EP2346597A1 - Method for manufacturing a product gas and generating steam, and modular product gas-steam reactor for carrying out said method - Google Patents
Method for manufacturing a product gas and generating steam, and modular product gas-steam reactor for carrying out said methodInfo
- Publication number
- EP2346597A1 EP2346597A1 EP09748066A EP09748066A EP2346597A1 EP 2346597 A1 EP2346597 A1 EP 2346597A1 EP 09748066 A EP09748066 A EP 09748066A EP 09748066 A EP09748066 A EP 09748066A EP 2346597 A1 EP2346597 A1 EP 2346597A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- reaction tube
- gas
- temperature
- catalyst
- reactor according
- 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- Withdrawn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
- 238000000034 method Methods 0.000 title claims abstract description 40
- 238000004519 manufacturing process Methods 0.000 title abstract description 6
- 239000007789 gas Substances 0.000 claims abstract description 84
- 239000003054 catalyst Substances 0.000 claims abstract description 43
- 239000002918 waste heat Substances 0.000 claims abstract description 10
- 238000001816 cooling Methods 0.000 claims abstract description 9
- 238000010438 heat treatment Methods 0.000 claims abstract description 8
- 230000001105 regulatory effect Effects 0.000 claims abstract 2
- 238000006243 chemical reaction Methods 0.000 claims description 107
- 238000012546 transfer Methods 0.000 claims description 19
- 239000000376 reactant Substances 0.000 claims description 10
- 230000008569 process Effects 0.000 claims description 8
- 230000005484 gravity Effects 0.000 claims description 6
- 238000009413 insulation Methods 0.000 claims description 5
- 239000007788 liquid Substances 0.000 claims description 5
- 239000002245 particle Substances 0.000 claims description 4
- NINIDFKCEFEMDL-UHFFFAOYSA-N Sulfur Chemical compound [S] NINIDFKCEFEMDL-UHFFFAOYSA-N 0.000 claims description 3
- 230000004913 activation Effects 0.000 claims description 3
- 230000015572 biosynthetic process Effects 0.000 claims description 3
- 229910052717 sulfur Inorganic materials 0.000 claims description 3
- 239000011593 sulfur Substances 0.000 claims description 3
- 238000003786 synthesis reaction Methods 0.000 claims description 3
- PXHVJJICTQNCMI-UHFFFAOYSA-N Nickel Chemical compound [Ni] PXHVJJICTQNCMI-UHFFFAOYSA-N 0.000 claims 4
- 229910017052 cobalt Inorganic materials 0.000 claims 2
- 239000010941 cobalt Substances 0.000 claims 2
- GUTLYIVDDKVIGB-UHFFFAOYSA-N cobalt atom Chemical compound [Co] GUTLYIVDDKVIGB-UHFFFAOYSA-N 0.000 claims 2
- 229910052759 nickel Inorganic materials 0.000 claims 2
- 229910000510 noble metal Inorganic materials 0.000 claims 2
- 230000000737 periodic effect Effects 0.000 claims 2
- 230000001276 controlling effect Effects 0.000 claims 1
- 238000007599 discharging Methods 0.000 claims 1
- 239000007787 solid Substances 0.000 claims 1
- 238000001179 sorption measurement Methods 0.000 claims 1
- 230000033228 biological regulation Effects 0.000 abstract description 3
- 230000008901 benefit Effects 0.000 description 4
- 238000001704 evaporation Methods 0.000 description 4
- 230000008020 evaporation Effects 0.000 description 4
- 238000012423 maintenance Methods 0.000 description 3
- 238000000746 purification Methods 0.000 description 3
- 238000000926 separation method Methods 0.000 description 3
- 230000008859 change Effects 0.000 description 2
- 230000010354 integration Effects 0.000 description 2
- 230000008439 repair process Effects 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 230000003213 activating effect Effects 0.000 description 1
- 230000006978 adaptation Effects 0.000 description 1
- 238000009529 body temperature measurement Methods 0.000 description 1
- 239000013590 bulk material Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 229910052729 chemical element Inorganic materials 0.000 description 1
- 150000001805 chlorine compounds Chemical class 0.000 description 1
- 230000003750 conditioning effect Effects 0.000 description 1
- 239000000470 constituent Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000011109 contamination Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 125000000753 cycloalkyl group Chemical group 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 230000017525 heat dissipation Effects 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000002386 leaching Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 230000007363 regulatory process Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 230000002195 synergetic effect Effects 0.000 description 1
- 238000011144 upstream manufacturing 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
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
- B01J8/003—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor in a downward flow
-
- 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
- B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
- B01J8/002—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor with a moving instrument
-
- 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
- B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
- B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
-
- 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
- B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
- B01J2208/00212—Plates; Jackets; Cylinders
-
- 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
- B01J2208/00477—Controlling the temperature by thermal insulation means
- B01J2208/00495—Controlling the temperature by thermal insulation means using insulating materials or refractories
-
- 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
- B01J2208/0053—Controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
-
- 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
- B01J2219/00002—Chemical plants
- B01J2219/00027—Process aspects
- B01J2219/00038—Processes in parallel
Definitions
- the present invention relates to a process for the production of steam and a product gas and to a modular product gas-steam reactor for carrying out the process according to the preamble of claims 1 and 12, respectively.
