Classifications

• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/02—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
  • B01J8/04—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 the fluid passing successively through two or more beds
  • B01J8/0446—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical
  • B01J8/0449—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds
  • B01J8/0453—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 the fluid passing successively through two or more beds the flow within the beds being predominantly vertical in two or more cylindrical beds the beds being superimposed one above the other
• • 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
• • 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
  • B01J12/00—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor
  • B01J12/007—Chemical processes in general for reacting gaseous media with gaseous media; Apparatus specially adapted therefor in the presence of catalytically active bodies, e.g. porous plates
• • 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
  • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J19/24—Stationary reactors without moving elements inside
  • B01J19/245—Stationary reactors without moving elements inside placed in series
• • 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
  • B01J8/04—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 the fluid passing successively through two or more beds
  • B01J8/0496—Heating or cooling the reactor
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
  • B01J8/1836—Heating and cooling the reactor
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
  • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
  • B01J8/20—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium
  • B01J8/22—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles with liquid as a fluidising medium gas being introduced into the liquid
  • B01J8/222—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 in the presence of a rotating device only
• • 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
  • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
  • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
• • 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
  • B01J8/24—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique
  • B01J8/26—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations
  • B01J8/28—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles according to "fluidised-bed" technique with two or more fluidised beds, e.g. reactor and regeneration installations the one above the other
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
• • C—CHEMISTRY; METALLURGY
  • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
  • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
  • C10G2/00—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon
  • C10G2/30—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen
  • C10G2/32—Production of liquid hydrocarbon mixtures of undefined composition from oxides of carbon from carbon monoxide with hydrogen with the use of catalysts
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
  • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
  • B01J2208/00008—Controlling the process
  • B01J2208/00017—Controlling the temperature
  • B01J2208/00106—Controlling the temperature by indirect heat exchange
  • B01J2208/00115—Controlling the temperature by indirect heat exchange with heat exchange elements inside the bed of solid particles
  • B01J2208/00132—Tubes
• • 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
• • 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
  • B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
  • B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
• • 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
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00051—Controlling the temperature
  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00076—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements inside the reactor
  • B01J2219/00081—Tubes
• • 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
  • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
  • B01J2219/00049—Controlling or regulating processes
  • B01J2219/00051—Controlling the temperature
  • B01J2219/00074—Controlling the temperature by indirect heating or cooling employing heat exchange fluids
  • B01J2219/00087—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor
  • B01J2219/00103—Controlling the temperature by indirect heating or cooling employing heat exchange fluids with heat exchange elements outside the reactor in a heat exchanger separate from the reactor
• • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
  • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
  • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
  • Y02P20/00—Technologies relating to chemical industry
  • Y02P20/50—Improvements relating to the production of bulk chemicals
  • Y02P20/582—Recycling of unreacted starting or intermediate materials

