CN102071037A - Dehydration method of low-grade oil - Google Patents
Dehydration method of low-grade oil Download PDFInfo
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Abstract
The invention relates to a dehydration method of low-grade oils. In the method of the invention, spacing hydrocarbons which are low boiling point hydrocarbons with good oil-water separation effect are used in the dehydration process of low-grade oils to ensure that the hydrocarbons of the steam material flow T1V separated from the top of a dehydration tower are all or mainly composed of spacing hydrocarbons; the material flow T1V is separated to oil solution T1VL and aqueous solution T1LW in an oil-water separation part (SP); the oil solution can be returned to the top of the dehydration tower to be used for tower top refluxing; and the aqueous solution T1LW has low oil content and can be easily treated by the conventional method with low cost. The method of the invention is particularly suitable for the dehydration process of low-grade oils such as low-temperature coal tar, medium-temperature coal tar and anthracene oil; and the spacing hydrocarbons are low boiling point hydrocarbons obtained through the hydroconversion of tar. Furthermore, by utilizing the characteristic that the aqueous solution T1LW does not contain oxygen, the aqueous solution T1LW is heated and converted to steam used for a proper technological process to replace fresh water, for example the steam can be used as the stripping steam of the low-grade oil dehydration tower or the power steam of a vacuum-pumping system during the decompression operation of the dehydration tower or the steam used in the coking process of the residual oil obtained through the separation of low-grade oils.
Description
Technical field
The present invention relates to a kind of poor quality oil dewatering, use at interval hydrocarbon 2F (low boiling hydrocarbon that oil-water separation is good, only contain at interval the oily(waste)water of hydrocarbon can adopt conventional sewage water treatment method to handle) in moisture poor quality oil 1F dehydration, the hydro carbons of the steam stream T1V that leaves dehydration column overhead preferably all is made up of interval hydrocarbon component, and logistics T1V is separated into fluid T1VL and water liquid T1VW at oily water separation part SP; Say especially, the present invention relates to a kind of dewatering that is suitable for moisture poor quality oils such as coalite tar, coal-tar middle oil, carbolineum.
Background technology
As everyone knows, coal tar contains water component usually, and its water-content can reach 1.0～5.0% even more.The water-content of coal tar is relevant with coal tar character, and is also relevant with the technological process operational condition that produces coal tar, and the water-content fluctuation of coal tar is bigger, and table 1 has been listed several industrial datas of coal tar water-content.
Table 1 coal tar kind and water-content full scale plant data
| Sequence number | The coal tar kind | The coal tar water-content, % |
| 1 | Coalite tar heavy oil | 6～20 |
| 2 | Coal-tar middle oil | 1～5 |
| 3 | Coal-tar middle oil coke chemicals oil | 0.3～0.4 |
| 4 | Middle coalite tar residuum coking product oil | 0.3～0.5 |
| 5 | Coal-tar heavy oil carbolineum | 0.5～2.0 |
| 6 | The coal-tar heavy oil washing oil | 0.5～2.0 |
With coal tar is the hydroconversion process that poor quality oil is produced fuel oil, comprises coal tar one stage hydrofining process usually.In coal tar one stage hydrofining process, water is disadvantageous component, on the one hand, in the heat temperature raising process before poor quality oil enters the one stage hydrofining reactor, the existence of water can aggravate the corrosion of acids in the coal tar (phenols and organic acid) to pipeline, equipment etc., the metal ions such as iron that corrosion produces enter the one stage hydrofining reactor, for guaranteeing the operational cycle of expection, must use more Hydrodemetalation catalyst (protective material) to increase the hydrogen consumption simultaneously; On the other hand, the increase of raw water content will improve the reaction process steam partial pressure, and will be unfavorable to catalyst performance stabilised and long-term operation; Again on the one hand, when water-containing material mixes with hydrogen sulfide containing hydrogen gas stream, form wet hydrogen sulfide corrosion condition, can aggravate the corrosion of pipeline, equipment etc.Therefore, before poor quality oil enters the hydrofining reaction part, carry out processed usually to reduce water-content as much as possible, dehydration method is unrestricted.
Known coal tar dewatering, do not use hydrocarbon at interval, the hydro carbons of the steam stream T1V that leaves dehydration column overhead all is made up of the coal tar light constituent, logistics T1V is separated into fluid T1VL and water liquid T1VW at oily water separation part SP, fluid T1VL can return the dehydration tower top and use as trim the top of column, and the oil ingredient of water liquid T1VW is the coal tar light constituent.For coal preparing natural gas engineering, can rely on the coal preparing natural gas to contain tar, phenol-containing wastewater treatment system and handle and contain tar sewage, but huge because of its scale of investment, many existence contain the occasion of tar sewage, no economic strength employing.
The shortcoming of conventional distillation method dewatering process is: the oil ingredient of water liquid T1VW is the coal tar light constituent, be difficult to adopt " the oily(waste)water oil-contaminated water processing method commonly used that contains petroleum base light oil " to handle, usually adopt the sewage burning process to handle, consume a large amount of fuel (being generally fuel gas), and increase pollutant discharge amount.Along with the increase of coal tar process scale, above-mentioned shortcoming is more obvious.
With 200,000 tons of/year coalite tar heavy-oil hydrogenation conversion systems is example, calculate when going into operation by 7200h/a, coalite tar heavy oil upgrading amount is 27.778t/h, by moisture 16%, the moisture 4.444t/h of coal-tar middle oil, the stripped vapor consumption is counted 1.389t/h by 5% of coalite tar heavy oil quantity usually, adds up to 5.833t/h, oil ingredient among the water liquid T1VW that conventional distillation method dewatering process obtains is the coal tar light constituent all, and related data is as follows:
1. adopt the sewage burning process to handle usually, consume a large amount of fuel (being generally fuel gas), and increase pollutant discharge amount.Said process only considers that the water vaporization heat just reaches 3.24MMKCal/h, the vaporization total heat surpasses 4.00MMKCal/h, need minimum 400 standard cubic meter of standard fuel gas (calorific value is that 10000kcal/ standard cubic meter unit price is generally 1.5 yuan/standard cubic meter)/hour, 600 yuan/hour of fuel prices, promptly 4,320,000 yuan/year;
2. sewage incineration system construction investment is about 260～3,000,000 yuan;
3. lose water resources 5.833t/h, amount to 4.2 ten thousand tons/year;
4. water liquid T1VW Shen matchmaker's tar light constituent content calculates by 0.3% and amounts to 17.5kg/h (126t/a), phenol component concentration and calculate by 0.1% and amount to 5.8kg/h (41.8t/a), and the discharging of its combustion product gases increases pollutant discharge amount.
Therefore, solve or improve the problems referred to above, have energy-saving effect, environment protecting, the water circulation use effect of reality and save results form investment.
The present invention use hydrocarbon at interval reduce oily(waste)water oil-contg, improve the coal tar dewatering of the oil nature of oily(waste)water, do not appear in the newspapers.
