CN102211003B - Temperature control device and method for controlling temperature of tube reactor - Google Patents
Temperature control device and method for controlling temperature of tube reactor Download PDFInfo
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- CN102211003B CN102211003B CN2011100903461A CN201110090346A CN102211003B CN 102211003 B CN102211003 B CN 102211003B CN 2011100903461 A CN2011100903461 A CN 2011100903461A CN 201110090346 A CN201110090346 A CN 201110090346A CN 102211003 B CN102211003 B CN 102211003B
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- heat
- register
- carrying agent
- temperature
- temperature adjustment
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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
- B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
- B01J8/06—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds in tube reactors; the solid particles being arranged in tubes
- B01J8/067—Heating or cooling the reactor
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
- F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F28—HEAT EXCHANGE IN GENERAL
- F28F—DETAILS OF HEAT-EXCHANGE AND HEAT-TRANSFER APPARATUS, OF GENERAL APPLICATION
- F28F13/00—Arrangements for modifying heat-transfer, e.g. increasing, decreasing
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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
- B01J2208/00212—Plates; Jackets; Cylinders
- B01J2208/00221—Plates; Jackets; Cylinders comprising baffles for guiding the flow of the heat exchange medium
-
- 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
- B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the reactor
Abstract
The invention provides a temperature control device for controlling the temperature of a tube bundle reactor for catalytic reactions using temperature-adjusting gas. The tube bundle reactor comprises a catalyst chamber and a heat carrier chamber adjacent to the catalyst chamber and separated from the catalyst chamber. The temperature control device communicates with the heat carrier inlet and the heat carrier outlet of the heat carrier chamber. The temperature-adjusting gas flows through the temperature control device and the heat carrier chamber in the circuit. The temperature control device comprises a compression gas supply device, a heating device for temperature-adjusting gas and a conveying device for temperature-adjusting gas. The temperature control device is arranged on a transportable frame, which can also be conveyed to various reactor systems as a mobile temperature control device. Meanwhile, a temperature control method for controlling the temperature of a tubular reactor is also provided.
Description
Technical field
The present invention relates to a kind of for by the register of temperature adjustment gas regulation for the temperature of the tube bundle reactor of catalytic reaction, wherein said tube bundle reactor comprises that a catalyst case and is in abutting connection with described catalyst case, but the heat-carrying agent chamber separated with described catalyst case, wherein said register can be connected with the heat-carrying agent outlet is mobile with the heat-carrying agent entrance of described heat-carrying agent chamber, described temperature adjustment gas flow is crossed register and the heat-carrying agent chamber in closed circuit, described register comprises: the Compressed Gas feedway, for the heater of described temperature adjustment gas with for the conveying device of described temperature adjustment gas.The present invention relates in addition a kind of method of utilizing the temperature of this register adjustable pipe bundle reactor.
Background technology
In order to implement heterogeneously catalysed gas phase reactions for example oxidation technology, hydrogenation process, dehydrogenating technology, nitriding process, alkylation process, in chemical industry, the tube bundle reactor that particularly has the isothermal fixed bed has been proved to be favourable as special fixed bed reactors structural type.
In the first embodiment, tube bundle reactor comprises the reactor master unit, and this master unit has the bundle of reaction tubes of vertical setting, wherein mostly contains granular catalyst and also contains in case of necessity inert material.Reaction tube its end part seal be fixed on bottom pipe bottom and lower pipe.Tube bank is surrounded by shell of reactor, described shell of reactor with each pipe sealed bottom, is connected and with its formation shell chamber, heat-carrying agent is mobile around reaction tube in this shell chamber.In this case, the shell chamber also is called as the heat-carrying agent chamber, and this pipe is called catalyst case.Described reaction can be the heat absorption or heat release.Reaction gas mixtures flows to reaction tube via the reactor cover that covers a pipe bottom and from reaction tube, discharges via the reactor cover that covers another pipe bottom as product gas mixture.
