CN102888244B - Production method of ship fuel oil - Google Patents
Production method of ship fuel oil Download PDFInfo
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- CN102888244B CN102888244B CN201210404393.3A CN201210404393A CN102888244B CN 102888244 B CN102888244 B CN 102888244B CN 201210404393 A CN201210404393 A CN 201210404393A CN 102888244 B CN102888244 B CN 102888244B
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Abstract
The invention relates to a production method of ship fuel oil, which comprises the following steps: heating catalytic slurry oil, filtering through a precision filter to remove tiny catalyst granules in the slurry oil, mixing with hydrogen, heating, contacting the mixture with a residual oil hydrofining catalyst, a distillate hydrofining catalyst and a distillate hydrocracking catalyst to carry out catalytic hydrogenation reaction on the mixture, carrying out gas-oil separation and fractionation on the reaction product to obtain a tail oil fraction, and mixing the tail oil fraction with vacuum residual oil in different proportions to obtain the finished product. Under mild reaction conditions and lower hydrogen consumption, the method provided by the invention can greatly enhance the doping proportion of the catalytic slurry oil in the ship fuel oil by more than 75%, ensures the indexes of metals, ash and the like in the ship fuel oil to be not overproof, greatly increases the calorific value, improves the compatibility of the ship fuel oil, and ensures the production of the high-quality ship fuel oil product.
Description
Technical field
The present invention relates to a kind of Production method of ship fuel oil.
Background technology
According to BP energy statistics and Purvin & Gertz, the demand of world's residue type oil fuel in 2009 is about 4.5 hundred million tons, wherein admiralty fuel oil demand is 1.4 hundred million tons, the demand of expectation the year two thousand twenty world residue type oil fuel is 3.3 hundred million tons, and the quantity of admiralty fuel oil will be increased to 1.9 hundred million tons.Due to the increase that international sea-freight is measured, the year two thousand twenty admiralty fuel oil consumption will increase by 5,000 ten thousand tons than 2009, and the ratio accounting for oil fuel also will bring up to about 60% by 30%.
2009, China's oil fuel consumption 3,395 ten thousand tons, self-produced 1,795 ten thousand tons, import 1,600 ten thousand tons; 9,200,000 tons are had, as about 1,195 ten thousand tons of furnace fuel, as 1,280 ten thousand tons of admiralty fuel oil wherein as local refinery stock.In admiralty fuel oil, the quantity of bonded oil is about 6,800,000 tons, cut oil type oil fuel quantity about 3,000,000 tons.It is predicted, 2009-2013 domestic admiralty fuel oil demand average annual growth rate can reach 11% ~ 20%, and by 2013, Chinese vessel oil fuel demand was about 32,000,000 tons.
From foreign trade bunkering situation, the foreign trade boats and ships refueled in China at present only account for 4% of port foreign trade boats and ships, far below 90% level at Singapore port; Within 2008, China's boats and ships bonded fuel oil supply is only 3.8% of the whole world, and Singapore is 25.6%, has a long way to go.China's cargo throughput of port and container throughput occupy the first in the world in continuous 5 years, and international ocean shipping handling total amount also keeps quick growth, and following admiralty fuel oil demand also will increase thereupon.
The reason that China's admiralty fuel oil share of market is not high mainly contains two aspects: one is that oil refining enterprise requires " eating dry bleeding ", produces pay little attention to oil fuel; Two is that China's service at port function is poor, and a lot of port ship of crossing all refuels on Japan, Korea S and Singapore and other places.
There are two principal features in admiralty fuel oil market: one is that specification of quality is unified, and all must act on the standard that International Maritime Organizaton formulates, this point is different from the situation of the quality on gasoline and diesel; Two is that mobility is strong, and its demand changes with marine trade amount and direction of trade, comparatively similar to the situation of aviation kerosene.From above situation, no matter be market abroad or domestic market, the demand of admiralty fuel oil all will increase further.
