 one small, due to each
The diameter of tubulation 106 is all smaller, highly of a relatively high, and it is more uniform that gas-liquid-solid three-phase can be mixed, when adding stop
Between, gas-liquid flow field distribution is improved, enlarge-effect is reduced so that it is more abundant that reaction can be carried out.Product gas is from tubulation
After being come out in 106, then by the expanding reach of reactor 1, reactor 1 is left from the head gas of reactor 1 outlet 105.
The multiple middle part of tubulation 106 is provided with area of epimere tubulation UNICOM 111, the two of area of the epimere tubulation UNICOM 111
End is provided with accurate filter；Multiple bottoms of tubulation 106 are provided with area of hypomere tubulation UNICOM 108, the hypomere tubulation UNICOM 108
The one end in area is discharge port 109.The usual filter is accurate filter, respectively has an essence at the two ends in area of epimere tubulation UNICOM
Close filter, main purpose is, for filtering out solvent, in the case of not parking, to change reaction dissolvent.
When find reaction efficiency decrease or solvent in there is yellow green color when, it should be due to side reaction generation
What green oil was caused.At this point it is possible to which a part of solvent in reactor 1 is filtered out from the accurate filter in reactor 1.
Solvent after filtering is entered in solvent tank 9, is then being passed into solvent reclamation device 10, is being passed through solvent reclamation device 10
Green oil is separated with solvent, solvent is re-entered into reactor 1 by the colvent inlet 104 at the top of reactor 1 again, and green oil is then
It can be preserved into green oil storage tank.
The product gas come out from the top of reactor 1, first passes through condenser 2 and is cooled down gas；Then, then gas-liquid is passed through
Separator 3 is separated the liquid such as gas and solvent, the solvent that the solvent and catalyst separated pass through the top of reactor 1
Entrance 104 is sent in reactor 1 again, and isolated gas is product ethene.
Shell and tube paste state bed reactor 1 provides heat, i.e. indirect heat exchange using heat transferring medium for reaction, will be changed using pump 5
Thermal medium is from thermal medium storage tank 4 is transferred to temperature conditioning unit；Temperature conditioning unit is bypassed by heater 6, the heat transferring medium being set up in parallel
With the three-line of cooler 7 composition, the different operating modes that it can be according to needed for reactor 1 are regulated and controled；When reaction system needs
When heating, heater 6 and heat transferring medium bypass are switched on, by adjusting the heat exchange in heat exchange power and heat transferring medium bypass
The flow of medium controls heating rate；When reactor 1 needs to move heat, it is possible to while controlling heating power, heat transferring medium
The flow and cooling power of bypass control the heat medium temperature to keep stable；When reaction system needs cooling, cooling is switched on
Device 7 and heat transferring medium bypass, cooling is controlled by adjusting the flow of the heat transferring medium in heat exchange power and heat transferring medium bypass
Speed；Temperature conditioning unit disclosure satisfy that requirement of each operating mode of shell and tube paste state bed reactor 1 for reaction system temperature.
It should be noted that each embodiment above by reference to described by accompanying drawing is only to illustrate the utility model rather than limit
Scope of the present utility model is made, it will be understood by those within the art that, do not departing from spirit of the present utility model and model
The modification carried out on the premise of enclosing to the utility model or equivalent substitution, all should cover within the scope of the utility model.
In addition, signified outer unless the context, the word occurred in the singular includes plural form, and vice versa.In addition, except non-specifically
Explanation, then all or part of of any embodiment can combine all or part of of any other embodiment to use.
Claims (10)
1. a kind of shell and tube paste state bed reactor, the reactor of ethene is prepared for high concentration acetylene, it is characterised in that the row
Tubular type paste state bed reactor includes tactic air inlet section, tubulation distribution section and expanding reach, in addition to connects the tubulation point
The epimere of cloth section and area of hypomere tubulation UNICOM, wherein,
The bottom of the air inlet section is provided with gas access, for reacting gas to be passed through into the shell and tube paste state bed reactor；
The tubulation distribution section is provided with multiple tubulations, is reacted for the reacting gas in tubulation distribution section,
Prepare upper position in the middle part of ethene, the multiple tubulation and be provided with area of epimere tubulation UNICOM, the two of area of the epimere tubulation UNICOM
End is provided with filter；The multiple tubulation bottom is provided with area of hypomere tubulation UNICOM, the one end in area of the hypomere tubulation UNICOM
It is provided with discharge port；
Gas vent is provided with the top of the expanding reach.
2. shell and tube paste state bed reactor as claimed in claim 1, it is characterised in that the shell and tube paste state bed reactor
Region between multiple tubulations and tubulation, which is constituted in shell side, the shell side, is provided with heat transferring medium.
