CN106824019A - 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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- CN106824019A CN106824019A CN201710037977.4A CN201710037977A CN106824019A CN 106824019 A CN106824019 A CN 106824019A CN 201710037977 A CN201710037977 A CN 201710037977A CN 106824019 A CN106824019 A CN 106824019A
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- 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
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- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
- C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
- C07C5/08—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds
- C07C5/09—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of carbon-to-carbon triple bonds to carbon-to-carbon double bonds
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- 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
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00176—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles outside the reactor
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- Combustion & Propulsion (AREA)
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- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
Abstract
The present invention relates 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 of the connection 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, react to prepare ethene in tubulation distribution section for reacting gas, multiple tubulations are provided with area of epimere tubulation UNICOM and area of hypomere tubulation UNICOM, and the two ends in area of epimere tubulation UNICOM are provided with filter, 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 of the present invention, 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 present invention relates to chemical field, ethene field is prepared especially with high concentration acetylene, and in particular to a kind of tubulation
The reaction system of formula 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, its product
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, Non-catalytic partial oxygen is passed through 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.With 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 being removed in ethene
Acetylene impurities, the reactor for using is fixed bed reactors, and solid-phase catalyst is loaded in the reactor 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
Hydrogenation reactor is there are still serious problems such as green oil generating amount big, catalyst cycle period is short, reactors easy " temperature runaway ".
The appearance of traditional paste state bed reactor solves above mentioned problem to a certain extent, because of its simple structure, 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.
The content of the invention
To overcome above mentioned problem, the present invention to provide a kind of shell and tube paste state bed reactor and reaction system so that reaction
Device internal temperature is uniform, increases reaction raw materials time of contact, reduces the impurity component in product, is conveniently replaceable solvent, carries
High efficiency.System of the present invention has green oil removal unit, greatly reduces shadow of the green oil to catalyst activity
Sound realizes the smooth long term running of device.
Shell and tube paste state bed reactor of the present invention, the reactor of ethene is prepared for high concentration acetylene.The row
Tubular type paste state bed reactor includes tactic
Air inlet section, tubulation distribution section and expanding reach, also join including connecting the epimere and hypomere tubulation of the tubulation distribution section
Logical area, 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 in tubulation distribution section for the reacting gas anti-
Should, ethene is prepared, the multiple tubulation middle part upper position is provided with area of epimere tubulation UNICOM, area of the epimere tubulation UNICOM
Two ends are provided 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 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 is provided with changes
Thermal medium outlet, for heat transferring medium to be entered into the shell side from the heat transferring medium entrance, exports 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 the hypomere tubulation UNICOM side sets
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 of the present invention, for preparing ethene using acetylene.The reaction system includes above-mentioned tubulation
Formula 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,
The heat transferring medium outlet of one end of the thermal medium storage tank and 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 including simultaneously
Arrange heater, cooler and the heat transferring medium bypass for setting.
Beneficial effects of the present invention：
The design in area of tubulation UNICOM in shell and tube paste state bed reactor of the present invention, in ensure that each tubulation
Liquid level is homogeneous, it is to avoid gas short circuit, the equipment of filter therein can reduce the impurity component in product.Additionally, tubulation
Each tubulation is a small slurry bed system in formula paste state bed reactor, because the diameter of each tubulation is smaller, height phase
To higher, it is more uniform that gas-liquid-solid three-phase can mix, and increased time of contact, improves gas-liquid flow field distribution, reduces
Enlarge-effect so that it is more abundant that reaction can be carried out.
In addition, system of the present invention, with green oil removal unit, greatly reduces green oil to catalyst activity
Influence realizes the smooth long term running of device.System of the present invention can realize the accurate control to system solvent temperature
System, keeps the temperature of solvent to stablize relatively, so as to ensure that the even running of whole system；Furthermore, using the aobvious of liquid phase solvent
Heat, heat-sinking capability is significantly improved, and can be quickly moved out the heat that selective hydrogenation of acetylene generation ethene is produced, and reduces reaction bed
Temperature, improves the conversion ratio of acetylene and the selectivity of ethene.