The present invention use hydrocarbon at interval reduce oily(waste)water oil-contg, improve the poor quality oil dewatering of the oil nature of oily(waste)water, do not appear in the newspapers.
Therefore, first purpose of the present invention is to propose a kind of oil-contg that uses hydrocarbon at interval to reduce oily(waste)water, improves the poor quality oil dewatering of the oil nature of oily(waste)water.
Second purpose of the present invention is to propose a kind of oil-contg that uses hydrocarbon at interval to reduce oily(waste)water, improves the coal tar dewatering of the oil nature of oily(waste)water.
The 3rd purpose of the present invention is to propose a kind of coal tar hydrogenating conversion process, use the benzoline of coal tar hydrogenating conversion process the finished product as the interval hydrocarbon reduce coal tar dehydration oily(waste)water oil-contg, improve the oil nature of oily(waste)water, hydrocarbon finally returns dehydration tower by circulation after the coal tar hydrogenating conversion process and uses at interval.
Summary of the invention
A kind of poor quality oil dewatering is characterized in that comprising following steps:
1. in poor quality oil dehydration part, use interval hydrocarbon 2F that the hydro carbons of the overhead vapor stream T1V that leaves the dehydration tower T1 that handles poor quality oil 1F mainly is made up of interval hydrocarbon component, T1V obtains fluid T1VL and water liquid T1VW in oily water separation part SP separated stream.
In order to reach best effect of the present invention, it is characterized in that:
1. hydrocarbon 2F joins in the dehydration tower T1 continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, at least a portion fluid T1VL returns dehydration tower T1 and uses as trim the top of column, and at least a portion fluid T1VL leaves oily water separation part SP and uses as dehydration tower T1 cat head light oil products.
Can be steam with water liquid T1VW thermal conversion, stripped vapor that uses as dehydration tower T1 or pumped vacuum systems power steam or as the separating obtained residuum coking process of poor quality oil 1F steam during as dehydration tower T1 decompression operation.
When the present invention was applied to dehydration inferior, hydrocarbon 2F can be 1F hydroconversion process HR gained low boiling hydrocarbon product at interval, and hydrocarbon 2F is preferably 1F hydrocracking gained and mainly is lower than the conventional liq hydrocarbon that 150 ℃ component is formed by conventional boiling point final boiling point at interval.At this moment, hydrocarbon 2F joins dehydration tower T1 top continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, part fluid T1VL returns dehydration tower T1 and uses as trim the top of column, part fluid T1VL leaves oily water separation part SP and recycles as the stock oil of 1F hydroconversion process HR
Poor quality oil 1F can be higher than 100 ℃ following oil product for conventional boiling point initial boiling point: coalite tar or coalite tar distillate or the coking of coalite tar coking thermally splitting gained generate oil or coal-tar middle oil or coal-tar middle oil distillate or coal-tar middle oil coking thermally splitting gained coking generation oil or coal-tar heavy oil carbolineum or coal-tar heavy oil washing oil or petroleum base hydrocarbon ils inferior or shale oil base hydrocarbon ils inferior
Dehydration tower T1 of the present invention operates under reduced pressure usually, and dehydration tower T1 cat head working pressure is usually less than 0.06MPa (absolute pressure).
Interval of the present invention hydrocarbon hydro carbons initial boiling point is than poor quality oil hydro carbons initial boiling point: general minimum low 30 ℃, minimum low 50 ℃ usually, preferably minimum low 70 ℃.
The present invention's hydrocarbon at interval can form short-circuit cycle, and hydrocarbon 2F joins the epimere of dehydration tower T1 continuously at interval, and at least a portion fluid T1VL leaves oily water separation part SP as recycling as interval hydrocarbon 2F.
The present invention interval hydrocarbon adds the implantation site and is generally: hydrocarbon 2F joins the epimere of dehydration tower T1 continuously at interval, hydrocarbon 2F opening for feed position is 1～15 apart from dehydration tower T1 cat head number of theoretical plate at interval, and hydrocarbon 2F opening for feed position is 1～15 apart from an adjacent high boiling liquid extraction mouthful number of theoretical plate at interval.
The present invention interval hydrocarbon adds the implantation site and is preferably: hydrocarbon 2F joins the epimere of dehydration tower T1 continuously at interval, hydrocarbon 2F opening for feed position is 5～10 apart from dehydration tower T1 cat head number of theoretical plate at interval, and hydrocarbon 2F opening for feed position is 5～10 apart from an adjacent high boiling liquid extraction mouthful number of theoretical plate at interval.
Embodiment
Below describe the present invention in detail.
Conventional gas hydrocarbon of the present invention refers to and is the gasiform hydro carbons under the normal condition, comprises methane, ethane, propane, butane.
Conventional liq hydrocarbon of the present invention refers to the hydro carbons that is in a liquid state under the normal condition, comprises the hydro carbons that pentane and boiling point thereof are higher.
The composition of component of the present invention or concentration or content or yield value unless stated otherwise, are the weight basis value.
Proportion of the present invention unless stated otherwise, refers to the ratio of water-mass density under fluid density and normal pressure under normal pressure, the 15.6 ℃ of conditions, the 15.6 ℃ of conditions.
Pressure of the present invention refers to absolute pressure.
Conventional boiling point of the present invention refers to vapour, the liquid equilibrium temperature of material under a barometric point.
Conventional boiling range of the present invention refers to the conventional boiling spread of cut.
Petroleum naphtha of the present invention refers to conventional boiling point and is lower than 180 ℃ conventional liq hydrocarbon.
It is 180～355 ℃ hydro carbons that diesel component of the present invention refers to conventional boiling point.
It is 355～490 ℃ hydro carbons that wax oil component of the present invention refers to conventional boiling point.
Heavy oil component of the present invention refers to conventional boiling point and is higher than 490 ℃ hydro carbons.
Moisture poor quality oil of the present invention refers to aqueous low grade oils.
It is a principal object of the present invention to: use hydrocarbon at interval in the poor quality oil dehydration, make the hydro carbons that leaves the pre-steam stream T1V of dehydration Tata by all or mainly forming by interval hydrocarbon component, logistics T1V is separated into fluid T1VL and water liquid T1VW at oily water separation part SP, fluid can return the dehydration tower top and use as trim the top of column, the oil-contg of water liquid T1VW is low, the oil ingredient character of water liquid T1VW is enhanced, and water liquid T1VW can adopt conventional cheaply oil-contaminated water processing method to handle and final qualified discharge under the optimal cases; The present invention is suitable for the dehydration of poor quality oils such as coalite tar, coal-tar middle oil, carbolineum, and hydrocarbon can transform the gained low boiling hydrocarbon for hydrogenation of tar at interval.