In order to obtain stable reaction condition, strive for reaching around the almost stationary temperature of the heat-carrying agent of reaction tube and good heat transmission.For the necessary auxiliary equipment of tube bundle reactor work, for example EGR, heat exchanger and heater in mostly being arranged on along separate routes, be usually located at the outside of shell of reactor and utilize short as far as possible connecting line to be directly connected on shell of reactor.Correspondingly, heat-carrying agent is entering shell of reactor and from shell of reactor, is flowing out near another pipe bottom near one pipe bottom.
Selection to the heat-carrying agent for this tube bundle reactor is determined by the maximum temperature occurred at work.When the about lower temperature under 300 ℃, the cooling boiling water that can utilize is realized.At this, the pressure in the heat-carrying agent chamber can be increased to about 100bar.Due to this boundary condition, reactor must be designed to have the pressure vessel of relatively thick degree.The advantage of this type of reactor is Temperature Distribution and transmitting in the extraordinary heat of shell side very uniformly in the heat-carrying agent chamber, can design simply mobile guiding device thus.
In another kind of embodiment, catalyst case and heat-carrying agent chamber can exchange.In other words, pipe can be designed to cooling tube and be flow through by heat-carrying agent.Catalyst is arranged in the shell chamber of cooling tube.In this case, pipe is called to the heat-carrying agent chamber, and the shell chamber is called catalyst case.
In the about temperature range of 250 ℃ to 650 ℃, carry out heat extraction through molten salt bath commonly used.This heat-carrying agent has low-down steam pressure and in stress-free mode, moves at work.For the about temperature below 400 ℃, can use organic heat-carrying agent, for example heat-carrying agent oil.Tube bundle reactor for this heat-carrying agent type is for example known from DE 2 207 166 A1 or EP 1 569 745 A1.
If when starting or stopping using tube bundle reactor and during operation, also must regulate and control (konditionieren) catalyst, special problem may occur." regulation and control " are interpreted as, make catalyst have certain characteristic.
Therefore, may be necessary that: before starting tube bundle reactor or while starting tube bundle reactor, make catalyst from inactive state be transformed into for the production of activated state, this inactive state for example by transportation be filled into catalyst case in the time with air in contacting of oxygen produce.Otherwise, may be necessary that: make active catalyst deactivation in order to change reliably and discharge when stopping using tube bundle reactor or after stopping using tube bundle reactor.
In addition, in different chemical reactions, the activity of catalyst weakens at work gradually, yet catalyst is in this same undesirably deactivatedization.This may be due to different reasons.Catalyst for example As time goes on oxidized or catalyst surface be coated with carbon black or other pollutant.In order to ensure economic production, must recover the activity of catalyst.It is complicated and expensive replacing catalyst fully, therefore as far as possible preferably regulates and controls in position catalyst, and described regulation and control also are called regeneration in this case.The regeneration interval is relevant to each technical process.
Described regulation and control realize in the following manner, that is: within the shorter time of several hours to several days orders of magnitude, guide regulation and control gas by catalyst inserts (Katalysatorsch ü ttung).This regulation and control gas has composition, the temperature and pressure that is suitable for corresponding technique.Oxidation reaction or reduction reaction appear.Each influence factor causes corresponding structural measure.Composition and pressure can change well by the conversion equipment in the reactor upstream usually.
The subject matter of each modulation process process is: on each position of catalyst inserts, will follow a temperature of determining.For this reason, only the temperature at reactor upstream regulation regulation and control gas is inadequate, because regulation and control gas has just reached the temperature identical with temperature in reactor after short input distance.In addition, the modulation process process is neither endothermic nor exothermic mostly.Therefore, from the heat-carrying agent side, be indispensable to the temperature adjustment of catalyst inserts.Difficult point is now: each heat-carrying agent system specifically is matched with corresponding production technology for economic reasons usually, and therefore required regulating and controlling temperature also can not be conditioned apparently higher than the reaction temperature in production technology.Therefore, in regulation and control duration, for the production of or the heat-carrying agent of work to replace by the heat-carrying agent that can follow regulating and controlling temperature.
In reaction temperature, for example be, in chemical production processes below 300 ℃, that carry out in moving (mode) at boiling water, due to temperature higher than 400 ℃, the regeneration technology short time, only using molten salt bath as heat-carrying agent for whole service.Yet the application molten salt bath is cooling more expensive than direct boiling water as heat-carrying agent.