3. shell and tube paste state bed reactor as claimed in claim 2, it is characterised in that the tubulation is distributed the lower side of section
Heat transferring medium entrance is provided with, upper side is provided with heat transferring medium outlet, for heat transferring medium to be entered from the heat transferring medium
Mouth enters the shell side, then exports discharge from the heat transferring medium.
4. shell and tube paste state bed reactor as claimed in claim 1, it is characterised in that the multiple tubulation bottom is provided with gas
Body distributor, is distributed with stomata thereon.
5. shell and tube paste state bed reactor as claimed in claim 4, it is characterised in that the lower side of the expanding reach is set
There is colvent inlet, area of hypomere tubulation UNICOM side is provided with discharge port, for solvent to be entered into institute from the colvent inlet
Multiple tubulations are stated, then are discharged from the discharge port.
6. shell and tube paste state bed reactor as claimed in claim 1, it is characterised in that the upper end of the expanding reach is provided with gold
Belong to demister.
7. a kind of reaction system, ethene is prepared for acetylene, it is characterised in that the reaction system includes such as claim 1-6
Any described shell and tube paste state bed reactor, condenser, gas-liquid separator, catalyst preparation tank and green oil removal unit,
Wherein,
The shell and tube paste state bed reactor have gas access, gas vent, colvent inlet, discharge port, heat transferring medium entrance,
Heat transferring medium exports and is arranged at the filter at area of epimere tubulation UNICOM two ends；
The condenser has high-temperature product gas entrance and mixed gas outlet, and the high-temperature product gas entrance is starched with the shell and tube
The gas vent of state bed reactor is connected；
The gas-liquid separator have gaseous mixture entrance, ethene outlet with solvent export mouth, the gaseous mixture entrance with it is described cold
The mixed gas outlet of condenser is connected；
The catalyst preparation tank is connected with the colvent inlet of the shell and tube paste state bed reactor；
The green oil removal unit is connected with the filter of the shell and tube paste state bed reactor, for receiving the filter mistake
The solvent of filter.
8. reaction system as claimed in claim 7, it is characterised in that the green oil removal unit includes solvent tank and solvent
Regenerating unit, wherein, there is the solvent tank green oil entrance to be exported with green oil, the green oil entrance and the shell and tube slurry
The filter of bed reactor is connected；
There is the solvent reclamation device de-oiling entrance to be exported with de-oiling, and the green oil of the de-oiling entrance and the solvent tank goes out
Mouth is connected, and the de-oiling outlet is connected with the colvent inlet of the shell and tube paste state bed reactor.
9. reaction system as claimed in claim 7, it is characterised in that the system also includes thermal medium storage tank and pump, wherein,
One end of the thermal medium storage tank and the heat transferring medium outlet of the shell and tube paste state bed reactor；
One end of the pump is connected with the other end of the thermal medium storage tank, the other end of the pump and the shell and tube slurry bed system
The heat transferring medium entrance connection of reactor.
10. reaction system as claimed in claim 9, it is characterised in that the system also includes temperature conditioning unit, and it is arranged on institute
State between shell and tube paste state bed reactor and the pump, for controlling the heat transferring medium into the shell and tube paste state bed reactor
Temperature, the heater, cooler and heat transferring medium that the temperature conditioning unit includes being set up in parallel is bypassed.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720062686.6U CN206519141U (en) | 2017-01-19 | 2017-01-19 | Shell and tube paste state bed reactor and reaction system |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201720062686.6U CN206519141U (en) | 2017-01-19 | 2017-01-19 | Shell and tube paste state bed reactor and reaction system |
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ID=59890126
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| Application Number | Title | Priority Date | Filing Date |
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| CN201720062686.6U Expired - Fee Related CN206519141U (en) | 2017-01-19 | 2017-01-19 | Shell and tube paste state bed reactor and reaction system |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111013497A (en) * | 2019-12-27 | 2020-04-17 | 江苏奥克化学有限公司 | Tube array reactor |
| CN113045370A (en) * | 2019-12-27 | 2021-06-29 | 辽宁奥克化学股份有限公司 | Sulfonation method |
-
2017
- 2017-01-19 CN CN201720062686.6U patent/CN206519141U/en not_active Expired - Fee Related
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN111013497A (en) * | 2019-12-27 | 2020-04-17 | 江苏奥克化学有限公司 | Tube array reactor |
| CN113045370A (en) * | 2019-12-27 | 2021-06-29 | 辽宁奥克化学股份有限公司 | Sulfonation method |
| CN111013497B (en) * | 2019-12-27 | 2022-03-22 | 江苏奥克化学有限公司 | Tube array reactor |
| CN113045370B (en) * | 2019-12-27 | 2023-07-18 | 辽宁奥克化学股份有限公司 | Sulfonation method |
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