- the method according to the invention can be subdivided into a first sub-process for producing a product gas and a second sub-process for producing steam, which are coupled to one another, wherein the product gas-steam reactor according to the invention is suitable for carrying out both sub-processes simultaneously.
- a chemical-physical conversion function (eg purification) of a feedstock gas introduced into the product gas-steam reactor can be attributed to the first sub-process, and an energy utilization function of the waste heat generated during the chemical-physical conversion can be attributed to the second subprocess.
- the conversion / purification of educt gases contaminated with particles, sulfur, hydrocarbons and / or chlorine compounds is conventionally realized by a complex combination of several reactors.
- the spatial separation of the reactors reflects the functional division in which each reactor is responsible for the removal of a constituent of the impurities, e.g. As a chemical element or particle, serves from the reactant gas.
- the technical and financial burden of each of these reactors, and in particular their connection and integration into an overall plant is enormous, since the chemical reactions that take place in the individual reactors, need adequate conditions in terms of temperature and pressure; the use of such systems is therefore only economical above a certain size and a certain gas throughput.
- the temperature profile is thus a function T (x) of the temperature as a function of a location x on an abscissa parallel to the longitudinal axis of the reaction tube and subdivides this into a plurality of temperature zones, wherein optimal reaction conditions can be set in the respective temperature zones for treatment reactions of the educt gas flowing through them ,
- T (x) of the temperature as a function of a location x on an abscissa parallel to the longitudinal axis of the reaction tube and subdivides this into a plurality of temperature zones, wherein optimal reaction conditions can be set in the respective temperature zones for treatment reactions of the educt gas flowing through them .
- the temperature profile is generated according to the invention by thermal insulation, heating and / or cooling of control sections, each temperature zone can be assigned a control section. It is clear that even if the controlled temperature profile is a step function T (n), where n is the respective control section, the actual temperature profile T (x) is a differentiable function.
- the dissipated during the cooling of a control section heat is inventively supplied to a steam generating unit (second sub-function).
- n 3 according to claim 2, wherein T (1)> T (2)> T (3) is consecutive in the flow direction, the present invention is not limited thereto.
- the number of temperature zones depends on the reactions taking place in the reaction tube and is more technically than fundamentally limited.
- a regulation is made so that the composition of the product gas is determined and this composition is used as a controlled variable for temperature control and / or throughput.
- the throughput, the reactions taking place in a particular reaction tube, the heat which can be dissipated, etc. are of course not independent of one another in terms of technical physics but can and must be coordinated with one another. This opens up several ways of influencing the regulatory process, wherein, if z. B. the throughput is a variable size of a particular control section, this size is inevitably a parameter in all other control sections.
- the activation of the catalyst can according to claim 9 u. a. be carried out by the heat, which is taken from the educt gas itself, the according to claim 11 z.
- the first sub-method of the method according to the invention can thus be a subsequent step of a larger overall process in which a product gas and steam is generated from biomass.
- the mentioned bioreactor can in this case, for example, a so-called heat pipe
- the waste heat of a control section instead of the steam generating unit can be supplied to another control section.