From a kind of known simpler and more economical method of cost DE 38 19 357 A1.The method relates to the regeneration of pellet type catalyst in the reaction tube of tube bundle reactor, and this tube bundle reactor comes cooling for the cooling fluid that pressure and its reaction tube of 20bar to 150bar are crossed the shell chamber by percolation.In this regeneration technology, at first from the shell chamber, removing cooling fluid, the catalyst that then will directly contact with hot regeneration gas be heated to 100 ℃ to 400 ℃, higher than the temperature of the temperature under working condition.Then the heat medium of gaseous state or steam-like is introduced in the shell chamber, the temperature difference between the reaction tube outside and shell of reactor inboard is maintained at 100 ℃ at the most thus.Regeneration (technique) can utilize hot nitrogen wash catalyst before starting.The nitrogen of heat or overheated water vapour for example can be used as heat-carrying agent.Utilize valve to realize the transformation of duty.Other details of the heat-carrying agent system of using in regeneration technology repeats no more.Yet in this method of temperature control, the temperature of the heat medium of gaseous state or steam-like at it from the shell chamber inlet until the outlet stroke on marked change, thereby the longitudinal temperature distribution along reaction tube is very inhomogeneous, and this point is disadvantageous for the even regeneration of catalyst.
WO2009/118372 A1 has described a kind of method, and the method is for regenerating the catalyst original position that contains cobalt and titanium of deactivatedization in fischer-tropsch process at the fixed bed gas that the oxidation step between 580 ℃ and 670 ℃ and reduction step utilization subsequently comprise hydrogen at least partly by temperature.Catalyst is preferably placed in the reaction tube of tube bundle reactor, and described reaction tube is undertaken cooling at regeneration period by water and/or steam on shell side.In stable operation, fischer-tropsch process in the situation that temperature between 100 ℃ and 600 ℃ and pressure between 5bar to 150bar, implementing.No longer the heat-carrying agent system is additionally instructed.
From known a kind of method and reactor be used to implementing the endothermic reaction DE 34 39 176 A1.At this, utilize simultaneously the catalyst of endothermic reaction regeneration in the second reactor in a reactor.The document proposes: the CO that guide heat-carrying agent in closed circuit, for example compresses
2.Described register has air blast and heater.Two reactors are changed mutually.Spatially the regeneration of the catalyst in remote isolated reactor assembly does not have reference significance at this each other.
Always efficiency is lower and/or cost is higher for the known solution of during catalyst inserts regulation and control, the temperature of tube bundle reactor being regulated, particularly the temperature of different reactor system being regulated.
Summary of the invention
Therefore the objective of the invention is: propose a kind of register and method, temperature for adjustable pipe bundle reactor and different reactor assembly, especially for regulation and control (Konditionieren) tube bundle reactor and different reactor assemblies, utilize this register and method can obtain Temperature Distribution and high heat discharge or high heat input very uniformly, simultaneously can reduction technology and cost.
According to the present invention, described purpose realizes in the following manner by the register that starts described type: described register is arranged on transportable framework and can be transported to different reactor assemblies as register movably.In addition according to the present invention, the described purpose also method of the feature by having claim 9 realizes.
According to the present invention, this register is arranged on transportable framework.This has realized the very compact design of register due to the structure space dwindled.Therefore, this register can be transported to different reactor assemblies in simple mode.By on a plurality of reactor assemblies, using successively movably register, reduced the correlative investment cost of each reactor assembly.The external dimensions of this transportable framework is preferably suitable with the basal plane of standard freight container at this, and for example width is 2.438m (8 feet), and length is 6.058m (20 feet) or 12.192m (40 feet).
The present invention utilizes the following fact: temperature adjustment power obviously improves by the Compressed Gas feedway, and now obviously reduce in the required structure space of register.Because gas supply device is the Compressed Gas feedway, thus when mass flow is identical volume flow so flowing velocity less.Therefore, when mass flow was identical, pressure loss approximately linear ground raise along with pressure and reduces.