Another important goal of the present invention is: utilize the oxygen-free characteristics of water liquid T1VW to be heated to be converted into steam to be used for suitable technological process, pumped vacuum systems power steam or as the separating obtained residuum coking process of poor quality oil steam during as the stripped vapor that uses as the poor quality oil dehydration tower or as the dehydration tower decompression operation, alternative fresh water.
Aqueous low grade oils of the present invention refers to oily water separation difficulty (disengaging time is long or degree of being separated from each other is low) oil product.
Oily water separation degree of being separated from each other of the present invention is low, refer to the oily water separation balance after, the water-content of oil phase higher or and the oil-contg of water higher.
Oily water separation degree of being separated from each other of the present invention is low, and water-content is higher in the oil phase, refer to oil product when entering the following process program water-content may exceed standard, limit usually such as the oil hydrogenation process that water-content is lower than 500PPm or lower in the oil phase.
Oily water separation degree of being separated from each other of the present invention is low, the oil-contg of water is higher, refer to water when entering the following process program oil-contg may exceed standard, usually oil content severe overweight when containing tar and waste water and enter sewage work, for this reason, generally will contain tar and waste water and introduce the incinerator burning.
Interval of the present invention hydrocarbon, the oil water separation process of the mixture that itself and water form must be easy to finish (starting time is short), relative separation degree height, and particularly, its relevant nature is preferably suitable with the relevant nature of petroleum base gasoline (or petroleum naphtha).
Described interval hydrocarbon, its component must comprise than the low component of poor quality oil hydro carbons initial boiling point, described interval hydrocarbon hydro carbons initial boiling point is than poor quality oil hydro carbons initial boiling point: general minimum low 30 ℃, minimum low 50 ℃ usually, preferably minimum low 70 ℃, so that guarantee " effect at interval ".
" at interval " implication of interval of the present invention hydrocarbon refers to: realize effect of the present invention based on " poor quality oil hydro carbons initial boiling point-interval hydrocarbon hydro carbons initial boiling point " difference (initial boiling point interval width).Usually, " poor quality oil hydro carbons initial boiling point-interval hydrocarbon hydro carbons initial boiling point " difference is the bigger the better.
Interval of the present invention hydrocarbon can be any suitable hydrocarbon ils, can be the lower boiling hydrocarbon ils from the factory outside, and can be have the lower boiling hydrocarbon ils of harmful effect from other device of inside plants to coal tar fractional distillation yet.
Interval of the present invention hydrocarbon, it can be any suitable hydrocarbon ils, because the hydrogenated oil that the coal tar hydrogenating conversion process generates is easy to obtain and character is suitable, for the dehydration of coal tar, the present invention recommends to use as far as possible the lower boiling hydrogenated oil of coal tar hydrogenating conversion process generation.
As mentioned above, interval of the present invention hydrocarbon, it can be any suitable hydrocarbon ils, because the final hydrogenated oil that coal tar two-stage method hydroconversion process generates is easy to obtain and character is suitable, for the dehydration of coal tar, the present invention recommends to use as far as possible the lower boiling hydrocarbon ils of second section hydrogenated oil of coal tar two-stage method hydroconversion process
Poor quality oil coal tar of the present invention, it can be the oil product that coalite tar or its distillate or its coking hot-work generate, it can be the oil product that coal-tar middle oil or its distillate or its coking hot-work generate, can be coal-tar heavy oil carbolineum or coal-tar heavy oil washing oil, can be the mixing oil of aforementioned oil product.
Coal tar hydrogenating conversion process of the present invention, feed coal tar is made up of the component of suitable hydrocracking.
Coalite tar in of the present invention, can be in blue carbon byproduct coal-tar middle oil of coal system or the coal gasification course byproduct coalite tar in oil or other high phenol content coalite tar or they contain phenol cut or their mixing oil.Carry out hot-work (such as coking, viscosity breaking etc.) if centering coalite tar or its contain the phenol cut, carbolic oil is extracted earlier in suggestion, and the cut that will extract then behind the carbolic oil is sent into hot procedure.
The present invention be applied to described in during coalite tar, dehydration tower can be the tar separation column simultaneously, can isolate carbolic oil, will can isolate residual oil simultaneously if contain the residue fraction that is not suitable for hydrocracking in the raw material.To extract lower boiling phenol (phenol, cresols, xylenol) when being target, the carbolic oil boiling range is generally 170～235 ℃.
When poor quality oil of the present invention is coal-tar heavy oil carbolineum or coal-tar heavy oil washing oil, dehydration tower can be the poor quality oil separation column simultaneously, poor quality oil is separated into mainly by conventional boiling point be lower than poor quality oil light constituent that 315 ℃ hydrocarbon component forms and mainly be higher than the poor quality oil heavy constituent that 315 ℃ hydrocarbon component is formed by conventional boiling point.
Coalite tar hydro-upgrading process in of the present invention, the raw material of processing are the middle coalite tar that the is suitable for hydrocracking cut lighter than cinder oil ingredient of coal tar (normally from).According to the present invention, because phenol price height, coal tar enters before the hydrocracking device, has incited somebody to action phenol Separation and Recovery wherein usually.
Because raw coal character and coking or gas-making process condition all change within the specific limits, the character of middle coalite tar also changes within the specific limits.The conventional boiling point of the character of coalite tar is generally 100～830 ℃, is generally 120～710 ℃, is 160～350 ℃ especially in of the present invention, organic sometimes oxygen level is 2.5～15%, especially be 3.5～10%, be 5～10% more particularly.
According to the present invention, if coalite tar is used to prepare hydrogenating materials in described, then carry out before the hydrogenation, usually through dehydration with cross the process of filtering solid particulate.Coalite tar in described contains the coal-tar pitch matter that is not suitable for hydrocracking or heavy colloid sometimes, and cutting the separate part of carbolic oil this moment, also can obtain mainly being higher than the middle coalite tar residue product that 490 ℃ component is formed by conventional boiling point.
Coal tar hydrogenation modification process of the present invention refers to the process of improving the coal tar quality that generation consumes the hydrogenation reaction of hydrogen, and its process can comprise unifining process and or hydrocracking process.Unifining process of the present invention refers to demetalization, takes off carbon residue, takes off impurity element, aromatic hydrocarbons is saturated is the hydrogenation process of major objective.Hydrocracking process of the present invention refers to realize that the molecule cracking is the hydrogenation process of major objective.
Impurity element in the hydro carbons of the present invention comprises non-hydrogen, carbons such as oxygen, sulphur, nitrogen, chlorine.
Impurity composition in the hydrocarbons hydrogenation conversion reaction effluent of the present invention refers to the hydride of non-hydrocarbon component in the stock oil such as water, ammonia, hydrogen sulfide, hydrogenchloride etc.