In recent years, for reducing the pressure that fuel cost constantly rises, marine fuel is progressively to the future development of heaviness, in poor quality and tempered oil.One is putting into effect in a large number along with new ship, full-bodied heavy fuel oil (HFO) consumption rapid development, two is impacts that are nervous by processed oil resource, price increase, the consumption of domestic DMC fuel wet goods substitute vessel diesel oil increases, but restriction that is few by output in domestic, supply wretched insufficiency, cannot meet the need of market.
Along with global energy shortage, constantly rising violently of crude oil price, the fuel source trend that supply falls short of demand manifests day by day.Petrol and diesel oil price constantly soaring China Petrochemical Industry and the PetroChina Company Limited. of causing is conceived to produce the higher petrol and diesel oil of sexual valence, has no time to attend to marine fuel oil market.Refinery constantly deepens residual oil weight-lightening producing level, although cause national oil-refining capacity annual increment to be 5% ~ 10%, the fuel oil output based on mink cell focus fails to be improved.The growth of oil fuel demand and the basicly stable of output result in oil fuel breach and strengthen year by year.Between 2009 to 2011 years, the sustainable growth of oil fuel demand, exceedes the oil fuel needs of half by providing by import.
Current admiralty fuel oil produces the main method adopting directly blending, and boats and ships residue type 380# oil fuel is usually concocted produced by visbreaking residue, heavy catalytic cycle oil (HCO), catalytic diesel oil three kinds of components.50 DEG C of viscosity are lower than 380 mm
2the residue type ship oil fuel of/s, is produced by the diesel oil distillate of calling in suitable proportion.
Crude oil price constantly soaring, makes oil supply business consider from the contrast of Cost and Benefit, adopts the mode of " non-traditional " to be in harmonious proportion heavy admiralty fuel oil, such as: interpolation waste lubricating oil; Chemical solvents waste material is used to carry out being in harmonious proportion with dissolved bitumen matter; Replace residual oil etc. with coal tar, these ways cause larger impact to the ignition quality of heavy oil and stability undoubtedly.For admixture coal tar: containing up to ten thousand kinds of compounds in coal tar, its composition is very complicated, form primarily of polycyclc aromatic compound, hydrocarbon content comparatively petroleum residual oil is low, wherein there are many components (such as aldehydes matter etc.) not only to human body and bad environmental, are also difficult to burning, therefore with the heavy oil that undressed coal tar is modulated, its get angry quality and combustionproperty all poor, therefore conventional production methods limit domestic ships combustion market sound development.
Therefore, no matter cut oil type or residue type ship oil fuel, continuation also increases by tomorrow requirement, and specification of quality improves constantly, and production method will change thereupon.China's oil refining industry should hold this market opportunity in time, payes attention to low-sulfur admiralty fuel oil and produces, both can be the guarantee that shipping industry provides supply of fuel, also can improve the whole competitiveness of China's oil refining.
Solid content is down to 0.05 by the problem that secondary filter technology solves catalytic slurry solid content high
solve fixed-bed reactor problem of pressure drop, hydrogenation is as the hydrocarbon composition technology improving oil product, significantly reduce the density of catalytic slurry, carbon residue, raising calorific value etc., produce the marine fuel oil distillate obtaining high-quality, for the production of the residue such as high-quality F120, F180, F380 type ship oil fuel, this technology is the good method of producing admiralty fuel oil with low value slurry oil.
Existing hydrogen addition technology is more automobile-used (or the aircraft is used) transport fuel for the production of high-quality, mainly concentrate on each fraction oil hydrogenation refining of processing or cracking, the hydrofining of vacuum residuum, little to the processing correlation technique of this low grade oils of catalytic slurry, the correlation technique of full catalytic slurry hydrogenation technique rarely has report, mainly the small granules of catalyst of catalytic slurry cannot remove, a solid content difficult problem is solved by proprietary secondary filter technology advanced at present, for slurry oil hydrocarbon composition, carry out hydrogenation catalyst combination, the admiralty fuel oil of production high-quality.For opening up new processing approach with the combustion of the ship of low value catalytic slurry production high-quality, the supply breach in China's high-quality ship combustion market can be met to a certain extent, alleviating the ship combustion intake pressure of China, alleviating the predicament of " energy security " of China.
