EP2928988B1 - Verfahren zur aufbereitung von schweröl - Google Patents

Verfahren zur aufbereitung von schweröl Download PDF

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Publication number
EP2928988B1
EP2928988B1 EP13802049.0A EP13802049A EP2928988B1 EP 2928988 B1 EP2928988 B1 EP 2928988B1 EP 13802049 A EP13802049 A EP 13802049A EP 2928988 B1 EP2928988 B1 EP 2928988B1
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EP
European Patent Office
Prior art keywords
heavy oil
oil
processing
temperature
centrifuge
Prior art date
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Active
Application number
EP13802049.0A
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German (de)
English (en)
French (fr)
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EP2928988A2 (de
Inventor
Jürgen Mackel
Christian Bruns
Heiko Sims
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GEA Mechanical Equipment GmbH
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GEA Mechanical Equipment GmbH
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Application filed by GEA Mechanical Equipment GmbH filed Critical GEA Mechanical Equipment GmbH
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    • 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 method for processing heavy oil on board ships for use as fuel, in particular for a diesel engine.
  • a "heavy oil” (English Heavy Fuel Oil, HFO) is a residual oil from distillation or from cracking plants in petroleum processing and is used as a fuel for large diesel engines, such as those in ships and for steam locomotives with oil main firing or in power plants to generate electricity.
  • HFO English Heavy Fuel Oil
  • MFO Marine (Residual) Fuel Oil
  • Bunker C Bunker C is also used.
  • the proportion of the so-called abrasive catalyst fines in the heavy oil to be processed as a starting material of the prior art and also of the process according to the invention should if possible already be below an upper limit below 60 mg/kg (ppm). Then this content of catalyst fines should be significantly reduced, in particular so that the abrasive substances do not damage the diesel engine. According to the regulations of the diesel manufacturers, even significantly lower upper limits of 20 ppm or even 15 ppm or 10 ppm or even 5 ppm should be observed in this regard. This can be achieved in particular on board ships with as little effort as possible.
  • the EP 2 530 135 A1 discloses a method for processing pyrolysis oil.
  • the EP 2 181 744 A1 discloses a process for refining oil through a separator and centrifuge sequence.
  • This oil can be heated before reaching the centrifuge, heating means being arranged at the inlet of the centrifuge.
  • the inlet and/or outlet is checked for density and/or temperature.
  • the density can be checked, for example, by measuring conductivity in order to obtain information on the water content in the oil.
  • a well-known plant for processing heavy fuel oil on board ships is shown 2 .
  • the heated heavy oil is conducted through a line section 106 into a centrifuge, here a three-phase separator 107, in which a dirty water phase W is separated from the heavy oil, which flows off through a drain line 108 and in which it is separated from a solid phase S is cleaned, which contains the abrasive catalyst fines and which is discharged through a discharge line 109.
  • the processed heavy oil phase - the "pure oil” - OIL2 is derived through a derivative 110 from the separator 107 for further use. It can be fed into an intermediate tank (not shown here) or fed directly to combustion in a diesel engine.
  • Thermal oil or saturated steam (“saturated or hot steam” or also referred to below as "HS”) is preferably fed to the heat exchanger 104 as the heat energy-emitting medium, the heat energy of which is used to heat the heavy oil in countercurrent.
  • the invention solves this problem by a method with the features of claim 1.
  • the at least temporary or permanent increase in the separating temperature according to claim 1 improves the separating efficiency. In this way, lower and at the higher temperatures of more than 100° C. or more than 105° C. or more than 110° C. or even more than 115° C. still lower catalyst fines contents in the clean oil can be achieved.
  • the optional heating in two stages is also particularly advantageous. On the one hand, the temperature needs to be increased to the very high separating temperature only immediately before the actual separating process.
  • the multiple and in particular two-stage heating of the heavy oil to be processed allows the "pure oil” heated to the separation temperature and derived from the at least one centrifuge, in particular the (three-phase) separator, to be used to flow through a heat exchanger in order to countercurrently Dissipate heat to the "feed fuel" to be cleaned in order to heat it to a first temperature T1, which is, however, still lower than the separating temperature T2. This reduces the total amount of heat required to heat the heavy oil to the separation temperature T2 and keeps the clean oil temperature in the downstream pipelines below the temperature T2, which may otherwise be more than 100°C.
  • Fig.1 When creating the Fig.1 is first fed through a line 1 (in which a valve 2 is switched here) from a tank HT1 to be processed heavy oil OIL1 preferably freed from coarse solids in a strainer 3 such as a sieve.
  • the heavy oil OIL1 to be processed is then conveyed - preferably with the aid of a pump 4 - from a tank T1, in which it has an initial temperature T0 of, for example, 40° to 60° C, through a first heating device, in particular a first heat exchanger 5A, in which it is heated to a first temperature T1 > T0, which is higher than the initial temperature and is preferably less than 95° C., in particular 60° to 80° C.
  • the heavy oil heated to the first temperature T1 is conducted through a line section 6 into a second heating device, preferably a second heat exchanger 5B, in which it is at least temporarily or permanently increased to a temperature higher than that of the first Temperature T1 even higher second temperature T2 is heated.
  • This temperature T2 is greater than 98°C, preferably greater than 100°C, in particular greater than 105°C and preferably even greater than 110°C.
