EP3233271A1 - Method for carrying out a chemical synthesis and synthesis reactor - Google Patents
Method for carrying out a chemical synthesis and synthesis reactorInfo
- Publication number
- EP3233271A1 EP3233271A1 EP16702887.7A EP16702887A EP3233271A1 EP 3233271 A1 EP3233271 A1 EP 3233271A1 EP 16702887 A EP16702887 A EP 16702887A EP 3233271 A1 EP3233271 A1 EP 3233271A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- reaction
- synthesis
- reaction chamber
- chambers
- reactor
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
- 238000003786 synthesis reaction Methods 0.000 title claims abstract description 69
- 230000015572 biosynthetic process Effects 0.000 title claims abstract description 58
- 238000000034 method Methods 0.000 title claims abstract description 20
- 238000006243 chemical reaction Methods 0.000 claims abstract description 149
- 238000007599 discharging Methods 0.000 claims abstract 2
- 239000007788 liquid Substances 0.000 claims description 24
- 239000003054 catalyst Substances 0.000 claims description 17
- 239000000463 material Substances 0.000 claims description 3
- 239000000376 reactant Substances 0.000 abstract description 9
- 239000007789 gas Substances 0.000 description 19
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 15
- 239000012071 phase Substances 0.000 description 11
- 239000007791 liquid phase Substances 0.000 description 6
- 239000003921 oil Substances 0.000 description 6
- 238000000926 separation method Methods 0.000 description 6
- 239000007858 starting material Substances 0.000 description 6
- 239000000126 substance Substances 0.000 description 6
- 238000001816 cooling Methods 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- 238000009833 condensation Methods 0.000 description 4
- 230000005494 condensation Effects 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 239000002245 particle Substances 0.000 description 4
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 230000008901 benefit Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000001257 hydrogen Substances 0.000 description 3
- 229910052739 hydrogen Inorganic materials 0.000 description 3
- 238000002156 mixing Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 229910002091 carbon monoxide Inorganic materials 0.000 description 2
- 239000000306 component Substances 0.000 description 2
- 230000017525 heat dissipation Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 239000002002 slurry Substances 0.000 description 2
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 2
- 241001026509 Kata Species 0.000 description 1
- 241000158147 Sator Species 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 239000003990 capacitor Substances 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 230000004907 flux Effects 0.000 description 1
- 230000004927 fusion Effects 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000010348 incorporation Methods 0.000 description 1
- 239000011261 inert gas Substances 0.000 description 1
- 229940057952 methanol Drugs 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000005580 one pot reaction Methods 0.000 description 1
- 230000021715 photosynthesis, light harvesting Effects 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000006557 surface reaction Methods 0.000 description 1
- 230000007306 turnover Effects 0.000 description 1
- 238000009736 wetting Methods 0.000 description 1
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.
Landscapes
- 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)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102015202680.9A DE102015202680A1 (en) | 2015-02-13 | 2015-02-13 | Process for carrying out a chemical synthesis and synthesis reactor |
PCT/EP2016/051046 WO2016128187A1 (en) | 2015-02-13 | 2016-01-20 | Method for carrying out a chemical synthesis and synthesis reactor |
Publications (1)
Publication Number | Publication Date |
---|---|
EP3233271A1 true EP3233271A1 (en) | 2017-10-25 |
Family
ID=55300469
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP16702887.7A Withdrawn EP3233271A1 (en) | 2015-02-13 | 2016-01-20 | Method for carrying out a chemical synthesis and synthesis reactor |
Country Status (7)
Country | Link |
---|---|
US (1) | US10562003B2 (en) |
EP (1) | EP3233271A1 (en) |
CN (1) | CN107249728A (en) |
AU (1) | AU2016218191B2 (en) |
CL (1) | CL2017002036A1 (en) |
