WO2021104613A1 - Procédé semi-sec optimisé pour le frittage d'aluminosilicates dans la production d'alumine - Google Patents

Procédé semi-sec optimisé pour le frittage d'aluminosilicates dans la production d'alumine Download PDF

Info

Publication number
WO2021104613A1
WO2021104613A1 PCT/EP2019/082626 EP2019082626W WO2021104613A1 WO 2021104613 A1 WO2021104613 A1 WO 2021104613A1 EP 2019082626 W EP2019082626 W EP 2019082626W WO 2021104613 A1 WO2021104613 A1 WO 2021104613A1
Authority
WO
WIPO (PCT)
Prior art keywords
fluidized bed
mixture
circulating fluidized
reactor
bed reactor
Prior art date
Application number
PCT/EP2019/082626
Other languages
English (en)
Inventor
Tobias Rothenfluh
Alessio SCARSELLA
Günter Schneider
Maciej WROBEL
Peter Sturm
Fabio STRAZZULLO
Original Assignee
Outotec (Finland) Oy
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 Outotec (Finland) Oy filed Critical Outotec (Finland) Oy
Priority to CN201990001481.4U priority Critical patent/CN219463345U/zh
Priority to BR212022010130U priority patent/BR212022010130U2/pt
Priority to PCT/EP2019/082626 priority patent/WO2021104613A1/fr
Publication of WO2021104613A1 publication Critical patent/WO2021104613A1/fr
Priority to AU2022100082A priority patent/AU2022100082B4/en
Priority to DKBA202200048U priority patent/DK202200048Y3/da

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
    • B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
    • B01J6/001—Calcining
    • 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
    • B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
    • B01J6/001—Calcining
    • B01J6/002—Calcining using rotating drums
    • 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
    • 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
    • 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
    • B01J8/224—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 the particles being subject to a circulatory movement

