EP3439777A1 - Réacteur et procédé pour convertir des réactions limitées par l'équilibre réactionnel - Google Patents
Réacteur et procédé pour convertir des réactions limitées par l'équilibre réactionnelInfo
- Publication number
- EP3439777A1 EP3439777A1 EP17733986.8A EP17733986A EP3439777A1 EP 3439777 A1 EP3439777 A1 EP 3439777A1 EP 17733986 A EP17733986 A EP 17733986A EP 3439777 A1 EP3439777 A1 EP 3439777A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- reactor
- hollow shaft
- stirring blade
- gas
- phase zone
- 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- Withdrawn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
- 238000006243 chemical reaction Methods 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title claims description 11
- 238000003756 stirring Methods 0.000 claims abstract description 36
- 239000000463 material Substances 0.000 claims abstract description 26
- 239000003054 catalyst Substances 0.000 claims abstract description 25
- 239000007795 chemical reaction product Substances 0.000 claims abstract description 11
- 239000000203 mixture Substances 0.000 claims description 32
- 239000007791 liquid phase Substances 0.000 claims description 19
- 239000000047 product Substances 0.000 claims description 18
- 239000002594 sorbent Substances 0.000 claims description 14
- 239000007788 liquid Substances 0.000 claims description 9
- 239000012071 phase Substances 0.000 claims description 5
- 239000007858 starting material Substances 0.000 claims description 5
- 239000000376 reactant Substances 0.000 abstract description 7
- 239000007789 gas Substances 0.000 description 52
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 6
- 238000003786 synthesis reaction Methods 0.000 description 5
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 4
- 239000001257 hydrogen Substances 0.000 description 4
- 229910052739 hydrogen Inorganic materials 0.000 description 4
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 3
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 3
- 238000009620 Haber process Methods 0.000 description 2
- 229910021529 ammonia Inorganic materials 0.000 description 2
- 238000004519 manufacturing process Methods 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 229910052757 nitrogen Inorganic materials 0.000 description 2
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 description 1
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 1
- 241000158147 Sator Species 0.000 description 1
- 239000002250 absorbent Substances 0.000 description 1
- 230000002745 absorbent Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 229910002091 carbon monoxide Inorganic materials 0.000 description 1
- 229910002090 carbon oxide Inorganic materials 0.000 description 1
- 230000006835 compression Effects 0.000 description 1
- 238000007906 compression Methods 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000001816 cooling Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 238000005580 one pot reaction Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 238000001179 sorption measurement Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 230000007306 turnover Effects 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 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
- B01J8/0242—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 flow within the bed being predominantly vertical
- B01J8/0257—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 flow within the bed being predominantly vertical in a cylindrical annular shaped bed
-
- 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
- B01J8/0278—Feeding reactive fluids
-
- 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
- B01J8/10—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by stirrers or by rotary drums or rotary receptacles or endless belts
-
- 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00805—Details of the particulate material
- B01J2208/00814—Details of the particulate material the particulate material being provides in prefilled containers
-
- 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
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00823—Mixing elements
- B01J2208/00858—Moving elements
- B01J2208/00876—Moving elements outside the bed, e.g. rotary mixer
-
- 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
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00884—Means for supporting the bed of particles, e.g. grids, bars, perforated 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
- B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
- B01J2208/00796—Details of the reactor or of the particulate material
- B01J2208/00938—Flow distribution elements
Definitions
- the invention relates to a process for the conversion of equilibrium limited reactions according to the preamble of claim 1 and a reaction apparatus for imple ⁇ wetting of equilibrium-limited reactions according to the preamble of claim 7.
- the object of the invention is to provide a process and a reaction plant for the implementation of equilibrium-limited reactions which, compared to the prior art, bring about a higher yield in the reaction process and require less technical effort.
- the object is achieved in a reactor for the implementation of equilibrium-limited reactions according to claim 1 and a method for the implementation of equilibrium-limited reactions according to claim 6.
- the reactor according to the invention for the reaction of equi ⁇ weight limited reactions comprises a reaction chamber with a Eduktzu thoroughlyvoriques, an outlet device for reaction products and a device for receiving catalyst material and a stirring device.
- the reactor is characterized in that the stirring device includes a hollow shaft at one end thereof a Gaseintrittsöff ⁇ voltage is provided and that a first stirring blade is provided with a gas outlet opening at the hollow shaft. Furthermore, to the hollow shaft in the area of the device for holding the catalyst material, a second blade on ⁇ sorted.
- the second impeller which is arranged in the region of the catalyst material causes a better mainly horizontal gas mixing in this area, and therefore, again vortexed for the reactants which are present in the gas mixture to the catalyst material ⁇ the, so again a continuous reaction process is guaranteed ,
- a liquid phase zone is seen ⁇ , wherein above this liquid phase zone, a Gaspha ⁇ Senzone present.