On the contrary, when given reactor assembly flow cross section, in the situation that the pressure loss remains unchanged, higher mass flow is circulated.Higher mass flow means higher heat absorption ability and the higher heat transmission on the reaction tube wall of temperature adjustment gas.At this, the temperature of the Compressed Gas in tube bundle reactor only improves a little, thereby temperature not only all distributes extremely equably on the cross section of tube bundle reactor but also along the longitudinal direction of reaction tube.Therefore, can obviously improve temperature adjustment power, and without excessively improving the driving power of recycle gas blower.Can save thus locus and the weight of drive motors and its electric supply installation.Simultaneously, can smaller select the internal duct of register and the flow cross section of equipment, reduce thus its structure space.
Preferably, described Compressed Gas feedway has compressor.Therefore, the compressed gas physical efficiency produces in mode simple and cost economy.
In a kind of favourable design of the present invention, the pressure of described Compressed Gas is in the scope of 3bar to 100bar, preferably in the scope in the scope of 5bar to 50bar, particularly preferably in 10bar to 30bar.In this pressure limit, particularly, in the pressure limit of 10bar to 30bar, realized the obvious rising of temperature adjustment power, and only needed less to improve the driving power of recycle gas blower.
Preferably, described register has two be used to the connecting line in the heat-carrying agent entrance that is connected to described heat-carrying agent chamber or heat-carrying agent outlet, and at least one in described connecting line has the elasticity middleware.By the connecting portion of this flexibility/flexibly, needn't be matched with for the compensated position tolerance connecting portion of reactor assembly bothersomely.In the movably design of register, can easily be connected on different reactor assemblies by this measure.
At this, described elasticity middleware have be used to absorb internal pressure, adjustable tension force unloading section.Thus, the elasticity middleware can absorb internal pressure in simple mode, and can not add load to pipeline component subsequently.
Preferably, described temperature adjustment gas comprises air, nitrogen, carbon dioxide, water vapour or its mixture.Can be easily so cost obtain in more economical way this gas.
In a kind of favourable embodiment of the present invention, described register comprises a cooling device for cooling described temperature adjustment gas, and described cooling device is designed to: water is directly sprayed in the temperature adjustment gas return path.Can simply and rapidly regulate/set the rated temperature of temperature adjustment gas thus.
Preferably, described register comprises the adjusting device be used to the temperature and pressure of regulating described temperature adjustment gas.Thereby the temperature and pressure that can keep very reliably temperature adjustment gas.
In a kind of favourable embodiment of the method according to this invention, for the catalyst inserts in tube bundle reactor regulates and controls, the heat-carrying agent loop of this tube bundle reactor is flow through by heat-carrying agent liquid or the part evaporation in the production phase, during the temperature adjustment gas circulation, temperature by described temperature adjustment gas---and, where necessary, pressure---be increased to the initial temperature of regulation process; Guiding regulation and control gas is by the catalyst inserts.The regulation and control of catalyst inserts also comprise used catalyst inserts regeneration.Utilize this measure to regulate and control in position the catalyst inserts in tube bundle reactor in simple mode.Due to Compressed Gas, the temperature of temperature adjustment gas not only all distributes very equably transverse to reaction tube but also along its longitudinal direction, thereby regulation process also carries out equably in whole catalyst inserts inside, and has guaranteed thus the even quality of catalyst inserts.In order to help the course of work, in the steps d of claim 9) in can be before regulation and control gas the guiding hot gas by the catalyst inserts.
As mentioned above, according to the present invention, register is installed on transportable framework, and register is transported to tube bundle reactor be used to carrying out temperature adjustment, is transported again after the temperature adjustment process finishes.Avoided thus otherwise must be arranged on the expense of the fixedly register in each tube bundle reactor.Reduce significantly by this way the correlative investment cost of the register of each tube bundle reactor.
The accompanying drawing explanation
Below by accompanying drawing, exemplarily elaborate the present invention.Wherein show:
Fig. 1 illustrates the flow chart according to the first embodiment of register of the present invention, in the heat-carrying agent loop of this register access tube bundle reactor;
Fig. 2 a illustrates the side view according to the second embodiment of register of the present invention with schematic diagram, in the heat-carrying agent loop of this register access tube bundle reactor;
Fig. 2 b is to illustrate the top view of the second embodiment in the 2a that publishes picture.