Definitions

  • the present invention describes an apparatus for treating aluminum comprising at least one device for mixing aluminum ore with limestone and sodium and/or potassium carbonate to obtain a mixture and a calcination reactor for producing the calcine.
  • the invention also relates to the corresponding process.
  • AI 2 O3 Aluminum oxide (AI 2 O3) is predominantly produced from bauxite in the Bayer pro- cess. The mined and milled ore is treated with sodium hydroxide at elevated tem peratures of 150 to 200 °C forming soluble sodium aluminate (NaAI0 2 ), which is precipitated as aluminum hydroxide (AI(OH)3) from the obtained supersaturated solution. In the following calcination step, AI 2 O3 is formed at temperatures >1000 °C.
  • the ore's silica content must be below 10%. Higher levels of silica result in the simultaneous dissolution of alumina and silica, forming insoluble sodium aluminosilicates in the process, which significantly increases the amount of sodium hydroxide per ton of produced AI 2 O3 and hence the overall yield.
  • the sintering process is classified as wet, semi-wet or dry sintering, depending on the water content of the feed.
  • the industrially applied wet sintering process operates with a slurry-like feed with an approximate water content of 30 wt.-%.
  • the semi-dry sintering demands the granulation of the feed material featuring a residual water content of 10-15 wt.-%.
  • a dry sintering approach is possible, if the caustic ratio equals 2 and if only calcinated limestone must be added to adjust the CaO/SiC>2 ratio accordingly.
  • the wet sintering ensures agglomerates and, therefore, an easy handling. How ever, it also suffers from the sticky consistence of its feed material, which leads to a high energy demand due to additional evaporation energy. Kilns with long residence times have to be applied for drying, calcination and subsequent sinter ing, resulting in a high specific energy consumption of 1200-1300 kcal/kg(sinter).
  • the dry sintering process for the sintering of nepheline to pro prise alumina is the most efficient approach in terms of energy consumption (650- 700 kcal/kg(sinter)).
  • the major advantage in (most of) the dry process is the pre calcination of the limestone in a flash pre-calciner prior to sintering in the rotary kiln. This allows for much higher throughputs and shorter rotary kilns, because the major part of the calcination does not take place in the kiln.
  • the dry sintering process is limited to ores featuring a caustic ratio of 2.
  • a semi-dry sintering process is e.g. disclosed in CN 105 540 627.
  • Bayer alkali red mud powder, lime, bauxite, soda ash and pulverized coal are mixed uniformly to be raw material pellets, and the raw material pellets are sintered to obtain the clinker of the alumina produced by the sintering process using two rotary kiln.
  • Such a semi-dry sintering approach dry to combine the benefits of a wet and a fry sintering. This results in kilns of smaller dimension and consequently a lower en ergy consumption of 800-900 kcal/kg(sinter) compared to the wet sinter approach.
  • an additional reduction of energy consumption, lower residence times and the handling of low melting alkalis is necessary in order to further reduce the process' energy consumption.
  • a plant with the features of claim 1 solves this task.
  • the setup of the plant consists of at least one device for mixing the crude aluminum ore with limestone and sodium and/or potassium carbonate. It further comprises a calcination reactor for producing the calcine.
  • the basic idea underlying the invention is that between mixing and calcination, a cir culating fluidized bed reactor is foreseen to pre-calcine the mixture.
  • the obtained mixture is granulated in two series-con- nected granulators.
  • the formation of granulates encapsulate the Na 2 C03 / K2C03additive within the grains.
  • the Na 2 CC>3/ K 2 CO3 solution added in the granulation process does not only pro- vide the solid mixture with the required alkalis, but also acts as a binder and de cisively enhances the granulation process. This was shown in a series of labora tory granulation tests.
  • the grain size is typically between typically 5-20mm, which is most preferred for fluidizing bed systems.
  • the used reactor type could be a kiln. This has the advantage that rotary kiln belongs to a relatively cheap and very well- known technology. However, it is also possible to use any kind of fluidizing bed reactor to improve heat and mass transfer.
  • a ratio R of (Na 2 0+K 2 0)/Al 2 03 is 0,95 ⁇ R ⁇ 1 ,05 to en sure a high product quality. Therefore, a control unit is used to control or regulate the amounts of ore and alkali mixed in the granulation.
  • the sodium and/or potassium carbonate is a salt solution stored in granulation liquor tanks. It is possible to admix water to control the solution's concentration. Therefore, it is also possible to work with a low- or supersaturated solution. Additional energy savings can be made by feed ing the granulation tanks with a (oversaturated) salt solution from the salt plant of the refinery. This saves additional evaporation energy in the salt plant, which cor responds to roughly 30 kcal per kg of produced sinter (depending on the concen tration of the salt solution).
  • At least one, preferably 2 to 3 pre-heating stage for the mixture and/or the granules is provided.
  • the material is heated from ambient temperature to about 200 °C. Thereby, it is possible to improve further the energy efficiency, particularly by any heat-recycling concept.
  • a dryer for the mixture or granules is foreseen before the circulating fluidized bed reactor. Therefore, it is possible to reduce the water content, preferably to a value below 1 wt.-%, and, as a consequence, also the energy consumption.
  • the granules have a very good drying behavior keeping the rotary dryer comparatively short.
  • the achieved mixture is preferably pre-calcined in the circulating fluidized bed reactor at 700 to 900 °C, preferably at 800 to 850 °C to achieve a sufficient rate of pre-calcination.
  • the final calcination step in the calcination reactor typically takes place at 800 to 1400°C, preferably at 1000 to 1300 °C.
