US20160122661A1 - Method for Treating Heavy Fuel Oil - Google Patents

Method for Treating Heavy Fuel Oil Download PDF

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Publication number
US20160122661A1
US20160122661A1 US14/650,263 US201314650263A US2016122661A1 US 20160122661 A1 US20160122661 A1 US 20160122661A1 US 201314650263 A US201314650263 A US 201314650263A US 2016122661 A1 US2016122661 A1 US 2016122661A1
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United States
Prior art keywords
heavy oil
oil
centrifuge
heating
temperature
Prior art date
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Abandoned
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US14/650,263
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English (en)
Inventor
Juergen Mackel
Chrisian 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
Assigned to GEA MECHANICAL EQUIPMENT GMBH reassignment GEA MECHANICAL EQUIPMENT GMBH ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: BRUNS, CHRISTIAN, SIMS, HEIKO, MACKEL, JUERGEN
Publication of US20160122661A1 publication Critical patent/US20160122661A1/en
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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 on-ship processing of heavy oil, for use as a fuel, especially for a diesel engine.
  • a “heavy oil” (heavy fuel oil, HFO) is a residue oil from distillation or from cracking plants in mineral oil processing, and serves as a fuel for large diesel engines, as used, for example, on ships and for steam locomotives with oil firing or in power plants for power generation.
  • the international trade designation of such an oil is: marine (residual) fuel oil (MFO); the US term Bunker C is sometimes also used.
  • the proportion of the so-called abrasive catalyst fines in the heavy oil for processing as starting material in the prior art and also in the process according to the invention should if at all possible already be below an upper limit of below 60 mg/kg (ppm). Then this content of catalyst fines is to be distinctly lowered, especially in order that the abrasives do not damage the diesel engine. According to specifications from diesel constructors, in this regard, even markedly lower upper limits of 20 ppm or even 15 ppm or 10 ppm or even 5 ppm should be complied with. This is to be achievable in particular on board ships with a minimum level of complexity.
  • FIG. 2 A known system for processing heavy oil on board ships is shown in FIG. 2 .
  • Heavy oil OIL 1 which is to be processed and flows in through a conduit 101 (here with a valve 102 connected therein) from a tank, which is not shown, and has a starting temperature T 0 is first freed of coarse solids in a soil trap 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 heated heavy oil is passed out of the heat exchanger 105 through a conduit section 106 into a centrifuge, a three-phase separator 107 here, in which a soil/water phase W is separated from the heavy oil and flows away through an outlet 108 , and in which it is cleaned to free it of a solid phase S which contains the abrasive catalyst fines and which is removed via an outlet 109 .
  • the processed heavy oil phase—the “clean oil”—OIL 2 is passed out of the separator 107 through an outlet 110 for further use. It can be passed here into an intermediate tank (not shown here) or fed directly to combustion in a diesel engine.
  • the heat exchanger 104 is preferably fed with thermal oil or saturated or hot steam (also referred to hereinafter as “HS”) as thermal energy-releasing medium, from which the thermal energy serves to heat the heavy oil in countercurrent.
  • HS thermal oil or saturated or hot steam
  • This method is to be improved further.
  • the invention achieves this object by a method having the features of claim 1 and of the further independent claim 11 .
  • the at least intermittent or permanent increase in the separation temperature according to claim 1 increases the separation efficiency. In this way, lower catalyst fines contents 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., even lower catalyst fines contents in each case can be achieved in the clean oil.
  • An additional particularly advantageous feature is the optional heating in two stages. Firstly, in this way, the increase in the temperature to the very high separation temperature need not be effected until immediately before the actual separating operation.
  • the multistage and especially two-stage heating of the heavy oil for processing allows the “clean oil” which has been heated to the separation temperature and conducted out of the at least one centrifuge, especially the (three-phase) separator, to be utilized for flow through a heat exchanger in order to release heat in countercurrent to the “feed fuel” to be cleaned, in order to heat it to a first temperature T 1 , but one which is still lower than the separation temperature T 2 . This reduces the amount of heat needed overall for heating of the heavy oil to the separation temperature T 2 , and keeps the clean oil temperature in the downstream pipelines below the temperature T 2 of otherwise possibly more than 100° C.