The specific embodiment
Fig. 1 schematically shows to have according to the parts of the embodiment of register 102 of the present invention and the flow chart of tube bundle reactor 100.
At tube bundle reactor 100 shown in this, be designed to single district.Tube bundle reactor 100 has a plurality of reaction tubes 103 that are filled with catalyst, and this reaction tube is to restrain 104 arranged in form.Reaction tube 103 is fixed in pipe bottom 105 and lower pipe bottom 106 hermetically.Pipe bottom 105,106 is connected with cylindricality shell of reactor 107 on its perimeter, this shell of reactor 107 surrounds tube bank 104.The common shell chambers 108 that form of pipe bottom 105,106 and shell of reactor 107, the heat-carrying agent 109 be in normal operation in this shell chamber 108 in is around shower reaction tube 103.Tube bank 104 for example can be designed to have the inner chamber without pipe in a tubular form or circlewise on whole cross section.Usually between annular tube bank 104 and shell of reactor 107, be formed with an outer shroud without pipe.Upper pipe bottom 105 can be connected with top airscoop shroud 110 by upper flange, and lower pipe bottom 106 is connected with bottom hood 111 by lower flange.When on reaction gas side and/or heat-carrying agent side, having high workload pressure, can advantageously with being welded to connect, substitute the flange connection, as illustrated in fig. 1.Reaction tube 103 passes in airscoop shroud 110 and hood 111.Airscoop shroud 110 has air inlet pipe 112, and hood 111 has blast pipe 113.Heat-carrying agent 109 is guided through the shell chamber 108 of tube bundle reactor 100 by the guide of flow device be applicable to.Heat-carrying agent shown in reactor 100 in by upper and lower annulus line 114,115 and corresponding upper and lower connecting line 116,117, distribute or accumulate on the perimembranous of reactor 100.Under, (being positioned at right side in Fig. 1) first that be connected to annulus line 114,115 in this unshowned heat-carrying agent system take on 118, this heat-carrying agent system has EGR, register and other possible parts.
Below the operation for the first duty and the second duty is described.At this, the first duty is interpreted as the normal operating conditions of tube bundle reactor 100, reacting gas 130 enters in reactor 100 in this normal operating conditions, in this reactor 100, carry out chemical reaction, and then from these reactor 100 outputs, wherein the heat-carrying agent 109 of circulation is controlled reaction temperature in the shell chamber 108 of tube bundle reactor 100.The second duty is interpreted as regulation process, and gas 131 is crossed reactor 100 at the pipe effluent in this regulation process, and the composition of the gas of applying in this gas 131 and the first duty is different.In addition, in the second duty, heat-carrying agent 132 has the characteristic different from the heat-carrying agent in the first duty.Particularly, this heat-carrying agent is Compressed Gas, for example has in addition other composition, other temperature or the combination of described characteristic.Register 102 according to the present invention is preferred for this second duty.Under this duty, for example the gas for regenerated catalyst is conducted through reaction tube 103, and in the situation that use the gaseous state heat-carrying agent, the temperature of heat-carrying agent 132 is raised to apparently higher than the temperature of the first duty.
Under the first duty, reacting gas 130 enters in top airscoop shroud 110 via top air inlet pipe 112, be distributed to there on pipe bottom 105, again via the bottom blast pipe 113 of reaction tube 103 and bottom hood 111 from reactor 100, flowing out.Equally also directing reaction gas 130 passes through reactor 100 from bottom to top.
The heat-carrying agent 109 of the reaction utilization circulation in shell chamber 108 finished in the first duty is controlled.At this, heat-carrying agent 109 is transfused in lower annular pipeline 115 or upper, annular pipeline 114 and from corresponding another annulus line 114,115, exports again.In the situation that utilize the heat-carrying agent of evaporation, preferred water to carry out cooling exothermic reaction, liquid heat-carrying agent 109 is transfused in lower annular pipeline 115, and is distributed on perimembranous there.Heat-carrying agent is transported in the shell chamber 108 of reactor 100 and utilizes there the guide of flow device (not shown at this) be applicable to be distributed to equably on the cross section of reactor 100 by a plurality of bottoms connecting line 117.Liquid-the steam formed in reactor 100-mixture is directed in upper, annular pipeline 114 and from this upper, annular pipeline and takes over from reactor 100, discharging by a top by a plurality of tops connecting line 116.