  • the mean residence time in the circulating fluidized bed reactor is between 15 and 25 minutes, preferably 20 +/- 2 minute and/or the mean residence time in the calcination reactor is between 30 and 200 minutes. These residence times partic ularly if they are correlated, lowers operation temperatures and avoiding liquid fractions of alkaline.
  • a first recycling line for re circulating hot exhaust gases is provided from the calcination reactor in the circu lating fluidized bed rector and/or in at least one pre-heating stage.
  • a second recycling line for recirculating hot exhaust gases is pro vided from the circulating fluidized bed reactor in at least one pre-heating stage.
  • At least one cooler is provided for cooling the calcine formed in the calcination reactor.
  • a third recycling line for recirculating hot exhaust gases is provided from the cooler in the calcination reactor and/or in the circulating fluidized bed rector and/or in at least one pre-heating stage.
  • a conduit feeds a gas with an oxygen content between 15 and 25% by weight as fluidizing gas into the circulating fluidized bed reactor.
  • the fluidizing gas simultaneously is used as an O2 source for chemical reactions.
  • the use of air or oxygen-enriched air as a cheap oxygen source is preferred.
  • the circulating fluidized bed reactor is configured such that at least 70% by weight of the carbon contained in the ore is removed. Thereby, a reduction of the overall mass flow in the calcining step is achieved. Moreover, the carbon burning provides at least parts of the energy, which is required for the endothermic calcination and which is optimal transported within the circulating fluidized bed.
  • the object of the invention is solved by the presented measures so that the handling of high silicon content aluminosilicate ores based on a semi-dry sin tering process is possible.
  • Combining the known advantages of the semi-dry base process over the established approaches is being achieved at a reasonable en ergy consumption.
  • the invention is also directed to a process according to claim 17.
  • a process contains the steps of (a) mixing aluminum ore with lime stone and so dium and/or potassium carbonate to obtain a mixture and (b) calcining the mixture to calcine.
  • the mixture is pre calcined in a circulating fluidized bed.
  • the moisture content of the mixture or granules introduced in the pre calcining is 10 to 15% by weight, which provides a good stability of the granules.
  • Fig. 1 shows schematically the inventive plant.
  • FIG. 1 shows the principal structure of a plant in accordance with the invention.
  • alumina ore Via conduit 10, alumina ore is fed into a homogenization silo 11, wherein it is mixed with recycled solids and/or limestone from fed in via conduits 13 and 14 to create a mixture.
  • Conduit 15 feeds at least one granulation liquor tank with a salt solution consisting of sodium and potassium carbonates that can be diluted with water injected via conduit 16, if necessary.
  • a salt solution consisting of sodium and potassium carbonates that can be diluted with water injected via conduit 16, if necessary.
  • the mixture as well as the made-up salt solution is then dosed via conduits 17 and 18 to a first granulator 17 where it fulfils three tasks: adding the required amount of alkalis to the solid mixture of limestone, nepheline and dust (and op tionally some recycle materials from the process), providing the moisture for gran ulation and acting as a binder.
  • the granulator 20 also works as a mixing device. Flowever, it is also possible to foresee an addition mixer be fore the granulator 20. It is very advisable but not necessary to have a second granulator 22, preferably connected in in series via conduit 21, to achieve the necessary granulation time, but also to have a good control over the final mois ture. In this context, it is possible to add additional water via conduit 24
  • the dryer 30 Downwards the granulators 20, 22, the produces granules are fed via conduit 23 into a dryer 30. Therein, the wet granules are dried, often with hot flue gases from conduit 63.
  • the dryer 30 is designed as a rotary dryer.
  • the off-gases are passed via conduit 32 in an electrostatic precipitator 33 and from there via conduit 35 in a not-shown off-gas treatment. Via conduit 34, small particles filtered out in the electrostatic precipitator 33 are fed into conduit 45 for recycling.
  • pre-heating section 40 comprises 2 or 3 stages. Further, consecutive venture / cyclone stages lead to particular god results.
  • hot gases fed in via conduit 53, preferably counter-current, can be used.
  • the off-gases from the pre-heating section 40 in an electrostatic precipitator 43 are withdrawn as exhaust gas via conduit 46 and 48 while the other part is transported via conduit 46 and 47 as a gas for carbonization. Filtered particles can be passed via conduit 44 and 45 into the first granulator 20.
  • the granules are passed via conduit 41 in a circulating fluidized bed reactor 50 for pre-calcining, which is in accordance with the invention to en sure the necessary very good heat and mass transfer.
  • the granules are de-carbonization to a degree of minimum 80 wt.-%.
  • the pre-calcined particles are fed via conduit 51 in a calcination reactor 60.
  • fluidizing gas is injected over the bottom nozzle grid. It is preferred that around 20 vol-% of fluidization gas is fresh air, whereby this percentage of fresh air can deviate de pending on the design of the circulating fluidized bed.
  • the bigger part of the fluidizing gas is air from a downward device transferred to the pre-calcina tion reactor via conduits 76, 78, a so-called tertiary air duct.
  • the resulting hot sinter is passed via conduit 61 into a cooler 70, where it is pref erably air-cooled by a grate cooler.
  • the cooler 70 is preferably cooled with air passed in via conduit 73.
  • This air withdrawn and at least partly used as a heat transfer medium in the pre-calcination reactor 50 and the calcining reactor 60. Further, air can be withdrawn via conduit 74 into an electrostatic precipitator 75 and from there via conduit 75 into a not-shown off-gas treatment.
  • Cooled product is withdrawn via conduits 71 , 72, whereby it is possible to admix small particles filtered in the electrostatic precipitator 75.