- the first impeller, the stirring ⁇ wings are arranged with the gas outlet openings in the region of the liquid phase zone and the second impeller is arranged in the gas phase.
- the Pro ⁇ -products present in the gas mixture is absorbed by the sorbent.
- the remaining gas of the gas mixture when it emerges from the liquid phase zone, ie ascend gas bubbles and pass into the gas phase zone, results in a high proportion of educts.
- the second impeller is in one embodiment of the invention preferably in the form of a Radial detergentrlochers ⁇ staltet, resulting in that the second impeller from the hollow shaft of the gas mixture in particular carries radially out ⁇ Shen and thereby in the range of the catalyst material, a good turbulence generated.
- the extent of the first impeller radial to the hollow shaft between 20% and 30% of the total reactor diameter.
- extension and impeller means the weites ⁇ th diameter over which extend the one or more stirring blades with respect to the hollow shaft.
- impeller is to be understood in general, since a large number of various stirring devices may be appropriate. Sigma stirrers, alpha stirrers, INTERMIG stirrers, MIG stirrers or disk stirrers may be used for the flow of the gas mixture, all of which have different geometrical constructions.
- the term impeller means any suitable for the distribution of the gas mixture and the circulation of the liquid phase zones device which is arranged on the hollow shaft. In a further embodiment of the invention is the
- Reactor designed in such a way that it moves the agitating blade in the operating state in such a way that a web speed of the agitating blade is between 5 m / s and 15 m / s.
- Another component of the invention is a process for the implementation of equilibrium-limited reactions according to claim 7, comprising the following steps: First, a catalyst material is arranged in the reactor, further one or more starting materials is introduced into the reactor, wherein it reacts for the reactants comes to a product and where ⁇ in a stirring device is provided, through which a gas mixture, is sucked in from an upper portion of the reactor and is passed through a hollow shaft in a lower portion of the reactor.
- the gas mixture is discharged from the gas outlet openings in a mounted on the hollow shaft first impeller.
- the gas mixture thus discharged is passed from there back into an upper region of the reactor, wherein it flows through the catalyst material located in the reactor.
- a further stirring blade is provided on the hollow shaft, through which a turbulence of the gas mixture is brought about in the region of the catalyst material.
- the circulation results in a flow in the gas mixture and thus in the reaction space, which makes it possible to obtain an isobaric operation at high pressures.
- a liquid phase zone is present, in particular with a sorbent as a liquid, caused by the introduction of gas in the liquid phase zone of gas bubbles, which have a high mass transfer ⁇ surface with the liquid, preferably in the sorbent, and thus an effective mass transfer, So the products allow to sorbent.
- ⁇ det a good mixing instead of liquid.
- FIG. 1 shows a reactor with a catalyst material and egg ⁇ ner stirring device, wherein the stirring device is driven in the reactor from below,
- Figure 2 shows a reactor analogous to that of Figure 1, in which a
- FIG. 3 shows a reactor as in FIG. 1, wherein the reactor is operated in such a way that the products are gaseous in the prevailing atmosphere.
- the reactor 2 according to FIG. 1 has a reaction space 4, an educt feed device 6 for the supply of starting materials 7 and an outlet device 8 for products 10. Furthermore, the reactor 2 comprises a device 12 for receiving catalyst material 14.
- the device 12 may be configured as a basket or net, wherein the catalyst material is present.
- the catalyst material 14 can be used as a bed in the Vorrich- However, it may also be arranged to improve the flow on multiple levels or layers in the device 12.
- the reactor 2 comprises a stirring device 16, which in turn comprises a hollow shaft 18, wherein a gas inlet opening 20 is provided on the hollow shaft 18 in an upper region 27 of the reactor.
- a first impeller 22, which has a gas outlet openings 24, is arranged on the hollow shaft 18 in a lower region 28 of the reactor.
- the gas mixture 38 which is a mixture of gaseous reactants and gaseous products 7 10 basically in Wesentli ⁇ Chen, introduced into a liquid phase zone 30th
- This liquid phase zone 30 comprises a Sorp ⁇ tion means 40 which is present here in a liquid form and serves substantially to absorb the reaction products from the reactor 10 and ultimately derive from the reactor. 2
- the liquid sorbent 40 collects in the liquid phase zone 28, which does not exclude that in the remaining reaction ⁇ space 4 liquid sorbent 40, for example in
- the sorbent 40 is also discharged through the outlet device 8 for products 10 and is supplied to a separation process which is not described in more detail here. Accordingly, the sorbent is 40 just ⁇ if telzuchtvortechnisch by a not further described here Sorptionsmit- back to the reactor 2 and the reaction chamber 4 is supplied.