Two-stage method hydrocarbon oil hydrogenation conversion process of the present invention refers to hydrotreatment process that the raw material hydrocarbon ils is converted into the finished product and comprises two hydrogenation reaction systems (one-stage hydrogenation reactive system and secondary hydrogenation reactive system) and supporting hydrogenated oil separate part (secondary hydrogenation generates separating of oil part and the one-stage hydrogenation that may exist generates separating of oil part).Two hydrogenation reaction systems form overall serial flow on the stock oil flow process.Two-stage method hydrogenation process of the present invention can be cancelled one-stage hydrogenation and generate separating of oil part.The hydrogenated oil separate part uses equipment such as separation column usually, and hydrogenated oil is separated into the narrow fraction oil product.
The final hydrogenated oil of poor quality oil of the present invention, refer to from two section first reaction zone reaction effluent or two section second reaction zone reaction effluent or the 3rd hydrogenation reaction effluent, finally derive from the conventional liq hydrocarbon of poor quality oil (not being to derive from process turning oil).
Poor quality oil is converted into the process of the final hydrogenated oil of poor quality oil, has experienced two hydroconversion reaction zones at least: one stage hydrofining reaction zone and another one hydroconversion reaction zone.
The all final hydrogenated oil of poor quality oil of the present invention, refer to all final hydrogenated oil, common each final hydrogenated oil all enters corresponding separation system and carries out Separation and Recovery, the separation system of final hydrogenated oil can produce turning oil (entering the hydroconversion reaction zone cyclic process) when producing the finished product in the present invention.
Secondary hydrogenation of the present invention generates oil, refer to from two section second reaction zone reaction effluent and or two section first reaction zone reaction effluent, finally derive from the conventional liq hydrocarbon of poor quality oil (not being to derive from process turning oil).
For coal-tar middle oil or coalite tar carry out the two-stage method hydrogenation produce the fine-quality diesel oil component and or petroleum naphtha component process, the one-stage hydrogenation reaction process is a unifining process usually, the secondary hydrogenation reaction process is a hydrocracking process.Described one stage hydrofining catalyzer can be the series combination of one or both or multiple catalyzer or load in mixture.The one stage hydrofining catalyzer can be Hydrobon catalyst and combinations thereof such as the hydrogenating desulfurization agent used of the unifining process of refining of petroleum diesel oil and/or wax oil, hydrodenitrification agent, hydrogenation aromatic hydrocarbons saturator.Because coal-tar middle oil or coalite tar metal content are higher usually, so use hydrogenation protecting agent (hydrodemetallation (HDM) agent) in one stage hydrofining reaction process (being usually located at the front portion of reaction process) usually.According to the present invention, one section under preferred operational condition, the target that can reach is: the nitrogen content of hydrotreated naphtha (mean value) generally is lower than 100PPm, is usually less than 30PPm, is preferably lower than 10PPm; The cetane value of hydrogenated diesel oil (mean value) improves more than 10, preferably improves more than 15 with boiling point component cetane value (mean value) than high-density high aromatic oil.According to the present invention, generate the oil separation part branch at one-stage hydrogenation and obtain that one-stage hydrogenation generates innage boiling point fraction 1HBO (being generally the wax oil cut) and one-stage hydrogenation generates oily low boiler cut 1LBO.In the secondary hydrogenation reactive moieties, at least a portion 1HBO enters secondary hydrogenation cracking reaction district and contacts with the secondary hydrogenation cracking catalyst and finish the secondary hydrogenation cracking reaction and be converted into secondary hydrogenation cracking reaction effluent.The hydrocracking catalyst that secondary hydrogenation cracking reaction district uses can be the series combination of one or both or multiple catalyzer and load in mixture, the secondary hydrogenation cracking catalyst can be suitable petroleum refining process diesel oil (comprising poor ignition quality fuel) and/or wax oil/or the hydrocracking process of heavy oil hydrocracking catalyst (comprise and relax cracking catalyst) and combination thereof of using, can select amorphous (sial) hydrocracking catalyst of not fusion molecular sieve or amorphous (sial) hydrocracking catalyst of a small amount of fusion molecular sieve for use, to strengthen adaptive faculty as far as possible to organic nitrogen compound in the raw material, improve the diesel component productive rate, also can use Hydrobon catalyst and hydrocracking catalyst and back catalyst for refining to carry out grating.Secondary hydrogenation cracking reaction one speech of the present invention, refer under hydrogen and appropriate catalyst existence condition, the reaction process (comprising cracking reaction usually) of the consumption hydrogen that 1HBO takes place, its minimum reaction depth should possess MIN industrial significance: such as the fraction of diesel oil of producing expection character, should be according to HBO character, expection fraction of diesel oil character and hydrocracking catalyst 2R1C performance are determined: in the hope of improving the fraction of diesel oil cetane value, reduce fraction of diesel oil density to re-set target, take into account liquid yield simultaneously, this process cracking conversion rate is generally 20～80%, be generally 35～65%.
According to coking heavy oil of coal tar process of the present invention, mainly be higher than coal-tar middle oil heavy oil or the coalite tar heavy oil that 490 ℃ of components are formed by atmospheric boiling point, partly finish pyrogenic reaction in pyrogenic reaction and be converted into conventional gas hydrocarbon, coking generation oil and coke.Pyrogenic reaction part operation condition is generally: temperature is that 400～550 ℃, pressure are normal pressure～2.0MPa.The preferred operational condition of pyrogenic reaction part is: temperature is that 435～530 ℃, pressure are normal pressure～1.0MPa.Pyrogenic reaction part optimal operation conditions is: temperature is that 435～495 ℃, pressure are normal pressure～1.0MPa.Pyrogenic reaction product productive rate of the present invention is: 15～30% conventional gas hydrocarbon, 15～35% coking generate oil, 45～65% cokes.
According to the present invention, in poor quality oil dehydration part, use hydrocarbon (low boiling hydrocarbon that oil-water separation is good) 2F at interval in poor quality oil 1F dehydration, the hydro carbons of the steam stream T1V that leaves dehydration tower T1 cat head mainly is made up of interval hydrocarbon component, and T1V obtains fluid T1VL and water liquid T1VW in oily water separation part SP separated stream.
Poor quality oil dehydration part of the present invention, refer to and use dehydration tower T1 to finish the part of poor quality oil 1F dehydration task, dehydration tower T1 can be the poor quality oil separation column simultaneously, its operational condition (comprises boiling range according to poor quality oil character, cut character, poor quality oil is to the cracking susceptibility or the easily condensation of temperature), the specific requirement of fractionation purpose (the dehydration task is separated task with hydro carbons) is determined, the parameter or the factor that need to determine comprise: the working pressure of tower, the structure of tower (total number of theoretical plate, each functional section number of theoretical plate, the setting that refluxes in the stage casing), the heat-supplying mode of tower (the low reboiler furnace of charging process furnace or tower is set), the heat-obtaining mode of tower (cat head water cooler or stage casing reflux cooler are set), the pressure reducing mode of tower (cat head vacuumizes and or the low water vapor stripping reduction oil gas dividing potential drop of using of tower), the sideline product quality controling mode (side line extract out liquid as product or be provided with side line extract out liquid carry heat up in a steamer tower or be provided with side line extract liquid steam stripped tower out or side line be set extract the liquid vacuum evaporating tower out), and the thermal exchange scheme between the dewatering system logistics, although project is more, but all belong to conventional this category of distillatory skill, these personnel of skill of this area all can judge.