Landscapes

  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Manufacture And Refinement Of Metals (AREA)
  • Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)

Abstract

L'invention concerne un appareil de traitement d'aluminium comprenant au moins un dispositif de mélange (20, 22, 30, 40) de minerai d'aluminium avec du calcaire et du carbonate de sodium et/ou de potassium pour obtenir un mélange et un réacteur de calcination (60) pour produire le calcinat. Un réacteur à lit fluidisé circulant (50) est disposé entre le dispositif de mélange (20, 22, 30, 40) et le réacteur de calcination (60), le mélange y étant pré-calciné.
PCT/EP2019/082626 2019-11-26 2019-11-26 Procédé semi-sec optimisé pour le frittage d'aluminosilicates dans la production d'alumine WO2021104613A1 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
CN201990001481.4U CN219463345U (zh) 2019-11-26 2019-11-26 用于处理铝的设备
BR212022010130U BR212022010130U2 (pt) 2019-11-26 2019-11-26 Processo semisseco otimizado para sinterização de aluminossilicatos na produção de alumina
PCT/EP2019/082626 WO2021104613A1 (fr) 2019-11-26 2019-11-26 Procédé semi-sec optimisé pour le frittage d'aluminosilicates dans la production d'alumine
AU2022100082A AU2022100082B4 (en) 2019-11-26 2022-06-21 Optimized semi-dry process for sintering of aluminosilicates in the production of alumina
DKBA202200048U DK202200048Y3 (da) 2019-11-26 2022-06-23 Optimeret halvtør proces til sintring af aluminiumsilikater i aluminiumoxidfremstilling

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
PCT/EP2019/082626 WO2021104613A1 (fr) 2019-11-26 2019-11-26 Procédé semi-sec optimisé pour le frittage d'aluminosilicates dans la production d'alumine

Related Child Applications (1)

Application Number Title Priority Date Filing Date
AU2022100082A Division AU2022100082B4 (en) 2019-11-26 2022-06-21 Optimized semi-dry process for sintering of aluminosilicates in the production of alumina

Publications (1)

Publication Number Publication Date
WO2021104613A1 true WO2021104613A1 (fr) 2021-06-03

Family

ID=68699458

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2019/082626 WO2021104613A1 (fr) 2019-11-26 2019-11-26 Procédé semi-sec optimisé pour le frittage d'aluminosilicates dans la production d'alumine

Country Status (4)

Country Link
CN (1) CN219463345U (fr)
BR (1) BR212022010130U2 (fr)
DK (1) DK202200048Y3 (fr)
WO (1) WO2021104613A1 (fr)

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1575871A1 (fr) * 2002-12-23 2005-09-21 Outokumpu Technology Oy Procede et appareil de production d'oxyde metallique a partir de composes metalliques
WO2008113553A1 (fr) * 2007-03-22 2008-09-25 Outotec Oyj Procédé et installation pour la production d'oxyde métallique à partir de sels métalliques
US20120052000A1 (en) * 2009-01-26 2012-03-01 Outotec Oyj Process and plant for producing metal oxide from metal salts
US20150056125A1 (en) * 2006-08-25 2015-02-26 Robert A. Rossi Process and system for producing commercial quality carbon dioxide from recausticizing process calcium carbonates
CN104843751A (zh) * 2015-06-10 2015-08-19 沈阳鑫博工业技术股份有限公司 一种铝土矿活化煅烧低温溶出系统及活化煅烧和溶出方法
EP2969953A2 (fr) * 2013-03-13 2016-01-20 Carbon Engineering Limited Partnership Recueil d'une solution caustique au moyen d'agrégats de cristaux de carbonate de calcium
CN105540627A (zh) 2016-01-19 2016-05-04 中国铝业股份有限公司 一种烧结法生产氧化铝的熟料制备方法
CN107935005A (zh) * 2016-10-12 2018-04-20 北京矿冶研究总院 粉煤灰碳酸盐溶液预处理及氧化铝提取的方法
US20180207598A1 (en) * 2015-06-02 2018-07-26 Outotec (Finland) Oy Process and system for thermal treatment of granular solids