Summary of the invention
The object of this invention is to provide a kind of Production method of ship fuel oil, to overcome the deficiency that the energy dissipation of current domestic production admiralty fuel oil technique is serious, working condition requirement is high, production cost is high.
The object of the invention is to be achieved through the following technical solutions:
A kind of Production method of ship fuel oil, comprises the following steps:
1) catalytic slurry is heated to 100-350 DEG C, under the pressure condition of 0.5-6Mpa, by inorganic membrane filtration catalytic slurry, the solid content of catalytic slurry is down to 0.05
, ash content (inorganic salt and organometallics and the impurity that some are mixed into) is down to less than 0.002%, and metal removal is higher than 95%;
2) 250-400 DEG C is heated to by filtering the catalytic slurry obtained in step 1), by Cemented filling to the first reaction zone, and the hydrogen passing into 2-18Mpa mixes with catalytic slurry, the catalytic slurry of mixing is contacted with residual hydrogenation catalyst for refining, catalyst for hydrorefining distillate oil, catalyst for distillate hydro-cracking successively with hydrogen, carries out catalyzed reaction;
3) by step 2) in the reactant flow that obtains through gas and oil separating plant, carry out gas-oil separation, be separated by the liquid in reactant with hydrogen-containing gas, hydrogen-containing gas can turn back to step 2 upon compression) recycle;
4) liquid of the separation of gained in step 3) is carried out fractionation, fractionation obtains petroleum naphtha, diesel oil distillate and tail oil fraction;
5) tail oil fraction obtained in step 4) is in harmonious proportion with different ratios and vacuum residuum according to the needs produced, can finished product be obtained.
Step 2) described in residual hydrogenation catalyst for refining comprise the compound of following weight percent: the MoO of NiO, 2.5%-3% of 0.5%-2%
3, 20%-30% the aluminum oxide of CoO and 65%-77%.
Step 2) described in catalyst for hydrorefining distillate oil comprise the compound of following weight percent: the WO of 23%-30%
3, 2.4%-3% the MoO of NiO, 2.3%-4%
3with the aluminum oxide of 65%-72.3%.
Step 2) described in catalyst for distillate hydro-cracking comprise the compound of following weight percent: the WO of 27%-30%
3, the molecular sieve of NiO, 23%-30% of 2.7%-3% and the aluminum oxide of 40%-47.3%.
Beneficial effect of the present invention is: adopt the inventive method, under the reaction conditions comparatively relaxed and relatively low hydrogen consumption, significantly can improve the mixed ratio of catalytic slurry in ship combustion up to more than 75%, ensure that ship fires metal, ash grades, and index does not exceed standard, significantly improve its calorific value, improve the consistency of ship combustion, ensure the ship combustion product of production high-quality.
Accompanying drawing explanation
With reference to the accompanying drawings the present invention is described in further detail below.
Fig. 1 is the schema of the Production method of ship fuel oil described in the embodiment of the present invention.
In figure:
1, slurry oil oil feeding device; 2, slurry oil charging stock tank; 3, slurry oil feed valve; 4, slurry oil fresh feed pump; 5, slurry oil well heater; 6, slurry oil strainer; 7, slurry heat-exchanger; 8, slurry oil process furnace; 9, hydrogen; 10, hydrogen control valve; 11, hydrogenator; 12, high pressure separating tank; 13, low pressure separation pot; 14, distillation tower; 15, petroleum naphtha control valve; 16, diesel component oil control valve; 17, after hydrogenation, slurry oil (tail oil) is in harmonious proportion control valve; 18, slag ladle is subtracted; 19, slag mediation control valve is subtracted; 20, finished product ship combustion tank.