Poor quality oil also contains harmful solid particulate (such as the solid particulate of diameter greater than 10～20 microns) usually; in order to prevent that harmful solid particulate from damaging hydrofining stock oil high-pressure delivery pump and being deposited on the one stage hydrofining beds, filters usually under the forward and backward proper temperature condition of dewatering.
The present invention advise poor quality oil enter the one stage hydrofining beds before (usually at described poor quality oil separate part) dewater and filtration treatment.
The dehydration of poor quality oil of the present invention comprises the hydrocarbon component sepn process of poor quality oil usually under the possible situation.
Coalite tar in of the present invention usually contains conventional boiling point at least between 100～490 ℃ cut, also may contain the coal-tar residue oil ingredient.
Coalite tar dehydration part in of the present invention, its hydrocarbon ils product has 2 usually at least, and one of them is the dehydration overhead oil.
Coalite tar dehydration part in of the present invention, usually adopt the operation of underpressure distillation separate mode, its underpressure distillation column overhead working pressure generally is lower than 0.06MPa, is usually less than 0.04MPa, to reduce the still-process temperature, cuts down the consumption of energy or slows down condensation and react with coking.
Coalite tar dehydration part in of the present invention, when handling wide fraction coal tar, usually comprise main fractionating tower, carbolic oil and carry and heat up in a steamer tower and adjacent high boiling point product and carry and heat up in a steamer tower, its objective is the conventional boiling range scope of control carbolic oil cut: be generally 160～240 ℃, be preferably 170～235 ℃.The described mode of operation of heating up in a steamer tower of carrying can be used modes such as reboiler or steam stripped, extracts the side line of main fractionating tower out separating of oil be oil and side line overhead gas (returning main fractionating tower) at the bottom of the side line tower.
Coalite tar dehydration part in of the present invention, handle narrow fraction coal tar when (being higher than low 240 ℃ of 160 ℃ or the conventional boiling point of final boiling point) such as the conventional boiling point of initial boiling point, can use a separation column to finish carbolic oil and cut, because can control the conventional boiling range scope of carbolic oil cut: be generally 160～240 ℃, be preferably 170～235 ℃.
Below describe the present invention in detail.
A kind of poor quality oil dewatering is characterized in that comprising following steps:
1. in poor quality oil dehydration part, use interval hydrocarbon 2F that the hydro carbons of the overhead vapor stream T1V that leaves the dehydration tower T1 that handles poor quality oil 1F mainly is made up of interval hydrocarbon component, T1V obtains fluid T1VL and water liquid T1VW in oily water separation part SP separated stream.
In order to reach best effect of the present invention, it is characterized in that:
1. hydrocarbon 2F joins in the dehydration tower T1 continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, at least a portion fluid T1VL returns dehydration tower T1 and uses as trim the top of column, and at least a portion fluid T1VL leaves oily water separation part SP and uses as dehydration tower T1 cat head light oil products.
Can be steam with water liquid T1VW thermal conversion, stripped vapor that uses as dehydration tower T1 or pumped vacuum systems power steam or as the separating obtained residuum coking process of poor quality oil 1F steam during as dehydration tower T1 decompression operation.
When the present invention was applied to dehydration inferior, hydrocarbon 2F can be 1F hydroconversion process HR gained low boiling hydrocarbon product at interval, and hydrocarbon 2F is preferably 1F hydrocracking gained and mainly is lower than the conventional liq hydrocarbon that 150 ℃ component is formed by conventional boiling point final boiling point at interval.At this moment, hydrocarbon 2F joins dehydration tower T1 top continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, part fluid T1VL returns dehydration tower T1 and uses as trim the top of column, part fluid T1VL leaves oily water separation part SP and recycles as the stock oil of 1F hydroconversion process HR
Poor quality oil 1F can be higher than 100 ℃ following oil product for conventional boiling point initial boiling point: coalite tar or coalite tar distillate or the coking of coalite tar coking thermally splitting gained generate oil or coal-tar middle oil or coal-tar middle oil distillate or coal-tar middle oil coking thermally splitting gained coking generation oil or coal-tar heavy oil carbolineum or coal-tar heavy oil washing oil or petroleum base hydrocarbon ils inferior or shale oil base hydrocarbon ils inferior
Dehydration tower T1 of the present invention operates under reduced pressure usually, and dehydration tower T1 cat head working pressure is usually less than 0.06MPa (absolute pressure).
Interval of the present invention hydrocarbon hydro carbons initial boiling point is than poor quality oil hydro carbons initial boiling point: general minimum low 30 ℃, minimum low 50 ℃ usually, preferably minimum low 70 ℃.
The present invention's hydrocarbon at interval can form short-circuit cycle, and hydrocarbon 2F joins the epimere of dehydration tower T1 continuously at interval, and at least a portion fluid T1VL leaves oily water separation part SP as recycling as interval hydrocarbon 2F.
The present invention interval hydrocarbon adds the implantation site and is generally: hydrocarbon 2F joins the epimere of dehydration tower T1 continuously at interval, hydrocarbon 2F opening for feed position is 1～15 apart from dehydration tower T1 cat head number of theoretical plate at interval, and hydrocarbon 2F opening for feed position is 1～15 apart from an adjacent high boiling liquid extraction mouthful number of theoretical plate at interval.
The present invention interval hydrocarbon adds the implantation site and is preferably: hydrocarbon 2F joins the epimere of dehydration tower T1 continuously at interval, hydrocarbon 2F opening for feed position is 5～10 apart from dehydration tower T1 cat head number of theoretical plate at interval, and hydrocarbon 2F opening for feed position is 5～10 apart from an adjacent high boiling liquid extraction mouthful number of theoretical plate at interval.
Embodiment one
Interval hydrocarbon character such as table 2, coalite tar character such as table 3, adopt the inventive method to dewater and the cut cutting, dehydration tower (separation column) operational condition and products scheme see Table 4, table 5 is the number of theoretical plate certificate of dehydration tower, table 6 is the number of theoretical plate certificate of a side line tower, and table 7 is the number of theoretical plate certificate of two side line towers, and hydrocarbon recycles at interval.