Definitions

• Recirculation unit are compensated. This is usually operated at high temperatures and leads to high costs. In addition, due to recirculation inert and foreign gases accumulate in the circulation, which leads to negative effects on the reaction. With recirculation, therefore, a small amount of recirculation gas is continuously withdrawn, which results in losses of starting materials and thus lower conversion efficiencies. Furthermore, the recirculated amount of gas leads to a high gas volume flow through the reactor, which increases the size and thus the cost of the reactor.
• the invention is therefore based on the object to provide a method for carrying out a chemical synthesis in which over the prior art with the same or reduced energy consumption, a higher degree of conversion of the reactants can be achieved.
• the object is achieved in a method for carrying out a chemical synthesis according to claim 1 and in a synthesis reactor according to claim 8.
• the method according to the invention for carrying out a chemical synthesis comprises the following steps:
• a Syntheseedukt which may comprise one or more compo nents ⁇ introduced into a reaction chamber.
• a pressure PI prevails.
• At least one synthesis product from the synthesis educt is formed in the reaction chamber. Furthermore, this synthetic product and not rea during the reaction ⁇ gêts, so unreacted Syntheseedukt is discharged from the reaction chamber ⁇ . In addition, outside the Reakti ⁇ onshunt followed by a separation of the synthesis product from the
• At least one heat pipe also called a heat pipe, is provided, which connects the two reaction chambers to one another.
• reaction heat which occurs in exothermic reactions, is exchanged between the reaction chambers.
• a heat exchange can also take place in endothermic reactions via the heat pipe.
• the heat pipe leaves while in one embodiment of the invention, one of the reaction chambers so that one end of the heat pipe is present outside at least one of the reaction chambers, and at this led out of the reaction chambers end occurs a thermal energy dissipation, for example by a entspre ⁇ sponding cooling device (in an exothermic reaction) or optionally a heating device (for endothermic Reakti ⁇ ons Adjust).
• Particulate catalyst supplied which is preferably present in this finely dispersed.
• the catalyst supports the reaction of synthesis educts to synthesis products by surface reactions and in particular influences the reaction rate.
• a non-polar liquid such as oil, in particular a heat transfer oil, has been found to be expedient ⁇ .
• the reaction can also be carried out in a fixed bed reactor using a catalyst.
• the reaction of Syntheseedukt to the synthesis product takes place here in the gas phase.
• This reaction procedure has the advantage over the reaction procedure in a carrier liquid that the reactor construction becomes simpler.
• the temperature regulation is technologically more complex and difficult to control, in particular through the use of heat pipes.
• the reaction in a fluidized bed reactor also in the use of a catalyst take place, wherein a bed containing at least partially Katalysatorma ⁇ terial is flowed from below with a gas stream and is fluidized.
• a further component of the invention is a synthesis reactor according to patent claim 8.
• This synthesis reactor has at least two reaction chambers, wherein at least one first reaction chamber has at least one supply device for a synthesis educt or, depending on the reaction, several synthesis educts.
• the first reaction chamber with a second reaction chamber via a supply line is connected to each other, wherein at the feed line a
• Product separation device is arranged at which at least one synthesis product, which is formed in the first Discussskam ⁇ mer from the Syntheseedukt, from a mixture of unreacted Syntheseedukt and synthesis product sketchschi ⁇ det.
• a higher pressure is present in the first reaction chamber than in the second reaction chamber.
• the Synthe ⁇ sereaktor is equipped with at least one heat pipe, which connects the two reaction chambers with each other and through which is effected the exchange of heat of reaction between the reaction chambers.
• a supply or removal of heat energy can be applied to this projecting out of the reaction chambers end, whereby the state already described is reached again that the reaction chambers are connected nearly isothermal MITEI ⁇ Nander, ie in the reaction chambers despite There occurring exothermic or endothermic reaction is almost the same reaction temperature.
• This is expedient for the individual reactions in the reaction chambers to proceed almost uniformly, thus permitting an advantageous reaction control in the individual reaction chambers.
• Figure 1 is a schematic representation of a multi-stage
• FIG. 2 shows a detail of a reactor from FIG. 1 with a reaction chamber and a more detailed depiction of a product separation device between two reactor chambers.
• the synthesis reactor 20 comprises, in particular when, as shown in Figure 1, is constructed stacked manner, in ⁇ is nem lower region, a supply device 3 for synthesis starting materials 2.
• the Syntheseedukte 2 are thus performed in a first reaction chamber 4, in which already a carrier liquid ⁇ ness 16 in the form of an oil which is a nonpolar liquid is present.
• a carrier liquid ⁇ ness 16 in the form of an oil which is a nonpolar liquid is present.
• hydrogen and carbon dioxide and / or carbon monoxide are introduced here as starting material, with a reaction taking place in methanol.
• a particulate, finely dispersed present catalyst not shown here, is further introduced.
• the Syntheseedukte 2 can react to the methanol in this case in particular at the Kata ⁇ lysatorober Formation.
• the gaseous educts 2 can, after they are introduced into the reactor chamber 4, partially dissolve in the carrier liquid 16. The reaction then takes place on the catalyst particles, in particular on its surface. Through a backdift fusion in the gas phase, the products accumulate there and can be deducted above the liquid phase. In the reaction chamber, a pressure of about 90 bar prevails.
