EP1735084A1 - Wirbelschichtverfahren und reaktor zur durchführung exothermer chemischer gleichgewichtsreaktionen - Google Patents

Wirbelschichtverfahren und reaktor zur durchführung exothermer chemischer gleichgewichtsreaktionen

Info

Publication number
EP1735084A1
EP1735084A1 EP05716251A EP05716251A EP1735084A1 EP 1735084 A1 EP1735084 A1 EP 1735084A1 EP 05716251 A EP05716251 A EP 05716251A EP 05716251 A EP05716251 A EP 05716251A EP 1735084 A1 EP1735084 A1 EP 1735084A1
Authority
EP
European Patent Office
Prior art keywords
fluidized bed
temperature
heat exchanger
reactor
heat
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Withdrawn
Application number
EP05716251A
Other languages
German (de)
English (en)
French (fr)
Inventor
Martin Sohn
Eckhard Stroefer
Olga Schubert
Thomas Grassler
Martin Fiene
Martin Sesing
Lothar Seidemann
Christian Walsdorff
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
BASF SE
Original Assignee
BASF SE
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by BASF SE filed Critical BASF SE
Publication of EP1735084A1 publication Critical patent/EP1735084A1/de
Withdrawn legal-status Critical Current

Links

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
    • B01J8/18—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
    • 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
    • B01J8/1872—Details of the fluidised bed 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
    • B01J8/24—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
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B7/00—Halogens; Halogen acids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B7/00—Halogens; Halogen acids
    • C01B7/01—Chlorine; Hydrogen chloride
    • C01B7/03—Preparation from chlorides
    • C01B7/04—Preparation of chlorine from hydrogen chloride
    • 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
    • B01J2208/00212—Plates; Jackets; Cylinders