Embodiment
As shown in Figure 1, a kind of Production method of ship fuel oil described in the embodiment of the present invention, comprises the following steps:
1) catalytic slurry is heated to 100-350 DEG C, under the pressure condition of 0.5-6Mpa, by the catalytic slurry that inorganic membrane filtration solid content is high, the solid content of catalytic slurry is down to 0.05
, ash content is down to less than 0.002%, and metal removal is higher than 95%;
2) 250-400 DEG C is heated to by filtering the catalytic slurry obtained in step 1), by Cemented filling to the first reaction zone, and the hydrogen passing into 2-18Mpa mixes with catalytic slurry, the catalytic slurry of mixing is contacted with residual hydrogenation catalyst for refining, catalyst for hydrorefining distillate oil, catalyst for distillate hydro-cracking successively with hydrogen, carries out catalyzed reaction;
3) by step 2) in the reactant flow that obtains through gas and oil separating plant, carry out gas-oil separation, be separated by the liquid in reactant with hydrogen-containing gas, hydrogen-containing gas can turn back to step 2 upon compression) recycle;
4) liquid of the separation of gained in step 3) is carried out fractionation, fractionation obtains petroleum naphtha, diesel oil distillate and tail oil fraction;
5) tail oil fraction obtained in step 4) is in harmonious proportion with different ratios and vacuum residuum according to the needs produced, can finished product be obtained.
Step 2) described in residual hydrogenation catalyst for refining comprise the compound of following weight percent: the MoO of NiO, 2.5%-3% of 0.5%-2%
3, 20%-30% the aluminum oxide of CoO and 65%-77%.
Step 2) described in catalyst for hydrorefining distillate oil comprise the compound of following weight percent: the WO of 23%-30%
3, 2.4%-3% the MoO of NiO, 2.3%-4%
3with the aluminum oxide of 65%-72.3%.
Step 2) described in catalyst for distillate hydro-cracking comprise the compound of following weight percent: the WO of 27%-30%
3, the molecular sieve of NiO, 23%-30% of 2.7%-3% and the aluminum oxide of 40%-47.3%.
During concrete use, the catalytic slurry of catalytic slurry is transported in slurry oil charging stock tank 2 by slurry oil oil feeding device 1, the switch of catalytic slurry pipeline is controlled by slurry oil feed valve 3, filtered being transported in slurry oil strainer 6 stored in the catalytic slurry in slurry oil charging stock tank 2 by slurry oil fresh feed pump 4, before arrival slurry oil strainer 6, catalytic slurry is heated to 100-350 DEG C by slurry oil well heater 5, catalytic slurry through filtering carries out being heated to 250-400 DEG C by slurry heat-exchanger 7 and slurry oil process furnace 8 again, enter in hydrogenator 11 after heating, in hydrogenator 11, catalytic slurry mixes with hydrogen 9, the add-on of hydrogen 9 is controlled by hydrogen control valve 10, mixed catalytic slurry and hydrogen in hydrogenator 11 successively with residual hydrogenation catalyst for refining, catalyst for hydrorefining distillate oil, catalyst for distillate hydro-cracking contacts, carry out catalyzed reaction, reacted product carries out gas-liquid separation by high pressure separating tank 12 and low pressure separation pot 13, liquid after separation is sent in distillation tower 14 and carries out fractionation, petroleum naphtha is obtained after fractionation, diesel oil distillate and tail oil fraction, the petroleum naphtha fractionated out, diesel oil distillate and tail oil fraction are gone out respectively by Cemented filling, respectively by petroleum naphtha control valve 15 during conveying, after diesel component oil control valve 16 and hydrogenation, slurry oil (tail oil) is in harmonious proportion control valve 17 and controls the output of the product that three kinds fractionate out, the tail oil fraction fractionated out in finished product ship combustion tank 20 with subtract the vacuum residuum (subtracting slag) that slag ladle 18 exports and mix by a certain percentage, the ratio of mixing is controlled by the slag mediation control valve 19 that subtracts on pipeline.
Embodiment:
Table one is the feedstock property of catalytic slurry slurry
Table two vacuum residuum feed character
Table three reaction conditions
Character after table four slurry oil hydrogenation
Table five is for raw material C with subtract slag and carry out mediation experimental data
As shown above, tail oil fraction and vacuum residuum can obtain different products with different blending ratios.