- the waste heat of the section A of the target temperature T A to the section C of the target temperature T c , if the section B is a target temperature T B with T B ⁇ T A , Tc, so that after a temperature decrease in section B, a temperature increase in section C should again take place.
- a product gas-steam reactor is modular, comprising at least one reaction unit (module) that transmits a reaction tube and a heat transfer device through which heat is transferred from the reaction tube to the vapor generating unit.
- the modularity has decisive advantages, as already mentioned in connection with the method according to the invention.
- the first sub-processes of the present invention which take place in the individual reaction units when the product gas-steam reactor comprises at least two reaction units, may be identical or different, e.g. B. according to claim 11 of the present invention in one of the Re- reaction units, preferably synthesis gas (eg biogas) can be used as starting gas.
- synthesis gas eg biogas
- n * k control sections result in each of the reaction tubes and thus, according to the empirical formula n * k (n * k + 1) / 2 discovered by Gauss, possible connections between the control sections, ie a complex and therefore very variable network .
- the reaction units can be separately "shut down" and replaced, for example for repair or modification of its construction.
- the temperature control units may each partially enclose the reaction tube as defined in claim 13.
- the temperature control units for uniform temperature increase or decrease of the respective reaction tube section in the form of a completely surrounding the reaction tube ring are formed.
- the ring is formed divisible to facilitate mounting of the ring to the reaction tube.
- the temperature control units may each comprise temperature control elements which form a ring structure interrupted in the circumferential direction of the reaction tube.
- the temperature control device may comprise, for example, a heat conduction arrangement according to claim 14.
- the conveying of the catalyst bed can be effected essentially by gravity according to claim 15 or by means of a conveying device according to claim 18.
- gravity conveying can be controlled by the, for example obliquely from top to bottom or preferably vertically arranged reaction tube by a corresponding lock according to claim 16, for example a rotary valve or a worm drive according to claim 17, the flow rate, ie the flow rate per unit time of the catalyst ,
- a worm drive according to the invention can be used not only to control the flow rate in the case of gravity conveying, but also as a conveying device according to claim 19 of the present invention; It then takes over the promotion and at the same time regulates the throughput of the amount of catalyst produced.
- the spatial arrangement of the reaction tube is arbitrary.
- any other conveyor direction which is suitable for the controlled transport of free-flowing bulk material.
- a conveyor can be used in addition, for example, with a slight inclination of the reaction tube to overcome frictional resistance.
- the lock is arranged at the second end and "the catalyst bed sits on it, its speed is proportional to the throughput and the conveying speed of the catalyst bed in the reaction tube, so that throughput or conveying speed can be used as a controlled variable.
- the sluice is arranged at the first end, its rate of rotation determines the delivery rate, the movement behind the sluice (ie in the reaction tube) of the catalyst charge is determined by the law of falling and is unchangeable.
- the reaction tube which is not fixed in shape and orientation in space according to claim 12, that is, for example, as a whole straight or circular, is formed or composed of straight and curved sections.
- this possibility basically applies both to gravity conveying and to conveying by means of a conveying device.
- the conveying force exerted by the gravity of the catalyst located in vertical or obliquely from top to bottom extending sections of the reaction tube must be sufficient to overcome horizontal or less steep sections or the reaction tube or friction.
- the promotion can advantageously be facilitated by turbulence of the catalyst bed to a moving fluidized bed.
- the reactor according to claim 21 of the present invention comprises a gas detector which detects the conditioning efficiency by determining the composition of the product gas serving as a controlled variable. Subsequently, for example, the measured composition (controlled variable) with a desired size (Reference variable) compared and the control difference are fed to a controller which controls, for example, a potentiometer as a control device for changing the current of the temperature control device or its temperature control units. As a load disturbance variable, the flow velocity of the educt gas can be integrated into the control loop.
- composition of the product gas can be compared with a desired value and the control difference can change a reference variable of a temperature control, ie a separate temperature control with a corresponding temperature measurement etc. should be provided.
- Decisive for the desired composition of the product gas is in each case an interaction of the flow rate of the educt gas, the state and throughput of the catalyst, temperature ranges and not least the composition or type of contamination of the educt gas.
- a temperature gradient in the flow direction of the educt gas which can be approximated depending on the size of the individual temperature control units, for example, to a linear, wherein the highest temperature in the environment of Eduktgaszu entry the Reaction tube prevails.