Compressed Gas is directed in the loop of sealing as the heat-carrying agent 132 of the second duty.At this, Compressed Gas 132 comprises air, nitrogen, carbon dioxide, water vapour or their mixture.Utilize the first recycle gas blower 119 that Compressed Gas is transported in tube bundle reactor 100.In order to ensure good heat transmission, preferably utilize guide of flow device lateral guiding Compressed Gas 132 through tube bank 104, go back where necessary the application specific device.Compressed Gas 132, accumulates in upper, annular pipeline 114 and by this upper, annular pipeline, is taken over 137 outputs from top from reactor 100, flowing out by top connecting line 116.Depending on the mode of regulation process, heat is fed to reaction tube 103 or discharges from reaction tube.Correspondingly, Compressed Gas 132 must be cooled or heat.In the situation that carry out coolingly, from the Compressed Gas 132 of upper, annular pipeline 114, flow through cooler 120, this cooler is preferably designed to aerial cooler.Alternatively or additionally, Compressed Gas 132 can be undertaken by unshowned mixing arrangement in Fig. 1 cooling, Compressed Gas 132 is undertaken cooling by the direct injection of water in this mixing arrangement.
If regulation process be heat absorption, namely absorb heat, in heater 123, be that Compressed Gas 132 heats.Then, again Compressed Gas 132 is transported in tube bundle reactor 100 by the first recycle gas blower 119.At this, can also change the serial connection sequence of parts of each series connection of register 102.Thereby this may be advantageously, that is: the heater streamwise is arranged on the downstream of the first recycle gas blower or is arranged to and arranges with this first recycle gas blower is parallel.In order to remain on the operating pressure in the heat-carrying agent system, be provided with pressure regulating system 127.At this, pressure sensor 128 gaging pressures.If hypotony, improve pressure by compressor 125, this compressor is connected to the position be applicable in the heat-carrying agent system.When hypertonia, open pressure-relief valve 129.
Example as the efficiency of register 102 according to the present invention and the method according to this invention, activate new catalyst inserts by the radial directed heat-carrying agent, with the normal operation for next time in tube bundle reactor 100.Will be in situation 1 by being in the air under environmental pressure activation and in situation 2, compare by compressed-air actuated activation.
Technical data:
13300 external diameters are that 30mm, length are the reaction tube of 8m.
Housing diameter 4900mm.
The nominal pipe diameter DN800 of the air inlet pipe of heat-carrying agent and blast pipe.
Approximately activating and discharging from reactor the heat of 200KW 300 ℃ the time.
Situation 1: be 50000m by conveying capacity
3The register of/h make to be under environmental pressure, inlet temperature is that the air of 300 ℃ circulates.
Situation 2: by being 19000m according to of the present invention, conveying capacity
3The register of/h make to be under absolute pressure 20bar, inlet temperature is that the air of 300 ℃ circulates.
Table 1: relatively calculate
As what the result provided from table 1, learn, in situation 1, in situation 2, be only 3.0K for 22.7K in the rising of reactor Air temperature.The mean heat transfer coefficient of air/reaction tube is 60W/m in situation 1
2K and be 190W/m in situation 2
2K.Therefore, when required circulating power is roughly the same, in situation 2, can obtain the obvious improvement of reaction tube 103 heat transmission and the temperature adjustment obviously improved, be isothermal.