  • Separation temperatures of up to 125°C currently appear to be sensible, with the range between 100° and 115°C being particularly preferred, since in this range the expenditure on equipment can still be well controlled, but on the other hand particularly good separation results are achieved with regard to the separation of the catalyst fines be achieved.
  • the heavy oil OIL1 which has been heated to the second temperature T2 is fed directly into at least one centrifuge, here a three-phase separator 7, in which a dirty water phase W is separated from the heavy oil, which flows off through a discharge line 8 and is it is cleaned of a solid phase S, which is discharged through a discharge line 9.
  • Solids can also be clarified and the water phase separated from the oil phase in two centrifuges connected in series (clarifier and phase separator).
  • a process water supply P is also provided on the separator 7 .
  • the oil preferably only needs a very short time from exiting the second heat exchanger to entering the centrifuge, so that it is fed directly from the second heating device, here the second heat exchanger 5B, into the centrifuge, here a three-phase separator 107 or reached.
  • the advantage of this procedure is that the heavy oil cannot lose any or only a practically relevant amount of heat before it reaches the centrifuge, which would impair the treatment process.
  • the processed heavy oil phase - hereinafter referred to as OIL2 or synonymously "pure oil” - is discharged through the discharge line 10 from the separator 7 for further use.
  • the clean oil is preferably first used as the heat energy-releasing medium of the first heat exchanger 5A or passed through it in order to deliver heat energy to the inflowing heavy oil to be treated.
  • heavy oil emerging from 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 is particularly easier to store.
  • the energy recovery significantly increases the profitability of the treatment process, as the energy consumption for heating the heavy oil to the separation temperature is reduced overall.
  • saturated steam HT or another suitable medium can be used as the heat energy-emitting medium, with which only the heavy oil then has to be heated from the first temperature T1 to the second temperature T2.
  • heavy fuel oil to be treated can first be circulated through the two heat exchangers 5A and 5B and then back into the tank T1 (indicated by the line 13 and the two-way valve 14) when starting up.
  • a sensor device 11 to carry out measurements of the catalyst fines content in the crude oil to be treated (Cat Fines IN) fed to the separator in the heavy oil to be treated, for example before heating.
  • the same sensor device 11 or a second sensor device 12 is preferably used to measure the cat fines content (Cat Fines IN) in the cleaned or processed clean oil that is draining off, for example directly in the clean oil that is drained from the separator.
  • the proportion of fines with an average diameter below a limit value can be determined.
  • a limit value in particular less than 10 ⁇ m
  • These measurements do not have to be directly real-time. Rather, samples can also be taken (eg at intervals of a few hours) - which are then examined for the catalyst fines content using suitable sensor equipment - such as is commercially available.
  • the measured values determined are then advantageously sent to a computing unit, not shown here, which acts as a regulation and control device for controlling the 1 shown plant is used and which regulates in particular the separating temperature T1 and/or the throughput with the pump 4 on the basis of the determined actual variables.
  • the regulation can take place as described above, but alternatively also in real time with online measurements of the catalyst fines content.
  • the above-mentioned catalyst fines content which is to be kept below a desired actual value
  • the current fuel consumption of the internal combustion engine as an actual value and/or the actual level in a clean oil tank can be used as control variables.
  • a reduction in throughput increases separation efficiency.
  • the electrical energy consumption is also reduced when the inflow pump speed is reduced.
  • the described - at least temporary increase - of the separation temperature to more than 98° C improves the separation efficiency and enables the lowest catalyst fines content to be achieved.
  • Catalyst abrasive fines levels can easily be reduced below engine builder limits, which can be well below 20ppm or even 15ppm or 10ppm or lower.
  • the result of the separating process is further improved with a further increase in temperature, although at temperatures up to 115° C. the equipment requirements are lower than for even higher temperatures.
  • the heavy oil preferably in several stages, to the separating temperature T2 of more than 98°, in particular more than 100° C. or 105° C. or more, and to carry out the separating process at this separating temperature T2. Due to the multi-stage design, the economic efficiency is further increased, as there is the possibility of energy recovery. However, it is also conceivable for the heavy oil to be warmed or heated directly to the separating temperature T2 in just a single heating device.
  • FIG. 3 shows a particularly advantageous tank arrangement with several tanks, which in a particularly advantageous manner with each other and with the plant Fig.2 are connected.
  • the heat exchangers and other details of 1 not shown to improve clarity.
  • two settling tanks ST1, ST2 are provided and two service tanks ST3, ST4, into which either clean oil OIL2 or heavy oil to be processed OIL1 can be introduced as required.
  • the line 10 therefore branches into all of these tanks ST1 to ST4.
  • the tanks ST1 to ST4 each have at least one discharge line. These derivations can each be opened in the desired manner with valves V1 to V4. All derivations also flow into the supply line 1 of the 2 .
  • This arrangement can be handled particularly flexibly and offers options for storing oils of different qualities as well as for pre-processing oils that have been stored in the tanks for a long time by first circulating the oil out of the tanks, then at a lower temperature, for example is "pretreated" to 98°C, and then sent back to the same tank.
  • the embodiment of 4 largely corresponds to that of 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 to be arranged in the lower area of the service tanks ST3 and ST4 in order to be able to return any sediment to the service tanks ST1 and ST2.