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP1575871A1 (fr) * 2002-12-23 2005-09-21 Outokumpu Technology Oy Procede et appareil de production d'oxyde metallique a partir de composes metalliques
US20150056125A1 (en) * 2006-08-25 2015-02-26 Robert A. Rossi Process and system for producing commercial quality carbon dioxide from recausticizing process calcium carbonates
WO2008113553A1 (fr) * 2007-03-22 2008-09-25 Outotec Oyj Procédé et installation pour la production d'oxyde métallique à partir de sels métalliques
US20120052000A1 (en) * 2009-01-26 2012-03-01 Outotec Oyj Process and plant for producing metal oxide from metal salts
EP2969953A2 (fr) * 2013-03-13 2016-01-20 Carbon Engineering Limited Partnership Recueil d'une solution caustique au moyen d'agrégats de cristaux de carbonate de calcium
US20180207598A1 (en) * 2015-06-02 2018-07-26 Outotec (Finland) Oy Process and system for thermal treatment of granular solids
CN104843751A (zh) * 2015-06-10 2015-08-19 沈阳鑫博工业技术股份有限公司 一种铝土矿活化煅烧低温溶出系统及活化煅烧和溶出方法
CN105540627A (zh) 2016-01-19 2016-05-04 中国铝业股份有限公司 一种烧结法生产氧化铝的熟料制备方法
CN107935005A (zh) * 2016-10-12 2018-04-20 北京矿冶研究总院 粉煤灰碳酸盐溶液预处理及氧化铝提取的方法

Also Published As

Publication number Publication date
CN219463345U (zh) 2023-08-04
DK202200048Y3 (da) 2022-08-12
BR212022010130U2 (pt) 2022-07-12
DK202200048U1 (da) 2022-07-01

Similar Documents

Publication Publication Date Title
US5049198A (en) Calcium sulfate process for the coproduction of Portland cement clinker and concentrated sulfur dioxide adequate to manufacture sulfuric acid
EP3221264B1 (fr) Procédé et appareil de fabrication de composés calcinés pour la production de produits calcinés
CA2745572C (fr) Procede et installation de production d'oxyde metallique a partir de sels metalliques
EP2707666B1 (fr) Procédé de décarbonatation
CA2747370A1 (fr) Procede et installation pour la production d'oxyde metallique a partir de sels metalliques
US4828620A (en) Calcination of calcium carbonate and blend therefor
JPS59111959A (ja) セメントクリンカをか焼するための方法と装置
AU2022100082A4 (en) Optimized semi-dry process for sintering of aluminosilicates in the production of alumina
CN105776268A (zh) 一种以粉煤灰为原料的干法烧成方法
US6569793B2 (en) Fluidized reaction of synthetic silicates
US20120100050A1 (en) Production of calcined lime from natural chalk material in a rotary kiln
WO2021104613A1 (fr) Procédé semi-sec optimisé pour le frittage d'aluminosilicates dans la production d'alumine
US4472202A (en) Process for producing hydraulic cement from dicalcium silicate
US4321239A (en) Method of thermal treatment of a carbonate suspension
CA3162196C (fr) Traitement thermique de matieres premieres minerales a l'aide d'un reacteur a lit fluidise mecanique
KR101854656B1 (ko) 순환유동층 보일러 연소재를 이용한 시멘트 클링커 제조장치 및 제조방법과 이에 의해 제조된 시멘트 클링커
JP3962152B2 (ja) セメントの製造方法
CN102653394A (zh) 用煤在多级多气氛流化床炉中还原石膏生产SO2和CaO
JPS5945624B2 (ja) セメント原料の焼成方法および装置
GB2102407A (en) Producing hydraulic cement from dicalcium silicate

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 19809820

Country of ref document: EP

Kind code of ref document: A1

WWE Wipo information: entry into national phase

Ref document number: 201990001481.4

Country of ref document: CN

REG Reference to national code

Ref country code: BR

Ref legal event code: B01A

Ref document number: 212022010130

Country of ref document: BR

NENP Non-entry into the national phase

Ref country code: DE

ENP Entry into the national phase

Ref document number: 212022010130

Country of ref document: BR

Effective date: 20220525

122 Ep: pct application non-entry in european phase

Ref document number: 19809820

Country of ref document: EP

Kind code of ref document: A1