- the stirring device 16 thus described is a self-priming gas introduction stirrer, through which gas is passed from the upper reaction region into the lower region 28 of the reactor. As described, the gas bubbles emerging from the second impeller thus facilitate the connection of the products present in these gas bubbles with the sorbent.
- a second impeller 26 is provided on the hollow shaft 18, the insbeson ⁇ particular is designed as Radialrrocker.
- Examples of such a stirrer with a mainly radially generated conveying direction are disc stirrers, impeller stirrers,
- the second impeller 26 in this case has an extension with respect to the Reaktor admirals ⁇ sers, which affects between 20 and 35% of this reactor diameter.
- the web speed of the second impeller be ⁇ carries it between 3 m / s to 6 m / s.
- the gas mixture 38 which is provided above the region in which the catalyst material 14 is arranged, is accordingly enriched in reaction products.
- the system comprises reactants that were not converted in the equilibrium state of the reaction at Kataly ⁇ sator material 14 and reaction production ⁇ te.
- This gas mixture 38 is again separated by the stirring device. sucked and occurs in the gas inlet opening 20 again in the hollow shaft 18, wherein the cycle process described begins again.
- the first impeller has an extension 34 which is between 20% and 30% of the diameter 36 of the reactor space.
- FIG. 1 shows a stirring device 16 which has a drive 29 in the lower region 28 of the reactor 2.
- FIG. 1 shows a stirring device 16 which has a drive 29 in the lower region 28 of the reactor 2.
- a drive 29 of the stirring device 16 is arranged in the upper region 27.
- the reactor 2 according to Figure 3 differs from the two reactors according to Figures 1 and 2 in that there the thermodynamic conditions are adapted in a way that no sorbent is required 40, but that the Pro ⁇ -products 10 in gaseous form, be removed from the reaction space 4.
- the gas inlet opening 20 of the hollow shaft is designed so that it is mounted outside of the reaction space 4.
- the liquid phase for example, could be in the form of a heat transfer oil Darge ⁇ provides, but which is not shown here in this illustration.
- reaction products 10 such as water and Metha ⁇ nol may additionally condensed out and the reaction heat to be dissipated.
- the remaining gas stream is then sucked by the first impeller and recycled back into the reaction chamber 4 to ⁇ .
- the gas recirculation is or any additional blowers only through the stirring device 16 upright preserver ⁇ th.
- the continuous removal of condensed reaction products 10, the reaction equilibrium is shifted analogously to the pick-up by the absorbent. additional The condensation of products in the region outside of the reaction space 2 could lead to a pressure drop, which then supports the flow of the gas stream.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Engineering & Computer Science (AREA)
- Combustion & Propulsion (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
- Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Abstract
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102016210224.9A DE102016210224A1 (de) | 2016-06-09 | 2016-06-09 | Reaktor und Verfahren zur Umsetzung von gleichgewichtslimitierten Reaktionen |
PCT/EP2017/064080 WO2017212016A1 (fr) | 2016-06-09 | 2017-06-09 | Réacteur et procédé pour convertir des réactions limitées par l'équilibre réactionnel |
Publications (1)
Publication Number | Publication Date |
---|---|
EP3439777A1 true EP3439777A1 (fr) | 2019-02-13 |
Family
ID=59253461
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP17733986.8A Withdrawn EP3439777A1 (fr) | 2016-06-09 | 2017-06-09 | Réacteur et procédé pour convertir des réactions limitées par l'équilibre réactionnel |
Country Status (7)
Country | Link |
---|---|
US (1) | US10441931B2 (fr) |
EP (1) | EP3439777A1 (fr) |
CN (1) | CN109310968A (fr) |
AU (1) | AU2017276766B2 (fr) |
CL (1) | CL2018003488A1 (fr) |
DE (1) | DE102016210224A1 (fr) |
