EP2928988A2 - Verfahren zur aufbereitung von schweröl - Google Patents
Verfahren zur aufbereitung von schwerölInfo
- Publication number
- EP2928988A2 EP2928988A2 EP13802049.0A EP13802049A EP2928988A2 EP 2928988 A2 EP2928988 A2 EP 2928988A2 EP 13802049 A EP13802049 A EP 13802049A EP 2928988 A2 EP2928988 A2 EP 2928988A2
- Authority
- EP
- European Patent Office
- Prior art keywords
- oil
- treated
- heavy
- temperature
- centrifuge
- 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.)
- Granted
Links
- 238000000034 method Methods 0.000 title claims abstract description 33
- 239000010763 heavy fuel oil Substances 0.000 title claims abstract description 20
- 239000003921 oil Substances 0.000 claims abstract description 55
- 238000000926 separation method Methods 0.000 claims abstract description 26
- 239000000446 fuel Substances 0.000 claims abstract description 19
- 239000012071 phase Substances 0.000 claims abstract description 17
- 239000008346 aqueous phase Substances 0.000 claims abstract description 5
- 239000010802 sludge Substances 0.000 claims abstract description 4
- 239000000295 fuel oil Substances 0.000 claims description 46
- 238000010438 heat treatment Methods 0.000 claims description 18
- 230000008569 process Effects 0.000 claims description 11
- 241000282326 Felis catus Species 0.000 claims description 8
- 238000005259 measurement Methods 0.000 description 6
- 238000002485 combustion reaction Methods 0.000 description 5
- 239000007787 solid Substances 0.000 description 4
- 230000001419 dependent effect Effects 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 229920006395 saturated elastomer Polymers 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- XLYOFNOQVPJJNP-ZSJDYOACSA-N Heavy water Chemical compound [2H]O[2H] XLYOFNOQVPJJNP-ZSJDYOACSA-N 0.000 description 2
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 2
- 230000033228 biological regulation Effects 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 239000010779 crude oil Substances 0.000 description 2
- 238000005265 energy consumption Methods 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000009467 reduction Effects 0.000 description 2
- 238000012958 reprocessing Methods 0.000 description 2
- 239000007790 solid phase Substances 0.000 description 2
- XUIMIQQOPSSXEZ-UHFFFAOYSA-N Silicon Chemical compound [Si] XUIMIQQOPSSXEZ-UHFFFAOYSA-N 0.000 description 1
- 230000009471 action Effects 0.000 description 1
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 1
- 229910052782 aluminium Inorganic materials 0.000 description 1
- 230000008859 change Effects 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 229910052681 coesite Inorganic materials 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 230000001276 controlling effect Effects 0.000 description 1
- 238000005336 cracking Methods 0.000 description 1
- 229910052906 cristobalite Inorganic materials 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 230000003137 locomotive effect Effects 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000002360 preparation method Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 238000004062 sedimentation Methods 0.000 description 1
- 229910052710 silicon Inorganic materials 0.000 description 1
- 239000010703 silicon Substances 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- 235000012239 silicon dioxide Nutrition 0.000 description 1
- 239000007858 starting material Substances 0.000 description 1
- 229910052682 stishovite Inorganic materials 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 229910052905 tridymite Inorganic materials 0.000 description 1
- 239000002351 wastewater Substances 0.000 description 1
Classifications
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/10—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for with the aid of centrifugal force
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
- C10G31/06—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G33/00—Dewatering or demulsification of hydrocarbon oils
- C10G33/06—Dewatering or demulsification of hydrocarbon oils with mechanical means, e.g. by filtration
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G33/00—Dewatering or demulsification of hydrocarbon oils
- C10G33/08—Controlling or regulating
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4068—Moveable devices or units, e.g. on trucks, barges
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
Definitions
- the present invention relates to a process for the treatment of heavy oil on board ships, for use as fuel, in particular for a diesel engine.
- Diesel manufacturers are even to comply with even lower upper limits of 20 ppm or even 15 ppm or 10 ppm or even 5 ppm. This can be achieved in particular on board ships with the least possible effort.
- a known plant for the treatment of heavy oil on board ships shows Fig. 2.
- Output temperature TO is first freed of coarse solids in a strainer 103, such as a sieve. Then, the heavy oil is passed with a pump 104 through a heat exchanger 105, in which it is heated to a temperature of up to 98 °.