- the variable "temperature zone” has the dimension [length] (along the reaction tube.)
- a temperature zone may comprise a plurality of temperature control units which regulate, for example, a constant temperature or a temperature gradient on the corresponding reaction tube section.
- the reactor according to the invention has corresponding devices, connections, inlets and outlets, which make it possible to operate the structure described above and whose realization is familiar to the person skilled in the art.
- a catalyst is conveyed as a moving fixed bed in a reaction tube counter to the flow direction of a starting gas, which is catalytically treated in the reaction tube by means of the catalyst, wherein the educt gas flows through a predetermined temperature profile.
- the temperature profile is spatially composed of several temperature zones with different high temperature ranges, wherein in the respective temperature zones optimum reaction conditions for certain reactions of the treatment of the educt gas are created.
- the reaction unit may be integrated into the evaporation unit, i.
- Each reaction unit of a plurality of reaction units can be integrated in the evaporation unit, so that the product gas / steam reactor according to the invention can also be adapted to the spatial situation.
- the integration in the evaporation unit also has the advantage of optimal heat transfer from respective control sections in the evaporation unit.
- Fig. 1 is a schematic sectional view of a reaction tube according to the invention for carrying out the method according to the invention for the production of steam and product gas by catalytic conversion of a reactant gas.
- Fig. 1 shows schematically a sectional view of a reaction tube 10 according to a
- Embodiment of the present invention with a longitudinal axis 12, in the direction of the reaction tube 10 in a first, a second and a third temperature zone with a higher temperature range between 800 0 C and 600 0 C, a mean temperature range between 600 ° C and 400 0 C. and a lower temperature range between 400 ° C and 300 ° C; and
- Fig. 2 shows schematically an arrangement of several (here three) reaction tubes connected via respective heat transfer units to a steam generating unit to a modular product gas-steam reactor according to the present invention.
- the second zone and the third zone are cooled by temperature control units 14 and 16, while for the heating of the first zone, the reactant gas at a temperature of about 800 0 C itself provides and their temperature by a heat transfer mung 18 is maintained.
- a catalyst bed 20 forming a moving fixed bed is conveyed in the direction of arrow 22 in the drawing from an uppermost end of the reaction tube 10 to a lower second end of the reaction tube 10, whereby the flow through a lock 24 is adjusted.
- the educt gas is introduced from below into the reaction tube 10 in the direction of the arrow 26, which is a supply line of the educt gas, and removed via a corresponding line 28 on the opposite side in the prepared state as product gas.
- the flow direction of the educt gas is thus opposite to the movement or conveying direction of the catalyst charge 20.
- zone 1 the long-chain and cyclic hydrocarbons are reformed with the vapor in the educt gas, ie carbon monoxide and hydrogen converted substance.
- the particles from the gas phase are retained in the catalyst bed, which acts as a so-called depth filter.
- the gas is cooled to the above temperature.
- the sulfur contained in the educt gas is absorbed and chemically bound, and the educt gas is methanized. Due to the continuous tracking or conveying of the catalyst feed 20, spent catalyst is replaced by fresh catalyst.
- control loop is indicated schematically by dotted lines.
- Each of the reaction tubes 10-i is subdivided into control sections whose boundaries are indicated by dashed lines and which are identified by the letters AH Each control section AH corresponds to a temperature zone which can be set by a control unit assigned to it
- Each of the reaction tubes 10-i comprises an infeed line 26 for Feed gas and a discharge line 28 for product gas, which are shown in Figure 2 for indicating the flow direction in each case as an arrow e flow direction of the moving catalyst bed 20 is shown at the top and bottom by arrows 22.
- the reaction tubes 10-1 and 10-2 each include three control sections AC and DF, respectively, while the reaction tube 10-3 includes only two control sections G and H.
- the number of control sections of the individual reaction tubes 10-i is of course only exemplary. In Fig.
- FIG. 2 is further schematically and exemplarily a heat transfer means for transferring heat between two control sections of the same reaction tube (10-1) by a Double arrow " ⁇ -» "40 and between two control sections of various reaction tubes (10-2 and 10-3) by a double arrow" ⁇ -»" 42 shown.