Present embodiment dehydration part is provided with a dehydration tower (separation column) and two side lines and carries and heat up in a steamer tower, total two-way charging, first charging is heavy oil (account for total raw material amount 54.8%) and middle oil (account for total raw material amount 45.2%), second charging is a hydrocarbon at interval, and hydrocarbon removes moisture, removes the naphtha product of the fraction oil hydrogenation refining process of gained behind the coal-tar pitch from poor quality oil at interval.The whole distillates (comprising hydrocarbon component at interval) that obtain at dehydration tower all enter described unifining process as charging.Present embodiment dehydration tower (separation column), have five products, first product is the moisture light oil of cat head (mainly being lower than 115 ℃ hydrocarbon component by conventional boiling point in the hydrocarbon of interval forms), second product is the cat head oil-containing water, three products are that oil (being that 128～162 ℃ interval hydrocarbon heavy constituent and coal tar light constituent formed by conventional boiling range mainly) is extracted in the stage casing out, four-product is side line bottom product (being that 174～209 ℃ coal tar component is formed by conventional boiling range mainly), the 5th product is No. two side line bottom products (being that 234～390 ℃ coal tar component is formed by conventional boiling range mainly), and the 6th product is tower ground coal asphaltic products. (main be higher than 433 ℃ coal tar component by conventional boiling point form).
Fractionator overhead pressure is 0.037MPa (absolute pressure).
Use the present invention can reduce water-content in the cat head light oil, reduce the cat head oil-containing water oil-contg, improve the character of the oil ingredient of cat head oil-containing water.
Present embodiment, cat head oil-containing water do not contain the carbolineum component substantially, and cat head oil-containing water institute oily ingredient can go to conventional refinery sewage work to finish oily water treatment from the interval hydrocarbon.
The interval hydrocarbon character of table 2 embodiment one
| Project | Lightweight oil |
| Density (20 ℃), kg/m 3 | 780 |
| Boiling range, ℃ (ASTM D86) | |
| IBP/10％ | 65/92 |
| 30％/50％ | 102/113 |
| 70％/90％ | 125/143 |
| 95％/EBP | 151/165 |
The coalite tar character of table 3 embodiment one
* heavy oil distillation data are the simulation distil data
The dehydration tower operational condition table of table 4 embodiment one
| Sequence number | Technical scheme | Embodiment | |
| 1 | The coal tar operational condition | ||
| 1.1 | Wet basis coal tar flow, kg/h | 19253 | |
| 1.2 | Water content in the coal tar, kg/h | 1351.1 | |
| 1.3 | The coal tar temperature, ℃ | 350 | |
| 1.4 | Coal tar pressure, MPa (A) | 0.1 | |
| 2 | The naphtha feed operational condition | ||
| 2.1 | The naphtha feed flow, kg/h | 2090 | |
| 2.2 | The naphtha feed temperature, ℃ | 40 |
| 2.3 | Naphtha feed pressure, MPa (A) | 0.1 | |
| 3 | The separation column operational condition | ||
| 3.1 | Total cooling load, MMkcal/h | 4.5641 | |
| 3.2 | Top pressure, MPa (A) | 0.037 | |
| 3.3 | Head temperature, ℃ | 64 | |
| 3.4 | Reflux temperature, ℃ | 40 | |
| 3.5 | Overhead product | ||
| Overhead water extraction amount, kg/h | 2609.48 | ||
| Overhead oil extraction amount, kg/h | 1180.32 | ||
| ASTMD86,5% distillates a temperature, ℃ | 88.120 | ||
| ASTMD86,95% distillates a temperature, ℃ | 114.949 | ||
| 3.6 | Sideline product | ||
| Sideline product extraction amount, kg/h | 3300.458 | ||
| Extract temperature out, ℃ | 98 | ||
| ASTMD86,5% distillates a temperature, ℃ | 127.935 | ||
| ASTMD86,95% distillates a temperature, ℃ | 162.040 |
The dehydration tower operational condition table of continuous table 4 embodiment one
| Sequence number | Technical scheme | Embodiment | |
| 3.7 | A side line bottom product | ||
| Sideline product extraction amount, kg/h | 3619 | ||
| Extract temperature out, ℃ | 164 | ||
| Load at the bottom of the side line tower, MMkcal/h | 0.1299 |
| ASTMD86,5% distillates a temperature, ℃ | 173.643 | ||
| ASTMD86,95% distillates a temperature, ℃ | 209.293 | ||
| 3.8 | Two side line bottom products | ||
| Sideline product extraction amount, kg/h | 9152 | ||
| Extract temperature out, ℃ | 236 | ||
| Load at the bottom of the two side line towers, MMkcal/h | 0.3290 | ||
| ASTMD86,5% distillates a temperature, ℃ | 234.045 | ||
| ASTMD86,95% distillates a temperature, ℃ | 390.149 | ||
| 3.9 | Stripped vapor inlet amount at the bottom of the tower, kg/h | 1261 | |
| Stripped vapor feeding temperature at the bottom of the tower, ℃ | |||
| Stripped vapor feed pressure at the bottom of the tower, MPa (A) | 0.05 | ||
| 3.9 | Column bottom temperature, ℃ | 283 | |
| 4.0 | Tower ground coal asphaltic products. | ||
| Bottom product extraction amount, kg/h | 2742 | ||
| ASTMD86,5% distillates a temperature, ℃ | 432.994 | ||
| ASTMD86,95% distillates a temperature, ℃ | 630.205 |
The number of theoretical plate certificate of the dehydration tower of table 5 embodiment one
| Project | Numerical value |
| The total plate number of dehydration tower | 32 |
| Overhead oil is extracted plate out | 1 (return tank) |
| The overhead water ejecting plate | 1 (return tank) |
| Interval hydrocarbon feed plate | 3 |
| Plate is extracted in the stage casing out | 6 |
| One side line overhead gas Returning plate | 10 |
| One side line tower is extracted plate out | 10 |
| Two side line overhead gas Returning plates | 16 |
| Two side line towers are extracted plate out | 18 |
| The coal tar plate | 26 |
| Stripped vapor feed plate at the bottom of the tower | 32 (tower low spatials) |
| Tower ground coal pitch is extracted plate out | 32 (tower low spatials) |
The number of theoretical plate certificate of the side line tower of table 6 embodiment one
| Project | Numerical value |
| The total plate number of one side line tower | 8 |
| One side line tower feed plate | 1 |
| One side line column overhead gas is extracted plate out | 1 |
| One side line bottom product is extracted plate out | 8 |
The number of theoretical plate certificate of the two side line towers of table 7 embodiment one
| Project | Numerical value |
| The total plate number of two side line towers | 8 |
| Two side line tower feed plates | 1 |
| Two side line column overhead gas are extracted plate out | 1 |
| Two side line bottom products are extracted plate out | 8 |
Embodiment two
Interval hydrocarbon character such as table 8, carbolineum character such as table 9 adopt the inventive method to dewater and the cut cutting, and the number of theoretical plate of dehydration tower is according to seeing Table 10, and dehydration tower (separation column) operational condition and products scheme see Table 11, and the interval hydrocarbon recycles.