DE (1) | DE102015202680A1 (en) |
WO (1) | WO2016128187A1 (en) |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102015202680A1 (en) | 2015-02-13 | 2016-08-18 | Friedrich-Alexander-Universität Erlangen-Nürnberg | Process for carrying out a chemical synthesis and synthesis reactor |
EP3556451B1 (en) * | 2018-04-20 | 2020-06-03 | Siemens Aktiengesellschaft | Method for operating a reactor system |
DE102019201172A1 (en) * | 2019-01-30 | 2020-07-30 | Siemens Aktiengesellschaft | Reactor cascade and method for operating a reactor cascade |
EP4059596A1 (en) | 2021-03-16 | 2022-09-21 | Paul Scherrer Institut | Process for methanol production from co2 with water removal |
Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2000077128A1 (en) * | 1999-06-09 | 2000-12-21 | Technische Universität München Lehrstuhl Für Thermische Kraftanlagen | Device for the gasification of carbonaceous feedstock |
WO2014116203A1 (en) * | 2013-01-22 | 2014-07-31 | Thermochem Recovery International, Inc. | Integrated two-stage thermochemical heat pipe reactor having a partitioned vessel |
Family Cites Families (19)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE3031477C2 (en) * | 1980-08-21 | 1986-09-18 | Saarbergwerke AG, 6600 Saarbrücken | Process for hydrogenating coal |
GB2249547A (en) * | 1990-10-29 | 1992-05-13 | Shell Int Research | Process for the production of methanol |
NL1003026C2 (en) * | 1996-05-03 | 1997-11-06 | Tno | Reactor for conducting gas phase / liquid phase / solid phase reactions, as well as a method for conducting such reactions using this reactor. |
US6537352B2 (en) * | 1996-10-30 | 2003-03-25 | Idatech, Llc | Hydrogen purification membranes, components and fuel processing systems containing the same |
US5925685A (en) * | 1996-11-18 | 1999-07-20 | Catalytic Distillation Technologies | Method for carrying out heterogeneous catalysis |
CN1194070C (en) * | 2003-05-08 | 2005-03-23 | 中国石化集团洛阳石油化工工程公司 | Petroleum atmospheric vacuum distillation process and unit |
DK1707259T3 (en) | 2005-04-01 | 2018-09-03 | Casale Sa | Process for heterogeneous synthesis of chemical compounds |
US7384985B2 (en) * | 2005-07-20 | 2008-06-10 | Exxonmobil Chemical Patents Inc. | Process for producing methanol |
DE102006050717A1 (en) * | 2005-10-24 | 2007-04-26 | Chemetall Gmbh | Preparation of functionalized five-membered ring heterocycles, useful in preparation of pharmaceuticals and plant-protection agents, by reaction with electrophile, hydrogen acceptor and alkali metal |
US7982046B2 (en) | 2005-10-24 | 2011-07-19 | Chemetall Gmbh | Method for the production of functionalized five-ring heterocycles, and use thereof |
US20100324157A1 (en) * | 2006-12-29 | 2010-12-23 | Bauman Richard F | High throughput fischer-tropsch catalytic process development method |
WO2009075692A2 (en) | 2007-05-14 | 2009-06-18 | Invista Technologies S.A.R.L. | High efficiency reactor and process |
PL2249958T3 (en) | 2008-02-25 | 2012-01-31 | Haldor Topsoe As | Reactor for the preparation of methanol |
WO2010083457A1 (en) * | 2009-01-15 | 2010-07-22 | Enventix, Inc. | System and method for providing an integrated reactor |
DE102009032524B3 (en) * | 2009-07-10 | 2011-02-03 | Highterm Research Gmbh | Reactor for producing a product gas by allothermic gasification of carbonaceous feedstocks |
EP2450100A1 (en) | 2010-10-22 | 2012-05-09 | Methanol Casale S.A. | Process and plant for the production of methanol with isothermal catalytic beds |
US8984992B2 (en) * | 2012-10-25 | 2015-03-24 | Abb Technology Ltd. | Socket with nut or bolt holding structure |
US20160030926A1 (en) * | 2013-03-15 | 2016-02-04 | Seerstone Llc | Compositions of Matter Comprising Nanocatalyst Structures, Systems Comprising Nanocatalyst Structures, and Related Methods |
DE102015202680A1 (en) | 2015-02-13 | 2016-08-18 | Friedrich-Alexander-Universität Erlangen-Nürnberg | Process for carrying out a chemical synthesis and synthesis reactor |
-
2015
- 2015-02-13 DE DE102015202680.9A patent/DE102015202680A1/en not_active Withdrawn
-
2016
- 2016-01-20 CN CN201680010032.7A patent/CN107249728A/en active Pending
- 2016-01-20 EP EP16702887.7A patent/EP3233271A1/en not_active Withdrawn
- 2016-01-20 AU AU2016218191A patent/AU2016218191B2/en not_active Ceased
- 2016-01-20 US US15/550,114 patent/US10562003B2/en not_active Expired - Fee Related