  • the invention of claim 11 additionally achieves optimized closed-loop control of a generic method but also of a method of the invention as claimed in any of claims 1 to 10 .
  • an advantageous method as claimed in any of the preceding claims or method for on-ship processing of heavy oil which is to be utilized as fuel for a diesel engine, having the following steps: a) providing heavy oil (OIL 1 ) for processing; b) passing the heavy oil (OIL 1 ) provided and for processing from step a), especially using at least one pump, onward into a centrifuge, with heating of the heavy oil for processing before it reaches the centrifuge to a separation temperature of—preferably—more than 98° C., and c) separating an aqueous phase and a sludge phase from a clean oil phase (OIL 2 ) in the centrifuge, also with performance of one or more of the following steps d) to f): d) the catalyst fines content (Cat Fines IN) in the incoming heavy oil for processing—especially prior to heating—is determined with a sensor device, e) the catalyst fines content (Cat Fines OUT) in the outgoing cleaned or processed clean oil is determined with the or a second sensor
  • FIG. 1 a plant of the invention for processing heavy oil
  • FIG. 2 an already known plant for processing heavy oil
  • FIG. 3 a tank arrangement for storing heavy oils
  • FIG. 4 a tank arrangement for storing heavy oils having an overflow-dependent closed-loop pump control system.
  • heavy oil OIL 1 for processing which flows in through a conduit 1 (here with a valve 2 connected therein) from a tank HT 1 , is first preferably freed of coarse solids in a soil trap 3 such as a sieve.
  • the heavy oil OIL 1 for processing preferably with the aid of a pump 4 —is passed from a tank T 1 in which it has a starting temperature T 0 of, for example, 40° to 60° C. through a first heating device, especially a first heat exchanger 5 A, in which it is heated to a first temperature T 1 >T 0 , higher relative to the starting temperature, of preferably less than 95, especially 60° to 80° C.
  • a first heating device especially a first heat exchanger 5 A, in which it is heated to a first temperature T 1 >T 0 , higher relative to the starting temperature, of preferably less than 95, especially 60° to 80° C.
  • the heavy oil heated to the first temperature T 1 is passed from the first heating device, especially the first heat exchanger 5 A, through a conduit section 6 into a second heating device, preferably a second heat exchanger 5 B, in which it is heated at least intermittently or permanently to an even higher second temperature T 2 compared to the first elevated temperature T 1 .
  • This temperature T 2 is greater than 98° C., preferably greater than 100° C., especially greater than 105° C. and preferably even greater than 110° C.
  • Separation temperatures of up to 125° seem advisable at present, particular preference being given to the range between 100° and 115° C., since the apparatus complexity can still be controlled efficiently within this range, but, on the other hand, particularly good separation results are achieved in terms of the removal of catalyst fines.
  • the heavy oil OIL 1 heated to the second temperature T 2 is passed out of the second heat exchanger 5 B directly into at least one centrifuge, here a three-phase separator 7 , in which a soil/water phase W is separated from the heavy oil and flows away through an outlet 8 , and in which it is cleaned to free it of a solid phase S which is removed via an outlet 9 .
  • the clarifying to remove solids and the separation of the water phase from the oil phase can also be effected in two series-connected centrifuges (clarifier and phase separator). According to FIG. 2 , in addition, a process water supply P is provided in the separator 7 .
  • the oil takes only a very short time from passing out of the 2nd heat exchanger until it enters the centrifuge, in order that it is passed or passes directly from the second heating device, the second heat exchanger 5 B here, into the centrifuge, a three-phase separator 107 here.
  • a three-phase separator 107 here.
  • OIL 2 processed heavy oil phase
  • clean oil hereinafter
  • the clean oil before being introduced into a tank or into an internal combustion engine, is first used as thermal energy-releasing medium in the first heat exchanger 5 A, i.e. passed through it, in order to release thermal energy to the incoming heavy oil for processing.