- the heat transfer device 34-1 is connected to only one control section to the upper control section A of the reaction tube 10-1
- the heat transfer device 34-2 is also provided with only one control section, namely the middle one Control section B of the reaction tube 10-2 connected.
- the heat transfer device 34-3 is connected to the upper and lower control sections G, H of the reaction tube 10-3. All connections (heat transfer paths) according to the embodiment comprise suitable provisions (not shown) for the release or interruption of the heat conduction therethrough.
- the heat transfer means 34-i opens with its end facing away from the respective reaction tube 10-i into the steam generating unit 36, where the heat dissipation takes place to a liquid medium 44, which is thereby converted into the vaporous state.
- the steam thus generated is discharged via a corresponding gas outlet opening 46 and fed to a further use.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
Description
Claims
Applications Claiming Priority (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE200810052375 DE102008052375A1 (en) | 2008-10-20 | 2008-10-20 | Combined production of vapor and methane gas from a feed gas, comprises producing methane gas by catalytic conversion of feed gas, transferring heat formed during conversion to vapor generating unit, and producing vapor in generating unit |
DE200810052374 DE102008052374A1 (en) | 2008-10-20 | 2008-10-20 | Steam and product gas generation involves conveying catalyst bed through reactor tube, where feeding gas is allowed to flow into catalyst bed against direction of travel of catalyst bed |
DE102009004750A DE102009004750A1 (en) | 2009-01-15 | 2009-01-15 | Steam and product gas generation involves conveying catalyst bed through reactor tube, where feeding gas is allowed to flow into catalyst bed against direction of travel of catalyst bed |
PCT/EP2009/063686 WO2010046347A1 (en) | 2008-10-20 | 2009-10-19 | Method for manufacturing a product gas and generating steam, and modular product gas-steam reactor for carrying out said method |
Publications (1)
Publication Number | Publication Date |
---|---|
EP2346597A1 true EP2346597A1 (en) | 2011-07-27 |
Family
ID=41508794
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP09748066A Withdrawn EP2346597A1 (en) | 2008-10-20 | 2009-10-19 | Method for manufacturing a product gas and generating steam, and modular product gas-steam reactor for carrying out said method |
Country Status (6)
Country | Link |
---|---|
US (1) | US20120114541A1 (en) |
EP (1) | EP2346597A1 (en) |
CN (1) | CN102186574A (en) |
BR (1) | BRPI0920580A2 (en) |
CA (1) | CA2739868A1 (en) |
WO (1) | WO2010046347A1 (en) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102010055706A1 (en) * | 2010-12-22 | 2012-06-28 | Tridelta Gmbh | Device for cooling a free-flowing or flowable product |
CN112934142B (en) * | 2021-02-01 | 2023-06-06 | 山东大学 | Homogeneous tubular reactor temperature control method and system based on back-stepping method |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4157380A (en) * | 1976-11-26 | 1979-06-05 | Prahl Walter H | Recovery of hydrogen chloride and chlorine from chlorine-containing organic wastes |
US5229102A (en) * | 1989-11-13 | 1993-07-20 | Medalert, Inc. | Catalytic ceramic membrane steam-hydrocarbon reformer |
US6126908A (en) * | 1996-08-26 | 2000-10-03 | Arthur D. Little, Inc. | Method and apparatus for converting hydrocarbon fuel into hydrogen gas and carbon dioxide |
DE102006034811A1 (en) * | 2006-07-27 | 2008-01-31 | Man Dwe Gmbh | Process for changing the temperature of a tube bundle reactor |
US7850944B2 (en) * | 2008-03-17 | 2010-12-14 | Air Products And Chemicals, Inc. | Steam-hydrocarbon reforming method with limited steam export |
-
2009
- 2009-10-19 WO PCT/EP2009/063686 patent/WO2010046347A1/en active Application Filing
- 2009-10-19 BR BRPI0920580A patent/BRPI0920580A2/en not_active IP Right Cessation
- 2009-10-19 CA CA2739868A patent/CA2739868A1/en not_active Abandoned
- 2009-10-19 EP EP09748066A patent/EP2346597A1/en not_active Withdrawn
- 2009-10-19 US US13/125,042 patent/US20120114541A1/en not_active Abandoned
- 2009-10-19 CN CN200980141245.3A patent/CN102186574A/en active Pending