Present embodiment dehydration part is provided with a dehydration tower (separation column), total two-way charging, first charging is moisture 1.5% carbolineum, second charging is a hydrocarbon at interval, and hydrocarbon is from the naphtha product of the hydrocracking process of carbolineum two-stage method hydroconversion process (unifining process connect with hydrocracking process use) at interval.The whole hydrocarbon productss that obtain at dehydration tower all enter the unifining process of described carbolineum two-stage method hydroconversion process as charging.Present embodiment dehydration tower (separation column), have four products, first product is the moisture light oil of cat head (mainly being lower than 134 ℃ hydrocarbon component by conventional boiling point in the hydrocarbon of interval forms), second product is the cat head oil-containing water, three products are that oil (being made up of interval hydrocarbon heavy constituent and carbolineum light constituent) is extracted in the stage casing out, and four-product is extracted oily (being made up of the carbolineum heavy constituent) out at the bottom of for tower.Fractionator overhead pressure is 0.037MPa (absolute pressure).
Use the present invention can reduce water-content in the cat head light oil, reduce the cat head oil-containing water oil-contg, improve the character of the oil ingredient of cat head oil-containing water.
Present embodiment, cat head oil-containing water do not contain the carbolineum component substantially, and cat head oil-containing water institute oily ingredient can go to conventional refinery sewage work to finish oily water treatment from the interval hydrocarbon.
Table 8 embodiment two is hydrocarbon character at interval
| Project | The interval hydrocarbon |
| Density (20 ℃), kg/m 3 | 798.4 |
| Boiling range, ℃ (ASTM D86) | |
| IBP/10％ | 66/92 |
| 30％/50％ | 102/112 |
| 70％/90％ | 125/143 |
| 95％/EBP | 151/166 |
Table 9 embodiment two raw material carbolineum character
The number of theoretical plate certificate of table 10 embodiment two dehydration towers
| Project | Numerical value |
| The total plate number of dehydration tower | 26 |
| Overhead oil is extracted plate out | 1 (return tank) |
| The overhead water ejecting plate | 1 (return tank) |
| Interval hydrocarbon feed plate | 8 |
| Plate is extracted in the stage casing out | 15 |
| The carbolineum feed plate | 23 |
| Plate is extracted in the carbolineum heavy constituent out | 26 (tower low spatials) |
Table 11 embodiment two dehydration tower operational condition tables
| Sequence number | Technical scheme | Embodiment | |
| 1 | Carbolineum feed operation condition | ||
| 1.1 | Butt carbolineum feed rate, kg/h | 12500 | |
| 1.2 | Water content in the carbolineum, kg/h | 187.5 | |
| 1.3 | The carbolineum feeding temperature, ℃ | 325 | |
| 1.4 | The carbolineum feed pressure, MPa | 0.1 | |
| 2 | The naphtha feed operational condition | ||
| 2.1 | The naphtha feed flow, kg/h | 1611 | |
| 2.2 | The naphtha feed temperature, ℃ | 100 | |
| 2.3 | Naphtha feed pressure, MPa | 0.1 | |
| 3 | Dehydration tower (separation column) operational condition | ||
| 3.1 | The cat head cooling load, MMkcal/h | 0.6621 | |
| 3.2 | Top pressure, MPa | 0.037 | |
| 3.3 | Head temperature, ℃ | 75 | |
| 3.4 | Reflux temperature, ℃ | 40 | |
| 3.5 | Overhead product | ||
| Overhead water extraction amount, kg/h | 186 | ||
| Overhead oil extraction amount, kg/h | 1330 | ||
| ASTMD86,5% distillates a temperature, ℃ | 80 | ||
| ASTMD86,95% distillates a temperature, ℃ | 134 | ||
| 3.6 | Sideline product |
| Sideline product extraction amount, kg/h | 3583 | ||
| Extract temperature out, ℃ | 183 | ||
| ASTMD86,5% distillates a temperature, ℃ | 175 | ||
| ASTMD86,95% distillates a temperature, ℃ | 358 | ||
| 3.7 | Column bottom temperature, ℃ | 310 | |
| 3.8 | Bottom product | ||
| Bottom product extraction amount, kg/h | 9199 | ||
| ASTMD86,5% distillates a temperature, ℃ | 316 |
Embodiment three
Interval hydrocarbon character such as table 12, semi coking tar character such as table 13, adopt the inventive method to dewater and the cut cutting, dehydration tower (separation column) operational condition and products scheme see Table 14, table 15 is the number of theoretical plate certificate of dehydration tower, table 16 is the number of theoretical plate certificate of a side line tower, and table 17 is the number of theoretical plate certificate of two side line towers, and hydrocarbon recycles at interval.
Present embodiment dehydration part is provided with a dehydration tower (separation column) and two side lines and carries and heat up in a steamer tower, total two-way charging, first charging is moisture 4.14% coal tar, second charging is a hydrocarbon at interval, and hydrocarbon removes moisture, removes the naphtha product of the fraction oil hydrogenation refining process of gained behind the coal-tar pitch from first raw material hydrocarbon at interval.The whole distillates (comprising hydrocarbon component at interval) that obtain at dehydration tower all enter described unifining process as charging.Present embodiment dehydration tower (separation column), have seven products, first product is the moisture light oil of cat head (mainly being lower than 115 ℃ hydrocarbon component by conventional boiling point in the hydrocarbon of interval forms), second product is the cat head oil-containing water, three products are that oil (being that 116～159 ℃ interval hydrocarbon heavy constituent and coal tar light constituent formed by conventional boiling range mainly) is extracted in the stage casing out, four-product is side line bottom product (being that 168～235 ℃ coal tar component is formed by conventional boiling range mainly), the 5th product is No. two side line bottom products (being that 243～340 ℃ coal tar component is formed by conventional boiling range mainly), the 6th product is that oil (being that 340～464 ℃ coal tar component is formed by conventional boiling range mainly) is extracted in second stage casing out, and the 7th product is tower ground coal asphaltic products. (main be higher than 468 ℃ coal tar component by conventional boiling point form).
Fractionator overhead pressure is 0.035MPa (absolute pressure).
Use the present invention can reduce water-content in the cat head light oil, reduce the cat head oil-containing water oil-contg, improve the character of the oil ingredient of cat head oil-containing water.
Present embodiment, the tar component content of cat head oil-containing water is lowered, and cat head oil-containing water institute oily ingredient major part can be used to take place steam from the interval hydrocarbon, as the stripped vapor of dehydration tower in the present embodiment.