Shown in Fig. 2 a and Fig. 2 b according to register 102 of the present invention, as the unit be arranged on compactly on transportable framework 139.As this illustrate, framework 139 can utilize hanger 140 promote and rise to installed position by transport vehicle.Other version is also possible.For example framework can be designed to container and have skid and promote connecting portion, on this lifting connecting portion, can be equipped with the towing hook of cargo vehicle, in order to container is dragged on its loading surface.After arrangement, the connecting line 133 of the connecting line 134 by the pressure side and suction side is realized being connected.Come the reactor connecting portion of the annulus line 114,115 of autoreactor 100 must be harmonious with the link position of register 102 as well as possible.Yet, for example due to the local circumstance that causes dislocation or tolerance, in fact only can limitedly follow this link position.Therefore, at least one in connecting line 133,134 has the flange connecting portion 135,136 with elasticity middleware 141,142.Can compensate within the specific limits the dislocation of connecting portion thus.If pipeline is connected to each other, link position utilize elasticity middleware 141,142 by for absorb internal pressure, adjustable tension force unloading section 143,144 is fixed on its position.
The all parts of register 102 is arranged to a unit compactness, the saving position on transportable framework 139.The connecting line 133 of suction side leads to cooler 120, and this cooler is designed to aerial cooler at this.Compressed Gas pipeline 145 leads to therefrom electric heater 123 and passes into therefrom in the first recycle gas blower 119, and Compressed Gas pipeline 145 leads to reactor 100 from this first recycle gas blower 119 via elasticity middleware 142.Pressure keeps by being arranged on the other compressor of electric heater 123 125.Pressure piping 146 leads to the intake line for the first air blast 119 above electric heater 123 from compressor 125.For example, yet this connection (structure) can also realize on other position, pass through from compressor 125 until the short connecting line of the pipeline 145 between cooler 120 and electric heater 123.Not shown adjusting device in this embodiment.
Feature of the present invention is not limited to shown example.These features for example can be with the mode combination with one another be applicable to.In addition, described device can be used similarly in multi-zone tube bundle reactor, for example in EP 1 590 076 A1, describes, and this multi-zone tube bundle reactor can be connected to the heat-carrying agent side in one or more districts.Described device is particularly suitable for using in off working state and process.This device for example can be for activation and regenerated catalyst, in addition in the time will removing the catalyst of kickback from inside reactor also for by oxidation technology, on purpose making catalyst deactivation, or for calcine technology.
Claims (11)
1. one kind for by the register of temperature adjustment gas regulation for the temperature of the tube bundle reactor of catalytic reaction, wherein said tube bundle reactor comprises a catalyst case and in abutting connection with described catalyst case but the heat-carrying agent chamber separated with described catalyst case, wherein said register can be connected with the heat-carrying agent outlet is mobile with the heat-carrying agent entrance of described heat-carrying agent chamber, described temperature adjustment gas flow is crossed register and the heat-carrying agent chamber in loop, and described register comprises:
Compressed Gas feedway (125),
For the heater of described temperature adjustment gas,
For the conveying device of described temperature adjustment gas,
It is characterized in that, it is upper and can be transported to different reactor assemblies as register movably that described register is arranged on transportable framework (139).
2. register according to claim 1, is characterized in that, described Compressed Gas feedway has compressor.
3. register according to claim 1 and 2, is characterized in that, described temperature adjustment gas (132) has the pressure in the scope of 3bar to 100bar.
4. register according to claim 1 and 2, it is characterized in that, described register has two and exports the connecting line on (137) be used to heat-carrying agent entrance (138) or the heat-carrying agent that is connected to described heat-carrying agent chamber (108), and at least one in described connecting line has the elasticity middleware.
5. register according to claim 4, is characterized in that, described elasticity middleware have be used to absorb internal pressure, adjustable tension force unloading section.
6. register according to claim 1 and 2, is characterized in that, described temperature adjustment gas (132) comprises air, nitrogen, carbon dioxide, water vapour or their mixture.
7. register according to claim 1 and 2, is characterized in that, described register comprises a cooling device for cooling described temperature adjustment gas (132), and described cooling device is designed to: water is directly sprayed in the temperature adjustment gas return path.
8. register according to claim 1 and 2, is characterized in that, described register comprises the adjusting device be used to the temperature and pressure of regulating described temperature adjustment gas (132).