Non-Patent Citations (1)
Title |
---|
See references of WO2010046347A1 * |
Also Published As
Publication number | Publication date |
---|---|
BRPI0920580A2 (en) | 2015-12-29 |
US20120114541A1 (en) | 2012-05-10 |
CA2739868A1 (en) | 2010-04-29 |
WO2010046347A1 (en) | 2010-04-29 |
CN102186574A (en) | 2011-09-14 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
DE60129686T2 (en) | REACTOR FOR EXOTHERMIC OR ENDOTHERMIC HETEROGENIC REACTIONS | |
EP2516358B1 (en) | Method for producing a methane-rich product gas and reactor system usable for that purpose | |
DE102012220926A1 (en) | Fixed Bed Reactor | |
EP2237869B1 (en) | Reactor for carrying out high pressure reactions, method for starting and method for carrying out a reaction | |
WO2009021258A1 (en) | Fluidized bed reactor system | |
EP2234713A1 (en) | Multi-passage thermal sheeting and heat exchanger equipped therewith | |
WO2005025716A1 (en) | Multi-phase fluid distributor for a bundled-tube reactor | |
DE102012220930A1 (en) | Fixed bed reactor useful for carrying out catalytic gas-phase reactions, comprises bundle of vertical heat exchanger tubes, catalyst chamber for accommodating catalyst bed, reactor jacket, upper and lower reactor head, and filling device | |
EP1590076A1 (en) | Multi-zone tubular reactor for carrying out exothermic gas-phase reactions | |
WO2019233673A1 (en) | Method, tube bundle reactor and reactor system for carrying out catalytic gas phase reactions | |
WO2014180693A1 (en) | Fluidized bed reactor and method of producing granular polysilicon | |
WO2010046347A1 (en) | Method for manufacturing a product gas and generating steam, and modular product gas-steam reactor for carrying out said method | |
EP2462398A1 (en) | Method and device for cooling a fine grained solid bulk while exchanging the open space gas contained therein simultaneously | |
DE102010014643A1 (en) | Tube bundle reactor, useful for catalytic gas phase reactions, comprises bundle of vertically arranged reaction tubes, a reactor shell, deflecting plate, reverse opening, bypass openings arranged in deflecting plate and adjusting device | |
DE102006054415A1 (en) | Method and device for injecting oxygen into a reaction gas flowing through a synthesis reactor | |
DE102010000270A1 (en) | Electrode for a reactor for the production of polycrystalline silicon | |
DE102009004750A1 (en) | Steam and product gas generation involves conveying catalyst bed through reactor tube, where feeding gas is allowed to flow into catalyst bed against direction of travel of catalyst bed | |
WO2016173775A1 (en) | Reactor device for releasing a gas from a reactant | |
EP2480632A2 (en) | Syngas reactor with a heated coke cloud | |
DE102018113737A1 (en) | Process and reactor system for carrying out catalytic gas phase reactions | |
WO2010085926A1 (en) | Apparatus and method for the synthesis of ammonia | |
CH703150B1 (en) | Apparatus and method for rapid thermal treatment of bulk materials. | |
EP1621250B1 (en) | Reactor for performing strong exothermic reactions with pressure increase | |
WO2012152638A1 (en) | Method and device for producing syngas from reactants which contain carbon, by means of gasification in a fluidised bed reactor | |
DE2616828C3 (en) | Fluidized bed tank |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
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 |
|
17P | Request for examination filed |
Effective date: 20110415 |
|
AK | Designated contracting states |
Kind code of ref document: A1 Designated state(s): 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 SE SI SK SM TR |
|
AX | Request for extension of the european patent |
Extension state: AL BA RS |
|
RIN1 | Information on inventor provided before grant (corrected) |
Inventor name: KIENBERGER, THOMAS Inventor name: KARL, JUERGEN Inventor name: HOCHLEITNER, THOMAS, DR. Inventor name: SCHWEIGER, ANDREAS |
|
DAX | Request for extension of the european patent (deleted) | ||
17Q | First examination report despatched |
Effective date: 20140130 |
|
RAP1 | Party data changed (applicant data changed or rights of an application transferred) |
Owner name: HIGHTERM RESEARCH GMBH |
|
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: 20160503 |