Definitions

  • An example of an exothermic chemical equilibrium reaction is the process of catalytic oxidation of hydrogen chloride with oxygen to chlorine, developed by Deacon in 1868.
  • Catalysts based on chromium oxide as are known, for example, from US Pat. No. 4,828,815, are also suitable.
  • the object of the invention is to provide an improved method for carrying out exothermic chemical equilibrium reactions in a fluidized bed reactor.
  • it is an object of the invention to provide a process with an improved space-time yield, i.e. to provide a greater yield with the same reactor volume and the same reaction time as in the processes known from the prior art.
  • Fluidized bed reactors generally have a cylindrical or approximately rotationally symmetrical geometry and are generally flowed through parallel to the axis of rotation.
  • the flow direction formulated above is also to be referred to as axial flow and to be distinguished from radial flows occurring locally within the fluidized bed, which, however, largely compensate in total over the total height of the fluidized bed.
  • An absolute temperature maximum i.e. the maximum temperature in the entire fluidized bed
  • Surface is the area of the fluidized bed through which the gas flows out of the fluidized bed.
  • catalyst systems which contain volatile active components at elevated temperature can be operated with better long-term stability.
  • Such catalyst systems are, for example, supported ruthenium compounds. Due to the temperature decreasing towards the surface of the fluidized bed, volatile catalyst compounds of colder catalyst particles in the upper area of the fluidized bed can be captured again and can be continuously returned to the lower areas of the fluidized bed.
  • the temperature decreases along the direction of flow from an absolute temperature maximum both to the gas distributor and to the surface of the fluidized bed.
  • the distance between the absolute temperature maximum and the gas distributor is less than the distance between the absolute temperature maximum and the surface of the fluidized bed.
  • the distance between the gas distributor base and the heat exchanger should therefore not be more than 10 m, preferably not more than 6 m and in particular not more than 3 m. In a very particularly preferred embodiment of the invention, this distance is not more than 2 m.
  • the temperature distribution can take place by arranging one or more dividing plates between two temperature zones in each case.
  • a temperature zone is to be understood as an area with an approximately constant temperature in the fluidized bed.
  • perforated or sieve trays are suitable as dividers.
  • the mixing of the fluidized bed is at the position of the separating bottom deteriorated, so that at the position of the separating bottom, less vortex granulate is entrained with the ascending gas bubbles and at the same time less vortex granulate flows through the dividing bottom against the direction of flow of the gas bubbles into the region of the fluidized bed below the dividing bottom. This worsens the convective heat transport, so that a clear temperature limit is established in the area of the partition.
  • a further improved separation of the temperature zones in the fluidized bed can be achieved by using an isolating partition.
  • the opening diameter on the underside of the perforated base is smaller than the average gas bubble diameter.
  • the opening diameter on the underside is preferably in the range from 0.5 to 10 cm, more preferably in the range from 0.7 to 8 cm and particularly preferably in the range from 1 to 5 cm.
  • the opening diameter on the top is preferably in the range from 0.5 to 30 cm, more preferably in the range from 2 to 20 cm and particularly preferably in the range from 5 to 15 cm.
  • the upper hole diameter is selected such that it is larger than the average gas bubble diameter.
  • the opening angle ie the angle between the side wall of the opening and the central axis of the opening, is selected such that it is greater than the angle of expansion of the gas bubbles, so that the vortex granules counteract against the gas flow in the openings along the side surfaces can flow.
  • the opening angle in a preferred embodiment is also larger than the slope angle of the granulate bed.
  • the angle of embankment is the angle at which the bulk material just begins to slip with a loose fill.
  • the opening angle is preferably in the range from 0 to 60 °, more preferably in the range from 10 to 50 ° and particularly preferably in the range from 20 to 40 °.
  • the fluidized bed granules contain the catalyst.
  • the individual granules can each consist of catalyst material or contain the catalyst material on their surface.
  • the catalyst comprises a metal component on an oxidic support.
  • Metal components are, for example, ruthenium or copper compounds.
  • Aluminum oxide, in particular ⁇ -aluminum oxide or ⁇ -aluminum oxide, zirconium oxide or titanium oxide or mixtures of these oxides, can be used as the oxide carrier.
  • the oxidic carriers are preferably used in powder form with an average particle diameter of 30 to 150 ⁇ m, more preferably 40 to 100 ⁇ m and in particular 50 to 80 ⁇ m.
  • the fine fraction with a par Particle size ⁇ 20 ⁇ m is preferably less than 40% by weight, more preferably less than 30% by weight and in particular less than 20% by weight.
  • FIG. 1 shows a schematic illustration of a fluidized bed reactor designed according to the invention with the temperature profile in the reactor
  • FIG. 3 shows a plan view of a dividing floor designed as a perforated floor with frusto-conical openings
  • the temperature transition from the temperature of the first temperature zone 6 to the temperature of the second temperature zone 8 takes place over a larger area of the fluidized bed 5.
  • the fluidized bed reactor 1 shown in FIG. 2 differs from the embodiment shown in FIG. 1 in that a second heat exchanger 28 is accommodated in the first temperature zone 6.
  • the structure and the mode of operation of the second heat exchanger 28 correspond to that of the heat exchanger 12.
  • a heat transfer medium is supplied to the second heat exchanger 28 via a heat transfer medium feed 29.
  • the heat carrier flows into heat exchanger tubes 31 through heat carrier distributor 30.
  • the heat exchanger tubes 31 open into steam collectors 32, via which the heat carrier is fed to a heat carrier outlet 33, is withdrawn from the second heat exchanger 28.
  • the partition 7 has an insulating effect.
  • it is either made of an insulating material or contains a thermally insulating layer.
  • FIG. 3 shows a plan view of an embodiment of a partition 7 with frustoconical openings 34.
  • the openings 34 can take on any arrangement known to the person skilled in the art. For example, in addition to the arrangement of the openings 34 shown here on axes perpendicular to one another, the openings 34 can also be arranged offset.
  • the height of the cavity 43 is identified by the reference symbol 42.
  • the height 42 is preferably in the range from 0.1 to 20 cm, more preferably in the range from 1 to 15 cm and in particular in the range from 3 to 10 cm.
  • the material for the wall 44 of the partition 7 is preferably chosen so that it is chemically stable against the educt gases and product gases.
  • the thickness of the wall 44 is preferably in the range from 1 to 50 mm, more preferably in the range from 2 to 30 mm and in particular in the range from 5 to 20 mm.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Inorganic Chemistry (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Catalysts (AREA)
EP05716251A 2004-03-25 2005-03-21 Wirbelschichtverfahren und reaktor zur durchführung exothermer chemischer gleichgewichtsreaktionen Withdrawn EP1735084A1 (de)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
DE102004014677A DE102004014677A1 (de) 2004-03-25 2004-03-25 Wirbelschichtverfahren und Reaktor zur Durchführung exothermer chemischer Gleichgewichtsreaktionen
PCT/EP2005/002973 WO2005092488A1 (de) 2004-03-25 2005-03-21 Wirbelschichtverfahren und reaktor zur durchführung exothermer chemischer gleichgewichtsreaktionen