  • the thermal energy-releasing medium used may especially be saturated or hot steam HT or another suitable medium, with which it is then merely necessary to heat the heavy oil from the first temperature T 1 to the second temperature T 2 .
  • a sensor device 11 to take measurements of the catalyst fines content in the dirty oil for processing coming into the separator (Cat Fines IN).
  • measurements of the catalyst fines content are additionally also made in the outgoing cleaned or processed clean oil—for example directly in the clean oil running out of the separator—with the same sensor device 11 or with a second sensor device 12 .
  • the proportion of fines having a mean diameter below a limit can be determined, for example.
  • These measures need not be effected directly in real time. Instead, it is also possible to take samples (for example at intervals of a few hours in each case) which are then analyzed with a suitable sensor system—as commercially available in principle—for the catalyst fines content.
  • the measurements determined are then advantageously passed to a computer unit, not shown here, which is utilized as (closed-loop) control device for control of the plant shown in FIG. 1 and which is used for closed-loop control especially of the separation temperature T 1 and/or the throughput with the pump 4 using the process variables determined.
  • the closed-loop control can be effected as described above or, alternatively, optionally also in real time with online measurements of the catalyst fines content.
  • Closed-loop control variables used may especially be the catalyst fines content mentioned, which is to be kept below a setpoint value, the current fuel consumption of the internal combustion engine as process variable and/or the actual level in a clean oil tank.
  • a reduction in the throughput increases the separation efficiency.
  • the electrical energy consumption is also reduced when the feed pump speed is reduced.
  • the throughput in the processing method can be used for closed-loop control as a function of one or more of the following measurement parameters or process variables:
  • The—at least intermittent—increase in the separation temperature to more than 98° C. described improves the separation efficiency and enables the attainment of very low catalyst fines contents.
  • the proportion of abrasive catalyst fines can be lowered in a simple manner below limits defined by engine manufacturers, which may also be well below 20 ppm or even below 15 ppm or 10 ppm or lower. With a further increase in temperature, the result of the separating operation is improved further, although the apparatus demands are lower at temperatures up to 115° C. than for even higher temperatures.
  • FIG. 3 shows a particularly advantageous tank arrangement having several tanks connected in a particularly advantageous manner to one another and to the plant of FIG. 2 .
  • the heat exchangers and further details from FIG. 1 were not included in the drawing to improve clarity.
  • Two settling tanks ST 1 , ST 2 are provided here, and two service tanks ST 3 , ST 4 , into which either clean oil OIL 2 or else heavy oil OIL 1 for processing can be introduced as required.
  • the conduit 10 therefore branches into all these tanks ST 1 to ST 4 .
  • the tanks ST 1 to ST 4 also each have at least one outlet. These outlets can each be opened with valves V 1 to V 4 in the desired manner. All the outlets also open into the inlet 1 in FIG. 2 .
  • This arrangement can be managed in a particularly flexible manner and gives options for storage of oils of various quality and also for pre-processing of oils which have been stored in the tanks for a long period by first “circulating” the oil from the tanks, then “pre-processing” the oil, for example, at a lower temperature up to 98° C., and then passing it back into the same tank.
  • FIG. 4 corresponds substantially to that from FIG. 3 , but has been supplemented with an overflow-dependent closed-loop pump control system.
  • service tanks ST 3 and ST 4 have at least one overflow conduit 201 , 202 to the service tanks ST 1 and ST 2 .
  • overflow conduits 201 , 202 should preferably be disposed in the lower region of the service tanks ST 3 and ST 4 , in order to be able to recycle any possible sediments into the service tanks ST 1 and ST 2 .
  • Flow indicators FIC are connected within each of the overflow conduits. These are connected to a closed-loop control device 203 which uses the flow rate into the overflow conduits here as the only process variable or as one of the process variables that it advantageously uses as well takes into account in the closed-loop control of the pump 204 .
  • the throughput of a pump 104 is subject to closed-loop control via a flow indicator 203 connected within the overflow conduits.