- the refined heavy oil phase - the "pure oil" - OIL2 is diverted from the separator 107 for further use by a discharge line 10, where it may be directed to an intermediate tank (not shown) or directly sent to combustion in a diesel engine
- Heat exchanger 104 is preferably used as the heat energy releasing medium
- the invention solves this problem by a method having the features of claim 1 and the independent claim 11.
- the at least temporary or permanent increase of the separation temperature according to claim 1 improves the separation efficiency.
- lower and at the higher temperatures of more than 100 ° C or more than 105 ° C or more than 1 10 ° C or even more than 1 15 ° C in each case even lower cat-fines in pure oil can be achieved.
- the optional heating in two stages is particularly advantageous. On the one hand, it is necessary to increase the temperature to the very high separation temperature only immediately before the actual separation process.
- the multiple and especially two-stage heating of the heavy fuel oil to be treated makes it possible to use the "pure oil” heated to the separating temperature and from the at least one centrifuge, in particular the (three-phase) separator, to flow through a heat exchanger in countercurrent Heat to be delivered to the "feed fuel” to be cleaned in order to heat it to a first temperature T1, which is still lower than the separation temperature T2. This reduces the total amount of heat necessary for heating the heavy oil to the separation temperature T2 and keeps the clean oil temperature in the subsequent pipes below the temperature T2 of otherwise possibly more than 100 ° C.
- Sensor device determines the cat fines content (Cat Fines OUT), f) the one or more certain cat-fines content from step d) and / or e) are used as actual variables of a control process and it is or will be based on the determined actual variables with a control device regulating particular the
- FIG. 1 shows a plant according to the invention for the treatment of heavy oil.
- Fig. 2 is an already known plant for the treatment of heavy oil
- FIG. 4 shows a tank arrangement for storing heavy oils with a
- a heavy oil OIL1 which flows into and out of a tank HT1, is first freed of coarse solids in a strainer 3, such as a sieve, through a line 1 (in which a valve 2 is connected here).
- the heavy fuel oil to be treated OIL1 - preferably by means of a pump 4 - from a tank T1, in which it has an outlet temperature TO, for example 40 ° to 60 ° C, passed through a first heating device, in particular a first heat exchanger 5A, in which it on a first relative to the outlet temperature higher temperature T1> TO of preferably less than 95 °, in particular 60 ° to 80 ° C, is heated.
- a first heating device in particular a first heat exchanger 5A, in which it on a first relative to the outlet temperature higher temperature T1> TO of preferably less than 95 °, in particular 60 ° to 80 ° C, is heated.
- the heated to the first temperature T1 heavy oil is by a
- This temperature T2 is greater than 98 ° C, preferably greater than 100 ° C, in particular greater than 105 ° C and preferably even greater than 1 10 ° C.
- Separation temperatures of up to 125 ° appear to be useful at the present time, the range between 100 ° and 15 ° C. being particularly preferred, since in this area the outlay on equipment is still easy to control, but on the other hand particularly good separation results with regard to the separation of the catalyst. Fines can be achieved.
- the heavy oil OIL1 heated to the second temperature T2 is passed directly into at least one centrifuge, here a three-phase separating separator 7, in which a wastewater phase W is separated from the heavy oil, which flows off through a discharge 8 and into which it is cleaned of a solid phase S, which is discharged through a discharge line 9.
- the clarification of solids and the separation of the water from the oil phase can also be done in two successive centrifuges (clarifier and phase separator). According to FIG. 2, there is also a process water supply P at the separator 7
- the oil from the exit from the second heat exchanger to the inlet to the centrifuge requires only a very short time, so that it flows directly from the second heating device, here the second heat exchanger 5B, into the
- Centrifuge here a three-phase Trennseparator 107 is passed or arrives. It is advantageous in this procedure that the heavy oil can not lose heat before reaching the centrifuge or heat to a practically relevant extent, which would worsen the treatment process.
- the treated heavy oil phase - hereinafter referred to as OIL2 or synonymously also "pure oil” - is discharged through the outlet 10 from the separator 7 to the other
- the pure oil before being introduced into a tank or in a
- the internal combustion engine is first used as the heat energy dissipating medium of the first heat exchanger 5A and passed therethrough to
- heavy oil leaving the separator 7 is advantageously used to heat the heavy oil to the first temperature T1 in the first heat exchanger 5A and, on the other hand, to cool the heated pure oil so that it can be stored more easily.
- the energy recovery significantly increases the efficiency of the treatment process, as the energy consumption for
- Heating the heavy oil is lowered to the Separiertemperatur total.
- the second heat exchanger 5B can be used as the heat energy dissipating medium in particular saturated steam HT or another suitable medium with which then only the heavy oil from the first temperature T1 must be heated to the second temperature T2.