- 2016-01-20 WO PCT/EP2016/051046 patent/WO2016128187A1/en active Application Filing
-
2017
- 2017-08-09 CL CL2017002036A patent/CL2017002036A1/en unknown
Patent Citations (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2000077128A1 (en) * | 1999-06-09 | 2000-12-21 | Technische Universität München Lehrstuhl Für Thermische Kraftanlagen | Device for the gasification of carbonaceous feedstock |
WO2014116203A1 (en) * | 2013-01-22 | 2014-07-31 | Thermochem Recovery International, Inc. | Integrated two-stage thermochemical heat pipe reactor having a partitioned vessel |
Non-Patent Citations (1)
Title |
---|
See also references of WO2016128187A1 * |
Also Published As
Publication number | Publication date |
---|---|
WO2016128187A1 (en) | 2016-08-18 |
US20180028996A1 (en) | 2018-02-01 |
CN107249728A (en) | 2017-10-13 |
US10562003B2 (en) | 2020-02-18 |
DE102015202680A1 (en) | 2016-08-18 |
CL2017002036A1 (en) | 2018-02-09 |
AU2016218191B2 (en) | 2018-04-19 |
AU2016218191A1 (en) | 2017-08-24 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
DE60025124T2 (en) | Method and apparatus for hydrogen production by reforming | |
DE69715661T2 (en) | METHOD AND SYSTEM FOR PRODUCING METHANOL | |
DE69714855T2 (en) | SHIFT CONVERTER | |
WO2016128187A1 (en) | Method for carrying out a chemical synthesis and synthesis reactor | |
WO2000030743A1 (en) | Reactor for carrying out gas-liquid, liquid-liquid or gas-liquid-solid chemical reactions | |
DE102004028200B3 (en) | Method for carrying out heterogeneous catalytic exothermic gas phase reactions for the synthesis of methanol | |
DE3019625A1 (en) | METHOD AND REACTOR FOR CARRYING OUT EXOTHERMAL OR. ENDOTHERMAL CATALYTIC REACTIONS IN GAS PHASE AT HIGH PRESSURE | |
DE69111820T2 (en) | HIGH CONVERSION AMMONIA SYNTHESIS. | |
DE2742204A1 (en) | REACTOR FOR CATALYTIC EXOTHERMAL REACTIONS | |
WO2016128188A1 (en) | Method for carrying out a chemical synthesis | |
EP1461139A1 (en) | Method for purifying off-gases from a melamine-producing installation | |
EP3802748A1 (en) | Method, tube bundle reactor and reactor system for carrying out catalytic gas phase reactions | |
WO2014009346A1 (en) | Device and method for producing phosgene | |
EP3115336B2 (en) | Method and plant for the cooling of synthesis gas | |
EP3416916B1 (en) | Nh3 synthesis configuration for large-scale installations | |
WO2019233674A1 (en) | Method and reactor system for carrying out catalytic gas phase reactions | |
DE19833644A1 (en) | Reactor unit in a system for generating a hydrogen-rich gas from a liquid raw fuel | |
EP4065514A1 (en) | Process and plant for preparation of ammonia | |
EP3124433A1 (en) | Installation and method for cooling synthesis gas | |
EP1670746B1 (en) | Method for controlling the reactor admission temperature during the production of methylamine | |
EP3894062A1 (en) | Reactor cascade and method for operating a reactor cascade | |
BE1030481B1 (en) | Ammonia converter for fluctuating partial load operation | |
WO2019234208A1 (en) | Method and device for carrying out a water-gas shift reactor | |
DE2339759A1 (en) | PROCESS FOR PRODUCING A HYDROGEN-RICH GAS | |
EP4327930A1 (en) | Multi-stage reactor for carrying out exothermic equilibrium reactions |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE INTERNATIONAL PUBLICATION HAS BEEN MADE |
|
PUAI | Public reference made under article 153(3) epc to a published international application that has entered the european phase |
Free format text: ORIGINAL CODE: 0009012 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: REQUEST FOR EXAMINATION WAS MADE |
|
17P | Request for examination filed |
Effective date: 20170720 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR |
|
AX | Request for extension of the european patent |
Extension state: BA ME |
|
DAV | Request for validation of the european patent (deleted) | ||
DAX | Request for extension of the european patent (deleted) | ||
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: EXAMINATION IS IN PROGRESS |
|
17Q | First examination report despatched |
Effective date: 20190517 |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: EXAMINATION IS IN PROGRESS |
|
STAA | Information on the status of an ep patent application or granted ep patent |
Free format text: STATUS: THE APPLICATION IS DEEMED TO BE WITHDRAWN |
|
18D | Application deemed to be withdrawn |
Effective date: 20210803 |