Publications (1)

Publication Number Publication Date
EP1735084A1 true EP1735084A1 (de) 2006-12-27

Family

ID=34963086

Family Applications (1)

Application Number Title Priority Date Filing Date
EP05716251A Withdrawn EP1735084A1 (de) 2004-03-25 2005-03-21 Wirbelschichtverfahren und reaktor zur durchführung exothermer chemischer gleichgewichtsreaktionen

Country Status (8)

Country Link
US (1) US20070202035A1 (ja)
EP (1) EP1735084A1 (ja)
JP (1) JP4664968B2 (ja)
KR (1) KR101285932B1 (ja)
CN (2) CN1956775A (ja)
DE (1) DE102004014677A1 (ja)
SG (1) SG175661A1 (ja)
WO (1) WO2005092488A1 (ja)

Families Citing this family (15)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP4389122B2 (ja) * 2006-02-27 2009-12-24 井関農機株式会社 苗移植機
ES2356488T3 (es) * 2006-09-19 2011-04-08 Basf Se Procedimiento para la obtención de cloro en un reactor de lecho fluidizado.
ES2347606T3 (es) 2006-09-19 2010-11-02 Basf Se Procedimiento para la abtencion de animas aromaticas en un reactor de lecho fluidizado.
US20090163756A1 (en) * 2007-12-19 2009-06-25 Uop Llc, A Corporation Of The State Of Delaware Reactor cooler
KR100937373B1 (ko) * 2008-02-14 2010-01-20 아사히 가세이 케미칼즈 가부시키가이샤 유동층 반응기의 온도 제어 방법
US20110318259A1 (en) * 2009-03-30 2011-12-29 Basf Se Process for preparing chlorine
KR20120106694A (ko) * 2009-06-24 2012-09-26 바스프 에스이 염화수소로부터 염소를 제조하는 방법
US20120134913A1 (en) * 2009-08-05 2012-05-31 Basf Se Method for producing chlorine by gas phase oxidation of hydrogen chloride in a fluidized-bed reactor
CN103764548A (zh) * 2011-07-05 2014-04-30 拜耳知识产权有限责任公司 在等温反应器中使用氧化铈催化剂的制氯方法
JP2014125418A (ja) * 2012-12-27 2014-07-07 Mitsubishi Materials Corp カーボンナノファイバーの製造装置及び製造方法
CN103965389B (zh) * 2014-05-13 2016-09-21 清华大学 碳纳米管-高分子复合材料的气相聚合生产方法及装置
US10385468B2 (en) 2016-06-06 2019-08-20 Ih Ip Holdings Limited Plasma frequency trigger
CN112439368B (zh) * 2019-09-05 2023-11-10 中石油吉林化工工程有限公司 一种用于制丙烯腈的反应器
CN112439367A (zh) * 2019-09-05 2021-03-05 中石油吉林化工工程有限公司 空气分布板
CN110694558B (zh) 2019-10-29 2021-01-22 浙江新安化工集团股份有限公司 一种多区式浆态列管反应器

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US3735498A (en) * 1970-04-21 1973-05-29 Ube Industries Method of and apparatus for fluidizing solid particles

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US3735498A (en) * 1970-04-21 1973-05-29 Ube Industries Method of and apparatus for fluidizing solid particles

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See also references of WO2005092488A1 *

Also Published As

Publication number Publication date
KR101285932B1 (ko) 2013-07-12
KR20070018917A (ko) 2007-02-14
CN1956775A (zh) 2007-05-02
US20070202035A1 (en) 2007-08-30
CN103288052A (zh) 2013-09-11
SG175661A1 (en) 2011-11-28
DE102004014677A1 (de) 2005-10-13
WO2005092488A1 (de) 2005-10-06
JP4664968B2 (ja) 2011-04-06
JP2007530403A (ja) 2007-11-01

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