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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)
US14/650,263 2012-12-10 2013-12-09 Method for Treating Heavy Fuel Oil Abandoned US20160122661A1 (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102012112026.9 2012-12-10
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

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US20160122661A1 true US20160122661A1 (en) 2016-05-05

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US14/650,263 Abandoned US20160122661A1 (en) 2012-12-10 2013-12-09 Method for Treating Heavy Fuel Oil

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)

Cited By (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20170067870A1 (en) * 2015-09-08 2017-03-09 Parker Hannifin Manufacturing Limited Method
GR20170100583A (el) * 2017-12-21 2019-07-08 Δουσης, Ευαγγελος Γεωργιου Συστημα αυτοματης ρυθμισης, βελτιστης παροχης και παρακολουθησης φυγοκεντρικων διαχωριστηρων καυσιμου
US10961467B2 (en) * 2017-06-28 2021-03-30 Alfa Laval Corporate Ab Fuel treatment system for an engine and a method using the system
WO2021240320A1 (en) 2020-05-25 2021-12-02 Serra Delgado Joan System and method for the comprehensive management of marpol i waste, on board a ship
US11511214B2 (en) 2016-09-06 2022-11-29 Alfa Laval Corporate Ab Method for cleaning fuel oil for a diesel engine
EP4428215A1 (de) * 2023-03-09 2024-09-11 Alfa Laval Corporate AB Verfahren zum betreiben eines systems mit einem zentrifugalabscheider

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2019221287A1 (ja) * 2018-05-18 2019-11-21 一般社団法人 ＨｉＢＤ研究所 バイオジェット燃料の製造方法
KR102630831B1 (ko) 2023-06-22 2024-01-29 주)씨에스캠 중유의 탄화물질 제거장치

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US20050197241A1 (en) * 2004-03-04 2005-09-08 Hutchison Hayes L.P. Three Phase Decanter Centrifuge

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EP0502404B1 (de) * 1991-03-04 1996-05-01 Federico Esteban Dr. Lantos Verfahren zur Verringerung des Verunreinigungsgrades von Brennstoffen
EP2181744A1 (de) * 2008-10-29 2010-05-05 Citec Engineering Oy AB Verfahren und Vorrichtung zum Trennen von Wasser und Feststoffen aus Schweröl
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
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JP5386641B2 (ja) * 2010-09-03 2014-01-15 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
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Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20170067870A1 (en) * 2015-09-08 2017-03-09 Parker Hannifin Manufacturing Limited Method
US9759706B2 (en) * 2015-09-08 2017-09-12 Parker Hannifin Manufacturing Limited Method and kit for monitoring catalyst fines in heavy fuel oil
US11511214B2 (en) 2016-09-06 2022-11-29 Alfa Laval Corporate Ab Method for cleaning fuel oil for a diesel engine
US10961467B2 (en) * 2017-06-28 2021-03-30 Alfa Laval Corporate Ab Fuel treatment system for an engine and a method using the system
GR20170100583A (el) * 2017-12-21 2019-07-08 Δουσης, Ευαγγελος Γεωργιου Συστημα αυτοματης ρυθμισης, βελτιστης παροχης και παρακολουθησης φυγοκεντρικων διαχωριστηρων καυσιμου
GR1009618B (el) * 2017-12-21 2019-10-14 Ευαγγελος Γεωργιου Δουσης Συστημα αυτοματης ρυθμισης, βελτιστης παροχης και παρακολουθησης φυγοκεντρικων διαχωριστηρων καυσιμου
WO2021240320A1 (en) 2020-05-25 2021-12-02 Serra Delgado Joan System and method for the comprehensive management of marpol i waste, on board a ship
EP4428215A1 (de) * 2023-03-09 2024-09-11 Alfa Laval Corporate AB Verfahren zum betreiben eines systems mit einem zentrifugalabscheider
WO2024184094A1 (en) * 2023-03-09 2024-09-12 Alfa Laval Corporate Ab Method for operating a system comprising a centrifugal separator

Also Published As

Publication number Publication date
WO2014090717A2 (de) 2014-06-19
SG11201504533SA (en) 2015-07-30
DE102012112026A1 (de) 2014-06-12
CN105051160A (zh) 2015-11-11
JP2016509075A (ja) 2016-03-24
KR102172671B9 (ko) 2022-02-14
WO2014090717A3 (de) 2015-08-27
KR20150093765A (ko) 2015-08-18
EP2928988B1 (de) 2022-11-23
KR102172671B1 (ko) 2020-11-02
BR112015012698A2 (pt) 2017-07-11
EP2928988A2 (de) 2015-10-14

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