System of the present invention solves the fixed bed reactors in preparing ethylene by selective hydrogenation of acetylene reaction well
In green oil generating amount it is big, catalyst cycle period is short, the problem of reactor easily " temperature runaway ", due to catalyst granules in fluid bed
Between mutual sharp impacts, cause the loss of catalyst, the difficulty of dedusting and due to the corrasion of solid particle, heat exchange component and
The problem of the serious wear of reactor.
Brief description of the drawings
Fig. 1 is the structural representation of shell and tube paste state bed reactor of the present invention.
Fig. 2 is the structural representation of reaction system of the present invention.
Specific embodiment
Below in conjunction with drawings and Examples, specific embodiment of the invention is described in more details, so as to energy
Enough more fully understand the advantage of the solution of the present invention and its various aspects.However, specific embodiments described below and implementation
Example is only descriptive purpose, rather than limitation of the present invention.
As shown in figure 1, shell and tube paste state bed reactor 1 of the present invention, the anti-of ethene is prepared for high concentration acetylene
Answer device.The shell and tube paste state bed reactor 1, by air inlet section, tubulation distribution section and expanding reach, also includes including tactic
Connect epimere and the area of hypomere tubulation UNICOM 111,108 of the tubulation distribution section.
As shown in figure 1, the air inlet section is arranged on the bottom of the shell and tube paste state bed reactor 1, in 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 for the reacting gas in tubulation distribution section, prepares ethene, the multiple tubulation 106
Middle part is provided with area of epimere tubulation UNICOM 111, and the two ends in area of the epimere tubulation UNICOM 111 are provided 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
The two ends in area of tubulation UNICOM are provided 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 Kong Jian
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 between hole
Centre-to-centre spacing is 1.5~3 times.
As shown in figure 1, the expanding reach is arranged on the top that the tubulation is distributed section, it is provided with the top of the expanding reach
Gas vent 105, the product for deriving 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 shell side, it is provided with the shell side
Heat transferring medium.The tube side of tubulation 106 of tubulation distribution section is the main place of the reaction of paste state bed reactor 1, 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, from the heat transferring medium
Outlet 103 is discharged.
As shown in figure 1, the bottom of the multiple 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 the gas for reducing reacted ethylene gas
Speed；The upper end of expanding reach is provided with metal demister 110, its Main Function is a part of solvent analysis that will be carried secretly in gas
Go out, in returning to reactor.As shown in Fig. 2 reaction system of the present invention, for preparing ethene using acetylene.It is described
Reaction system includes above-mentioned shell and tube paste state bed reactor 1, condenser 2, gas-liquid separator 3, catalyst preparation tank 4 and green
Oily 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 export 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.
From the top of reactor 1 product out, by the cooling of cooler, gas-liquid separator 3 is subsequently passed, then pass through
Gas-liquid separation is crossed, product ethene is obtained, the solvent in gas is condensed out；The solvent for condensing 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 de-oiling entrance is connected with the green oil outlet of the solvent tank 9,
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 a part of solvent in reactor 1 is filtered out from the accurate filter in reactor 1.
Solvent after filtering is entered into solvent tank 9, is then being passed into solvent reclamation device 10, by 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
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 that heater 6, cooler 7 are 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 is 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 into reactor 1, and the operating pressure of reactor 1 is 0.15~0.45MPa, and temperature is 90~
180℃。
Reacting gas is entered into air inlet section, and tubulation is entered into 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
In the middle of the internal solvent of pipe 106.Section is distributed in tubulation, each tubulation 106 is a small paste state bed reactor 1, 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 mix, when increased stop
Between, gas-liquid flow field distribution is improved, reduce enlarge-effect so that it is more abundant that reaction can be carried out.Product gas are from tubulation
In 106 out after, then by the expanding reach of reactor 1, reactor 1 is left from the head gas of reactor 1 outlet 105.
The middle part of the multiple 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；The bottom of multiple tubulations 106 is 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 a part of solvent in reactor 1 is filtered out from the accurate filter in reactor 1.