The present invention is not limited to above-mentioned preferred forms; anyone can draw other various forms of products under enlightenment of the present invention; no matter but any change is done in its shape or structure; every have identical with the application or akin technical scheme, all drops within protection scope of the present invention.
Claims (2)
1. a Production method of ship fuel oil, is characterized in that, comprises the following steps:
1) catalytic slurry is heated to 100-350 DEG C, under 0.5-6Mpa pressure condition, by inorganic membrane filtration catalytic slurry, the solid content of catalytic slurry is down to 0.05, and ash content is down to less than 0.002%, and metal removal is higher than 95%;
2) 250-400 DEG C is heated to by filtering the catalytic slurry obtained in step 1), by Cemented filling to the first reaction zone, and the hydrogen passing into 2-18Mpa mixes with catalytic slurry, the catalytic slurry of mixing is contacted with residual hydrogenation catalyst for refining, catalyst for hydrorefining distillate oil, catalyst for distillate hydro-cracking successively with hydrogen, carries out catalyzed reaction;
3) by step 2) in the reactant flow that obtains through gas and oil separating plant, carry out gas-oil separation, the liquid in reactant be separated with hydrogen-containing gas;
4) liquid of the separation of gained in step 3) is carried out fractionation, fractionation obtains petroleum naphtha, diesel oil distillate and tail oil fraction; And
5) tail oil fraction obtained in step 4) is in harmonious proportion with different ratios and vacuum residuum according to need of production, can finished product be obtained;
Described residual hydrogenation catalyst for refining comprises the compound of following weight percent: the MoO of NiO, 2.5%-3% of 0.5%-2%
3, 20%-30% the aluminum oxide of CoO and 65%-77%;
Described catalyst for hydrorefining distillate oil comprises the compound of following weight percent: the WO of 23%-30%
3, 2.4%-3% the MoO of NiO, 2.3%-4%
3with the aluminum oxide of 65%-72.3%;
Described catalyst for distillate hydro-cracking comprises the compound of following weight percent: the WO of 27%-30%
3, the molecular sieve of NiO, 23%-30% of 2.7%-3% and the aluminum oxide of 40%-47.3%.
2. Production method of ship fuel oil according to claim 1, is characterized in that, in step 3), the hydrogen-containing gas obtained by gas-oil separation, turns back to step 2 upon compression) recycle.
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| Application Number | Priority Date | Filing Date | Title |
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| CN201210404393.3A CN102888244B (en) | 2012-10-22 | 2012-10-22 | Production method of ship fuel oil |
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| CN201210404393.3A CN102888244B (en) | 2012-10-22 | 2012-10-22 | Production method of ship fuel oil |
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| CN102888244B true CN102888244B (en) | 2015-07-15 |
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN103468301A (en) * | 2013-10-11 | 2013-12-25 | 广东石油化工学院 | Catalytic slurry oil preprocessing device coupled with heating and filtering functions |
| RU2692483C2 (en) * | 2014-12-04 | 2019-06-25 | ЭкссонМобил Рисерч энд Энджиниринг Компани | Low-sulfur ship bunker fuels and methods for production thereof |
| US20190233741A1 (en) * | 2017-02-12 | 2019-08-01 | Magēmā Technology, LLC | Multi-Stage Process and Device for Reducing Environmental Contaminates in Heavy Marine Fuel Oil |
| CN109705909B (en) * | 2017-10-25 | 2020-11-13 | 中国石油化工股份有限公司 | Method for producing bunker fuel oil from coal tar |
| CN110205160A (en) * | 2019-06-11 | 2019-09-06 | 黄河三角洲京博化工研究院有限公司 | It is taken off based on catalytic cracked oil pulp and consolidates-add the process that hydrogen prepares bunker fuel oil |
| CN114106877B (en) * | 2020-08-27 | 2023-06-09 | 中国石油化工股份有限公司 | System and method for producing low-sulfur marine fuel oil |
| CN113969196B (en) * | 2021-10-26 | 2022-12-16 | 中国石油化工股份有限公司 | Low-sulfur marine fuel oil and preparation method thereof |
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