WO (1) | WO2017212016A1 (fr) |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DK3556451T3 (da) | 2018-04-20 | 2020-08-31 | Siemens Ag | Fremgangsmåde til drift af et reaktoranlæg |
EP3556460A1 (fr) | 2018-04-20 | 2019-10-23 | Siemens Aktiengesellschaft | Réacteur de mise en uvre de réactions à équilibre réduit |
CN109046219B (zh) * | 2018-09-19 | 2019-06-07 | 亚洲创建奕宏化工(河源)有限公司 | 自清洁环保型胶体反应装置 |
DE102019201172A1 (de) | 2019-01-30 | 2020-07-30 | Siemens Aktiengesellschaft | Reaktorkaskade und Verfahren zum Betreiben einer Reaktorkaskade |
Family Cites Families (21)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB695301A (en) * | 1950-06-06 | 1953-08-05 | Monsanto Chemicals | Improvements in or relating to manufacture of vanillin from lignin |
US4594228A (en) * | 1984-05-21 | 1986-06-10 | The Standard Oil Company | Mixing apparatus |
FR2580271B1 (fr) * | 1985-04-16 | 1994-07-08 | Air Liquide | Procede de production d'ozone |
DE3866864D1 (de) * | 1988-02-05 | 1992-01-23 | Process Engineering Consultant | Verfahren zur herstellung von methanol. |
DE3806543A1 (de) * | 1988-03-01 | 1989-09-14 | Herbert Huettlin | Wirbelschichtapparatur, insbes. zum granulieren pulverfoermiger substanz |
DE4109502A1 (de) * | 1991-03-22 | 1992-09-24 | Degussa | Katalysator zur haertung von fettsaeuren und verfahren zu seiner herstellung |
DE4435839A1 (de) * | 1994-10-07 | 1996-04-11 | Bayer Ag | Schlammphasenreaktor und dessen Verwendung |
US5759242A (en) * | 1996-07-23 | 1998-06-02 | Praxair Technology, Inc. | Radial bed vaccum/pressure swing adsorber vessel |
DE10104849A1 (de) * | 2000-02-09 | 2001-07-26 | Roland Adler | Modularer gradientenfreier Versuchsreaktor für heterogen-gaskatalytische Reaktionen an körnigen Katalysatorpartikeln |
FR2818160B1 (fr) * | 2000-12-20 | 2003-03-07 | Air Liquide | Procede d'oxydation de type oxydation par voie humide ou ozonation |
US7074962B2 (en) * | 2002-02-15 | 2006-07-11 | Air Products And Chemicals, Inc. | Catalyst holder and agitation system for converting stirred tank reactor to fixed bed reactor |
US7279145B2 (en) * | 2003-03-10 | 2007-10-09 | Lyondell Chemical Technology, L.P. | Multiphase reactor design incorporating filtration system for fixed--bed catalyst |
TWI263675B (en) * | 2004-12-15 | 2006-10-11 | Ind Tech Res Inst | Process for preparing nanofluids with rotation packed bed reactor |
RU2288209C1 (ru) * | 2005-03-28 | 2006-11-27 | Институт Катализа Им. Г.К. Борескова Сибирского Отделения Российской Академии Наук | Способ получения метанола из синтез-газа |
DK2650047T3 (en) * | 2010-12-07 | 2018-02-26 | Tokyo Inst Tech | AMMONIA SYNTHESIS CATALYST AND AMMONIA SYNTHESIS PROCEDURE |
DE102011016742A1 (de) * | 2011-04-12 | 2012-10-18 | Linde Aktiengesellschaft | Kolonne |
CN102584526B (zh) * | 2011-12-28 | 2014-09-10 | 上海碧科清洁能源技术有限公司 | 一种由合成气制备甲醇的膜接触器方法以及用于该方法的膜反应器 |
CN204147861U (zh) * | 2014-08-21 | 2015-02-11 | 山东鲁化天九化工有限公司 | 一种氢化釜用自吸式搅拌器 |
CN204208558U (zh) * | 2014-09-29 | 2015-03-18 | 天津一化化工有限公司 | 一种新型自吸式反应釜 |
CN204973923U (zh) * | 2015-08-19 | 2016-01-20 | 泉州海岸线新材料科技有限公司 | 一种高效加气反应器 |
CN205253105U (zh) * | 2015-12-03 | 2016-05-25 | 薛永和 | 一种可实现釜内气体自循环的新型搅拌反应釜 |
-
2016
- 2016-06-09 DE DE102016210224.9A patent/DE102016210224A1/de not_active Withdrawn
-
2017
- 2017-06-09 EP EP17733986.8A patent/EP3439777A1/fr not_active Withdrawn
- 2017-06-09 US US16/307,932 patent/US10441931B2/en not_active Expired - Fee Related
- 2017-06-09 WO PCT/EP2017/064080 patent/WO2017212016A1/fr active Application Filing
- 2017-06-09 AU AU2017276766A patent/AU2017276766B2/en not_active Ceased
- 2017-06-09 CN CN201780035181.3A patent/CN109310968A/zh active Pending
-
2018
- 2018-12-05 CL CL2018003488A patent/CL2018003488A1/es unknown
Also Published As
Publication number | Publication date |
---|---|
AU2017276766A1 (en) | 2018-12-06 |
WO2017212016A1 (fr) | 2017-12-14 |
US10441931B2 (en) | 2019-10-15 |
CL2018003488A1 (es) | 2019-02-15 |
US20190217267A1 (en) | 2019-07-18 |
AU2017276766B2 (en) | 2020-04-16 |
DE102016210224A1 (de) | 2017-12-14 |
CN109310968A (zh) | 2019-02-05 |
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