9. one kind for regulating the method for the temperature of the tube bundle reactor (100) of catalytic reaction by temperature adjustment gas (132), wherein said tube bundle reactor (100) comprises a catalyst case (103) and in abutting connection with described catalyst case but the heat-carrying agent chamber (108) separated with described catalyst case, described heat-carrying agent chamber (108) is the part in heat-carrying agent loop, guiding described temperature adjustment gas (132) in described heat-carrying agent loop, described method comprises the steps:
A) prepare to be transported to tube bundle reactor (100) according to the described register of any one in claim 1 to 8 (102) and by described register (102);
B) register (102) is received in described heat-carrying agent loop;
C) with given pressure, fill described heat-carrying agent loop with described temperature adjustment gas (132);
D) make described temperature adjustment gas (132) circulation.
10. method according to claim 9, it is characterized in that, in order to regulate and control the catalyst inserts in described tube bundle reactor (100), the heat-carrying agent loop of described tube bundle reactor is flow through by heat-carrying agent (109) liquid or the part evaporation in the production phase, during step d), carry out following step:
E) temperature of described temperature adjustment gas (132) is increased to the initial temperature of regulation process;
F) guiding regulation and control gases (131) are by the catalyst inserts.
11. according to the described method of claim 9 or 10, it is characterized in that, transport described register (102) after the temperature adjustment process finish.
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| Application Number | Priority Date | Filing Date | Title |
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| DE201010014642 DE102010014642B4 (en) | 2010-04-12 | 2010-04-12 | Temperature control device and method for controlling the temperature of a tube bundle reactor |
| DE102010014642.0 | 2010-04-12 |
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| CN102211003A CN102211003A (en) | 2011-10-12 |
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| GB2561898A (en) * | 2017-04-28 | 2018-10-31 | Mexichem Fluor Sa De Cv | Improvements in or relating to propellant conditioning assemblies |
| CN108097175A (en) * | 2018-01-31 | 2018-06-01 | 新疆美克化工股份有限公司 | Formaldehyde catalyst contrast experiment's self-balancing consersion unit |
| DE102018113735A1 (en) * | 2018-06-08 | 2019-12-12 | Man Energy Solutions Se | Process, tube bundle reactor and reactor system for carrying out catalytic gas phase reactions |
| CN112588210A (en) * | 2021-01-15 | 2021-04-02 | 西安航天华威化工生物工程有限公司 | Benzoic anhydride reaction device capable of producing 8 ten thousand tons each year |
| CN113499740B (en) * | 2021-08-06 | 2023-03-10 | 宁波巨化化工科技有限公司 | Method and device for reducing difference and controlling temperature of gas-phase fixed bed circulating reactor |
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| BE795180A (en) | 1972-02-16 | 1973-05-29 | Deggendorfer Werft Eisenbau | COOLING GROUP INTENDED FOR EQUIPMENT FOR PERFORMING EXOTHERMIC CHEMICAL REACTIONS |
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| US7118917B2 (en) * | 2001-03-07 | 2006-10-10 | Symyx Technologies, Inc. | Parallel flow reactor having improved thermal control |
| EP1569745B1 (en) | 2002-12-12 | 2019-03-20 | MAN Energy Solutions SE | Shell-and-tube type reactor for catalytic gas phase reactions |
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| US8431507B2 (en) | 2008-03-28 | 2013-04-30 | Shell Oil Company | Process for regenerating a catalyst |
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| DE3439176A1 (en) * | 1984-10-25 | 1986-04-30 | Linde Ag, 6200 Wiesbaden | Process and reactor for carrying out an endothermic reaction |
| CN1561257A (en) * | 2002-07-10 | 2005-01-05 | Lg化学株式会社 | Catalytic oxidation reactor with enhanced heat exchanging system |
| CN1708350A (en) * | 2002-12-12 | 2005-12-14 | 曼德韦有限公司 | Jacketed tube reactor comprising a bypass line for the heat transfer medium |
| CN101180116A (en) * | 2005-05-31 | 2008-05-14 | 埃克森美孚化学专利公司 | Reactor temperature control |
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| CN102211003A (en) | 2011-10-12 |
| DE102010014642B4 (en) | 2014-08-07 |
| DE102010014642A1 (en) | 2011-10-13 |
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