Solvent after filtering is entered into solvent tank 9, is then being passed into solvent reclamation device 10, by 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
Can be preserved into green oil storage tank.
From the top of reactor 1 product gas out, first pass through condenser 2 and cooled down gas；Then, then by gas-liquid
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, for reaction provides heat, i.e. indirect heat exchange, will be changed using heat transferring medium using pump 5
Thermal medium is transferred in temperature conditioning unit from thermal medium storage tank 4；Temperature conditioning unit is bypassed by the heater 6, heat transferring medium being set up in parallel
Constituted with the three-line of cooler 7, the different operating modes that it can be according to needed for reactor 1 are regulated and controled；When reaction system needs
When intensification, 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 come control heat medium temperature keep stabilization；When reaction system needs cooling, cooling is switched on
Device 7 and heat transferring medium are bypassed, and 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 used to illustrate rather than limitation originally
The scope of invention, it will be understood by those within the art that, it is right under the premise without departing from the spirit and scope of the present invention
Modification or equivalent that the present invention is carried out, all should cover within the scope of the present invention.Additionally, signified unless the context
Outward, the word for occurring in the singular includes plural form, and vice versa.In addition, unless stated otherwise, then any embodiment
All or part of can combine any other embodiment all or part of 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, also including connecting 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 in tubulation distribution section for the reacting gas,
Ethene is prepared, the multiple tubulation middle part upper position is 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 constitutes shell side, and heat transferring medium is provided with the shell side.
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, is discharged being exported 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 the 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 is 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
Category 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 has gaseous mixture entrance, ethene outlet and solvent export mouth, and the gaseous mixture entrance is cold with described
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, the solvent tank has green oil entrance with green oil outlet, 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 de-oiling entrance goes out with the green oil of the solvent tank
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,
The heat transferring medium outlet of one end of the thermal medium storage tank and 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 temperature conditioning unit includes the heater, cooler and the heat transferring medium bypass that are set up in parallel.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201710037977.4A CN106824019A (en) | 2017-01-19 | 2017-01-19 | Shell and tube paste state bed reactor and reaction system |
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| CN201710037977.4A CN106824019A (en) | 2017-01-19 | 2017-01-19 | Shell and tube paste state bed reactor and reaction system |
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| CN109289713A (en) * | 2018-10-18 | 2019-02-01 | 辽宁石油化工大学 | A kind of mosquito-repellent incense coil pipe isothermal reactor and application method |
| CN110694558A (en) * | 2019-10-29 | 2020-01-17 | 浙江新安化工集团股份有限公司 | Multi-region slurry-state 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 |
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- 2017-01-19 CN CN201710037977.4A patent/CN106824019A/en active Pending
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| CN109173942A (en) * | 2018-09-10 | 2019-01-11 | 李洁 | A kind of tubular heat exchanger and F- T synthesis paste state bed reactor |
| CN109173942B (en) * | 2018-09-10 | 2021-01-01 | 山东嘉隆新能源股份有限公司 | Fischer-Tropsch synthesis slurry bed reactor containing tube type heat exchanger |
| CN109289713A (en) * | 2018-10-18 | 2019-02-01 | 辽宁石油化工大学 | A kind of mosquito-repellent incense coil pipe isothermal reactor and application method |
| CN110694558A (en) * | 2019-10-29 | 2020-01-17 | 浙江新安化工集团股份有限公司 | Multi-region slurry-state tube array reactor |
| CN110694558B (en) * | 2019-10-29 | 2021-01-22 | 浙江新安化工集团股份有限公司 | Multi-region slurry-state tube array reactor |
| US11918992B2 (en) | 2019-10-29 | 2024-03-05 | Zhejiang Wynca Chemical Industry Group Co., Ltd | Multi-region slurry shell-and-tube reactor |
| CN113045370A (en) * | 2019-12-27 | 2021-06-29 | 辽宁奥克化学股份有限公司 | Sulfonation method |
| 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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