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  • 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)
EP13802049.0A 2012-12-10 2013-12-09 Verfahren zur aufbereitung von schweröl Active EP2928988B1 (de)

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 EP2928988A2 (de) 2015-10-14
EP2928988B1 true 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 (pt)
EP (1) EP2928988B1 (pt)
JP (1) JP2016509075A (pt)
KR (1) KR102172671B1 (pt)
CN (1) CN105051160A (pt)
BR (1) BR112015012698A2 (pt)
DE (1) DE102012112026A1 (pt)
SG (1) SG11201504533SA (pt)
WO (1) WO2014090717A2 (pt)

Families Citing this family (8)

* Cited by examiner, † Cited by third party
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 (en) * 2017-06-28 2019-01-02 Alfa Laval Corporate AB Fuel treatment system for an engine and a method using the system
GR1009618B (el) * 2017-12-21 2019-10-14 Ευαγγελος Γεωργιου Δουσης Συστημα αυτοματης ρυθμισης, βελτιστης παροχης και παρακολουθησης φυγοκεντρικων διαχωριστηρων καυσιμου
CN112189046B (zh) * 2018-05-18 2023-03-28 一般社团法人HiBD研究所 生物喷气燃料的制造方法
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
EP4428215A1 (en) * 2023-03-09 2024-09-11 Alfa Laval Corporate AB Method for operating a system comprising a centrifugal separator
KR102630831B1 (ko) 2023-06-22 2024-01-29 주)씨에스캠 중유의 탄화물질 제거장치

Citations (1)

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Publication number Priority date Publication date Assignee Title
EP2181744A1 (en) * 2008-10-29 2010-05-05 Citec Engineering Oy AB Method and arrangement for separating water and particular material from heavy fuel oil

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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 (en) * 1991-03-04 1996-05-01 Federico Esteban Dr. Lantos Method for decreasing the level of contamination of fuels
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
EP2598606A2 (en) * 2010-07-27 2013-06-05 Phillips 66 Company Refinery desalter improvement
WO2012029167A1 (ja) * 2010-09-03 2012-03-08 三菱化工機株式会社 分離板型遠心分離機及びその運転方法
EP2530135B1 (de) * 2011-05-30 2022-05-25 GEA Mechanical Equipment GmbH Verfahren zur Klärung von Pyrolyseöl

Patent Citations (1)

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Publication number Priority date Publication date Assignee Title
EP2181744A1 (en) * 2008-10-29 2010-05-05 Citec Engineering Oy AB Method and arrangement for separating water and particular material from heavy fuel oil

Also Published As

Publication number Publication date
JP2016509075A (ja) 2016-03-24
CN105051160A (zh) 2015-11-11
WO2014090717A2 (de) 2014-06-19
US20160122661A1 (en) 2016-05-05
KR20150093765A (ko) 2015-08-18
WO2014090717A3 (de) 2015-08-27
EP2928988A2 (de) 2015-10-14
DE102012112026A1 (de) 2014-06-12
BR112015012698A2 (pt) 2017-07-11
SG11201504533SA (en) 2015-07-30
KR102172671B1 (ko) 2020-11-02
KR102172671B9 (ko) 2022-02-14

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