• the temperature is preferably in a range between 150 ° C and 350 ° C, in this example at 250 ° C.
• reaction stage in the next reaction chamber 10 This stage of the reaction in the reaction chamber 10 is operated at a ge ⁇ ringeren reaction pressure than the reaction step in the reaction chamber 4 to ermögli overflow of the remaining Syntheseedukte without the installation of a pressure increasing means such as a blower or a compressor ⁇ chen.
• the pressure difference between the reaction stages must be chosen so that pressure losses are compensated for overflow from stage 1 in the reaction chamber 4 to stage 2 in the reaction chamber 10.
• a pressure difference of about 5 bar from one of a reaction chamber to the other has been found to be advantageous.
• a valve 24 should be used.
• stage 2 in the reaction chamber 10 the synthesis reactants 2 can then react again until the chemical equilibrium.
• the structure of the reactor 20 is repeated step by step, so many steps in the form of reaction chambers 10 are used, as is necessary and economical for the most complete implementation of Synthe- seedukte 2.
• the reaction chambers 10 may be optionally smaller dimensioned to stage by stage. The remaining at the last reaction stage
• Reactant gas contains inert gases and foreign and can be withdrawn as a so- ⁇ -called purge gas 26th Alternatively, a return of this gas to the reaction input at the inlet is also possible. possibly after a successful treatment possible.
• a heat pipe 12 is in the simplest case a closed pipe in which a heat transfer medium is in the two-phase region. Is fed at any point of the heat pipe heat, there is an evaporation of the nickelträ ⁇ transfer medium. The steam then flows to the colder end and condenses there again. Through this process, very high heat flows in a compact design can be transferred almost isothermally.
• the backflow of the liquid phase can be done solely by gravity, if the evaporation takes place at the lower end of the tube 12 and the condensation above. Furthermore, the return of the liquid phase can be ensured by capillary effects, for example by the installation of wire mesh or wicks.
• the heat pipes in the presented reactor 20 are advantageously provided with internals not shown here, which make a uniform wetting of the inner wall with liquid phase possible.
• internals not shown here, which make a uniform wetting of the inner wall with liquid phase possible.
• evaporation but also condensation take place. Evaporation always takes place in the hottest area of the heat pipe 12 and condensation then in the coldest area. Therefore, the concept allows a very effective and flexible heat exchange between the individual reaction chambers 4, 10.
• a nearly isothermal reaction is possible along the entire synthesis reactor 20.
• the various stages in the form of the reaction chambers 4 and 10 are operated at different pressures (pi, p2 ... p n ) but at a nearly constant temperature.
• the heat pipes 12 can be led out of the synthesis reactor 20 at the upper or at the lower end. As a result, heat supply or heat dissipation is possible at this end of the heat pipe 12 led out of the synthesis reactor 20.
• heat supply or heat dissipation is possible at this end of the heat pipe 12 led out of the synthesis reactor 20.
• In exothermic reactions is generally a heat dissipation in the form of cooling necessary. Cooling at the end of the heat pipe it ⁇ enables thus a constant temperature along the reac tors ⁇ .
• the heat will merohre 12 preferably with water as a heat transfer medium Betrie ⁇ ben. Water in this temperature range enables good heat transfer capabilities and acceptable vapor pressures and so ⁇ 12 with an acceptable wall thickness of the tubes or the heat ⁇ Al ternatively, other heat transfer media or mixtures multifuel can be used.
• the individual reaction chambers can be constructed according to different concepts.
• a catalyst may be introduced in a fixed bed of bed or the heat pipes may be provided with a catalyst structure on the surface and the reaction then takes place in the gas phase on a Kataly ⁇ capacitor.
• the reaction chambers can be designed as fluidized beds. Here, a bed is we ⁇ iquess partially flows reasonable of catalyst material from the bottom and fluidized. The reaction then takes place again on the catalyst surface in the gas phase.
• the individual reaction chambers 4, 10 are designed as liquid-phase reactors, so-called slurry reactors.
• catalyst particles are finely distributed in a carrier liquid 16 introduced ⁇ .
• the gaseous Syntheseedukte 2 for example for the production of methanol, the reactants H 2 and CO 2 / CO, are introduced into the reaction chamber 4, and it finds a researcherss- least partially solve the Syntheseedukte 2 in the Anlagenflüs ⁇ stechnik 16 instead.
• the reaction then takes place on the surfaces of the catalyst particles.
• FIG. 2 also illustrates that the reaction chamber 4, which is traversed by heat pipes 12, does not necessarily have to connect directly to the next reaction chamber 10.
• the individual reaction chambers 4 and 10 may also be arranged sequentially spaced from each other, if this is predetermined by the technical structure, appropriate.

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• Chemical & Material Sciences (AREA)
• Organic Chemistry (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Engineering & Computer Science (AREA)
• Combustion & Propulsion (AREA)
• Oil, Petroleum & Natural Gas (AREA)
• General Chemical & Material Sciences (AREA)
• Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)

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• 2015
  • 2015-02-13 DE DE102015202680.9A patent/DE102015202680A1/de not_active Withdrawn
• 2016
  • 2016-01-20 US US15/550,114 patent/US10562003B2/en not_active Expired - Fee Related
  • 2016-01-20 EP EP16702887.7A patent/EP3233271A1/de not_active Withdrawn
  • 2016-01-20 AU AU2016218191A patent/AU2016218191B2/en not_active Ceased
  • 2016-01-20 WO PCT/EP2016/051046 patent/WO2016128187A1/de active Application Filing
  • 2016-01-20 CN CN201680010032.7A patent/CN107249728A/zh active Pending
• 2017
  • 2017-08-09 CL CL2017002036A patent/CL2017002036A1/es unknown

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