- the determined measured values are then advantageously forwarded to a processing unit, not shown here, which is used as a control and control device for controlling the system shown in FIG. 1 and which regulates in particular the separating temperature T1 and / or the flow rate with the pump 4 on the basis of the determined actual variables established.
- the regulation can be carried out as described above, but alternatively, if appropriate, also in real time with online measurements of the cat-fines content.
- the treatment process can be precisely regulated.
- the above-mentioned cat-fines content which is to be kept below a desired actual value, can be used as controlled variables, the actual fuel consumption of the internal combustion engine as the actual value and / or the actual water level in a clean oil tank.
- Processing methods are regulated as a function of one or more of the following measured variables or actual variables:
- the described - at least temporary increase - the separation temperature to more than 98 ° C improves the separation efficiency and allows the achievement of lowest cat-fines content.
- the proportion of abrasive cat-fines can be easily reduced below engine builder limits, which may well be well below 20ppm or even below 15ppm or 10ppm or lower. With further increased temperature, the result of the separation process is further improved, but at temperatures up to 1 15 ° C the apparative
- the heavy oil preferably in several stages to the separation temperature T2 of more than 98 °, in particular more than 100 ° C. or 105 ° C. or more, and to perform the separation process at this separation temperature T2.
- the multi-stage economy is further increased because there is the possibility of energy recovery. It is also conceivable, the heavy oil directly in only a single heating device on the
- Fig. 3 shows a particularly advantageous tank arrangement with several tanks, which are connected in a particularly advantageous manner with each other and with the system of Figure 2.
- Fig. 3 the heat exchanger and further details of FIG.
- two setting tanks ST1, ST2 are provided here and two service tanks ST3, ST4, into which, depending on requirements, either pure oil OIL2 or heavy fuel oil OIL1 to be treated can be introduced.
- the line 10 therefore branches into all these tanks ST1 to ST4.
- the tanks ST1 to ST4 further each have at least one derivative. These derivatives can be opened in each case with valves V1 to V4 in the desired manner.
- This arrangement is particularly flexible to handle and offers opportunities for storage of oils of various qualities as well as for the preparation of oils that have been stored in the tanks for a long time by the oil first "in a circle "is led out of the tanks, then" pre-treated "at a lower temperature to 98 ° C, for example, and then returned to the same tank.
- the embodiment of FIG. 4 largely corresponds to that of FIG. 3, but is supplemented by an overflow-dependent pump control.
- the service tanks ST3 and ST4 have at least one overflow line 201, 202 to the service tanks ST1 and ST2.
- overflow lines 201, 202 are preferably in the lower region of
- FIC Flow Indicator
- control device 203 which here only or u.a. the flow rate in the overflow lines used as actual size, which they are taken into account in the control of the pump 204 advantageously used with.
Landscapes
- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Mechanical Engineering (AREA)
- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
DE102012112026.9A DE102012112026A1 (de) | 2012-12-10 | 2012-12-10 | Verfahren zur Aufbereitung von Schweröl |
PCT/EP2013/075895 WO2014090717A2 (de) | 2012-12-10 | 2013-12-09 | Verfahren zur aufbereitung von schweröl |
Publications (2)
Publication Number | Publication Date |
---|---|
EP2928988A2 true EP2928988A2 (de) | 2015-10-14 |
EP2928988B1 EP2928988B1 (de) | 2022-11-23 |
Family
ID=49725131
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP13802049.0A Active EP2928988B1 (de) | 2012-12-10 | 2013-12-09 | Verfahren zur aufbereitung von schweröl |
Country Status (9)
Country | Link |
---|---|
US (1) | US20160122661A1 (de) |
EP (1) | EP2928988B1 (de) |
JP (1) | JP2016509075A (de) |
KR (1) | KR102172671B1 (de) |
CN (1) | CN105051160A (de) |
BR (1) | BR112015012698A2 (de) |
DE (1) | DE102012112026A1 (de) |
SG (1) | SG11201504533SA (de) |
WO (1) | WO2014090717A2 (de) |
Families Citing this family (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB201515921D0 (en) * | 2015-09-08 | 2015-10-21 | Parker Hannifin Mfg Uk Ltd | Method |
PL3290093T3 (pl) | 2016-09-06 | 2022-07-04 | Alfa Laval Corporate Ab | Metoda oczyszczania oleju napędowego do silnika wysokoprężnego |
EP3421573A1 (de) * | 2017-06-28 | 2019-01-02 | Alfa Laval Corporate AB | Kraftstoffbehandlungssystem für einen motor und verfahren zur behandlung einer heizöl unter verwendung von dem system |
GR1009618B (el) * | 2017-12-21 | 2019-10-14 | Ευαγγελος Γεωργιου Δουσης | Συστημα αυτοματης ρυθμισης, βελτιστης παροχης και παρακολουθησης φυγοκεντρικων διαχωριστηρων καυσιμου |
SG11202011450RA (en) * | 2018-05-18 | 2020-12-30 | Hibd Laboratory Ass | Production method for bio-jet fuel |
ES2883410B2 (es) | 2020-05-25 | 2022-04-20 | Delgado Joan Serra | Sistema y metodo para la gestion integral de residuos marpol i, a bordo de un buque |
KR102630831B1 (ko) | 2023-06-22 | 2024-01-29 | 주)씨에스캠 | 중유의 탄화물질 제거장치 |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2181744A1 (de) * | 2008-10-29 | 2010-05-05 | Citec Engineering Oy AB | Verfahren und Vorrichtung zum Trennen von Wasser und Feststoffen aus Schweröl |
Family Cites Families (9)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB765478A (en) * | 1954-04-10 | 1957-01-09 | Westfalia Separator Ag | Process and apparatus for purifying heavy fuel oils |
US3692668A (en) * | 1971-03-03 | 1972-09-19 | Texaco Inc | Process for recovery of oil from refinery sludges |
JPS5540203A (en) * | 1978-08-08 | 1980-03-21 | Mitsui Eng & Shipbuild Co Ltd | Crude heavy oil supplying method of diesel engine for ship |
EP0502404B1 (de) * | 1991-03-04 | 1996-05-01 | Federico Esteban Dr. Lantos | Verfahren zur Verringerung des Verunreinigungsgrades von Brennstoffen |
US7255670B2 (en) * | 2004-03-04 | 2007-08-14 | Hutchison Hayes, L.P. | Three phase decanter centrifuge |
CN101633849B (zh) * | 2009-08-21 | 2013-03-27 | 广东新华粤石化股份有限公司 | 脱除催化裂化油浆中催化剂粉末的方法 |
US8747658B2 (en) * | 2010-07-27 | 2014-06-10 | Phillips 66 Company | Refinery desalter improvement |
KR101312345B1 (ko) * | 2010-09-03 | 2013-09-27 | 주식회사 삼공사 | 분리판형 원심분리기 및 그 운전방법 |
EP2530135B1 (de) * | 2011-05-30 | 2022-05-25 | GEA Mechanical Equipment GmbH | Verfahren zur Klärung von Pyrolyseöl |
-
2012
- 2012-12-10 DE DE102012112026.9A patent/DE102012112026A1/de not_active Ceased
-
2013
- 2013-12-09 JP JP2015546045A patent/JP2016509075A/ja active Pending
- 2013-12-09 CN CN201380064399.3A patent/CN105051160A/zh active Pending
- 2013-12-09 KR KR1020157017960A patent/KR102172671B1/ko active IP Right Review Request
- 2013-12-09 US US14/650,263 patent/US20160122661A1/en not_active Abandoned
- 2013-12-09 SG SG11201504533SA patent/SG11201504533SA/en unknown
- 2013-12-09 WO PCT/EP2013/075895 patent/WO2014090717A2/de active Application Filing
- 2013-12-09 EP EP13802049.0A patent/EP2928988B1/de active Active
- 2013-12-09 BR BR112015012698A patent/BR112015012698A2/pt not_active Application Discontinuation
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2181744A1 (de) * | 2008-10-29 | 2010-05-05 | Citec Engineering Oy AB | Verfahren und Vorrichtung zum Trennen von Wasser und Feststoffen aus Schweröl |
Also Published As
Publication number | Publication date |
---|---|
KR20150093765A (ko) | 2015-08-18 |
EP2928988B1 (de) | 2022-11-23 |
DE102012112026A1 (de) | 2014-06-12 |
JP2016509075A (ja) | 2016-03-24 |
BR112015012698A2 (pt) | 2017-07-11 |
CN105051160A (zh) | 2015-11-11 |
KR102172671B1 (ko) | 2020-11-02 |
US20160122661A1 (en) | 2016-05-05 |
WO2014090717A2 (de) | 2014-06-19 |
KR102172671B9 (ko) | 2022-02-14 |
SG11201504533SA (en) | 2015-07-30 |
WO2014090717A3 (de) | 2015-08-27 |
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