Table 12 is implemented three interval hydrocarbon character
| Project | Lightweight oil |
| Density (20 ℃), kg/m 3 | 743.9 |
| Boiling range, ℃ (ASTMD86) | |
| IBP/10％ | 98/102 |
| 30％/50％ | 109/121 |
| 70％/90％ | 132/137 |
| 95％/EBP | 141/147 |
The coal tar character (butt) of table 13 embodiment three
The dehydration tower operational condition table of table 14 embodiment three
| Sequence number | Technical scheme | Embodiment | |
| 1 | The coal tar operational condition | ||
| 1.1 | Wet basis coal tar flow, kg/h | 42422 | |
| 1.2 | Water content in the coal tar, kg/h | 1758 | |
| 1.3 | The coal tar temperature, ℃ | 364 | |
| 1.4 | Coal tar pressure, MPa (A) | 0.1 | |
| 2 | The naphtha feed operational condition | ||
| 2.1 | The naphtha feed flow, kg/h | 5928 | |
| 2.2 | The naphtha feed temperature, ℃ | 45 | |
| 2.3 | Naphtha feed pressure, MPa (A) | 0.1 | |
| 3 | The separation column operational condition | ||
| 3.1 | Total cooling load, MMkcal/h | 8.4578 | |
| 3.2 | Top pressure, MPa (A) | 0.035 | |
| 3.3 | Head temperature, ℃ | 48 | |
| 3.4 | Reflux temperature, ℃ | 40 | |
| 3.5 | Overhead product | ||
| Overhead water extraction amount, kg/h | 5534 | ||
| Overhead oil extraction amount, kg/h | 2050 | ||
| ASTMD86,5% distillates a temperature, ℃ | 85.7 | ||
| ASTMD86,95% distillates a temperature, ℃ | 104.5 | ||
| 3.6 | Product is extracted in first stage casing out |
| The first stage casing product extraction amount, kg/h | 4790 | ||
| Extract temperature out, ℃ | 86 | ||
| ASTMD86,5% distillates a temperature, ℃ | 122.6 | ||
| ASTMD86,95% distillates a temperature, ℃ | 143.8 |
The dehydration tower operational condition table of continuous table 14 embodiment three
| Sequence number | Technical scheme | Embodiment | |
| 3.7 | A side line bottom product | ||
| Sideline product extraction amount, kg/h | 3671 | ||
| Extract temperature out, ℃ | 156 | ||
| Load at the bottom of the side line tower, MMkcal/h | 0.1269 | ||
| ASTMD86,5% distillates a temperature, ℃ | 171.8 | ||
| ASTMD86,95% distillates a temperature, ℃ | 225.0 | ||
| 3.8 | Two side line bottom products | ||
| Sideline product extraction amount, kg/h | 8321 | ||
| Extract temperature out, ℃ | 242 | ||
| Load at the bottom of the two side line towers, MMkcal/h | 0.3011 | ||
| ASTMD86,5% distillates a temperature, ℃ | 249.9 | ||
| ASTMD86,95% distillates a temperature, ℃ | 328.5 | ||
| 3.9 | Product is extracted in second stage casing out | ||
| The second stage casing product extraction amount, kg/h | 22124 | ||
| Extract temperature out, ℃ | 301 |
| ASTMD86,5% distillates a temperature, ℃ | 344.1 | ||
| ASTMD86,95% distillates a temperature, ℃ | 442.6 | ||
| 3.10 | Stripped vapor inlet amount at the bottom of the tower, kg/h | 3783 | |
| Stripped vapor feeding temperature at the bottom of the tower, ℃ | |||
| Stripped vapor feed pressure at the bottom of the tower, MPa (A) | 0.10 | ||
| Column bottom temperature, ℃ | 327 | ||
| 3.11 | Tower ground coal asphaltic products. | ||
| Bottom product extraction amount, kg/h | 5643 | ||
| ASTMD86,5% distillates a temperature, ℃ | 503.1 | ||
| ASTMD86,95% distillates a temperature, ℃ | 696.2 |
The number of theoretical plate certificate of the dehydration tower of table 15 embodiment three
| Project | Numerical value |
| The total plate number of dehydration tower | 40 |
| Overhead oil is extracted plate out | 1 (return tank) |
| The overhead water ejecting plate | 1 (return tank) |
| Interval hydrocarbon feed plate | 5 |
| Plate is extracted in first stage casing out | 10 |
| One side line overhead gas Returning plate | 14 |
| One side line tower is extracted plate out | 15 |
| Two side line overhead gas Returning plates | 20 |
| Two side line towers are extracted plate out | 22 |
| Plate is extracted in second stage casing out | 29 |
| The coal tar plate | 34 |
| Stripped vapor feed plate at the bottom of the tower | 40 (tower low spatials) |
| Tower ground coal pitch is extracted plate out | 40 (tower low spatials) |
The number of theoretical plate certificate of the side line tower of table 16 embodiment three
| Project | Numerical value |
| The total plate number of one side line tower | 8 |
| One side line tower feed plate | 1 |
| One side line column overhead gas is extracted plate out | 1 |
| One side line bottom product is extracted plate out | 8 |
The number of theoretical plate certificate of the two side line towers of table 17 embodiment three
| Project | Numerical value |
| The total plate number of two side line towers | 8 |
| Two side line tower feed plates | 1 |
| Two side line column overhead gas are extracted plate out | 1 |
| Two side line bottom products are extracted plate out | 8 |
Although this paper only enumerates three embodiment, be enough to show effect of the present invention.
Claims (43)
1. poor quality oil dewatering is characterized in that comprising following steps:
1. in poor quality oil dehydration part, use interval hydrocarbon 2F that the hydro carbons of the overhead vapor stream T1V that leaves the dehydration tower T1 that handles poor quality oil 1F mainly is made up of interval hydrocarbon component, T1V obtains fluid T1VL and water liquid T1VW in oily water separation part SP separated stream.
2. method according to claim 1 is characterized in that:
1. hydrocarbon 2F joins in the dehydration tower T1 continuously at interval, and the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, and at least a portion fluid T1VL returns dehydration tower T1 and uses as trim the top of column.
3. method according to claim 2 is characterized in that:
1. interval hydrocarbon 2F joins the epimere of dehydration tower T1 continuously, and at least a portion fluid T1VL leaves oily water separation part SP and uses as dehydration tower T1 cat head light oil products.
4. method according to claim 1 is characterized in that:
2. be that steam uses with water liquid T1VW thermal conversion.
5. method according to claim 4 is characterized in that:
2. be that steam is used as the stripped vapor that dehydration tower T1 uses with water liquid T1VW thermal conversion.
6. method according to claim 4 is characterized in that:
2. with water liquid T1VW thermal conversion steam pumped vacuum systems power steam when being used as dehydration tower T1 decompression operation.
7. method according to claim 4 is characterized in that:
2. be that steam is used as the separating obtained residuum coking process of poor quality oil 1F steam with water liquid T1VW thermal conversion.
8. method according to claim 2 is characterized in that:
2. be that steam uses with water liquid T1VW thermal conversion.
9. method according to claim 8 is characterized in that:
2. be that steam is used as the stripped vapor that dehydration tower T1 uses with water liquid T1VW thermal conversion.
10. method according to claim 8 is characterized in that:
2. with water liquid T1VW thermal conversion steam pumped vacuum systems power steam when being used as dehydration tower T1 decompression operation.
11. method according to claim 8 is characterized in that:
2. be that steam is used as the separating obtained residuum coking process of poor quality oil 1F steam with water liquid T1VW thermal conversion.
12. method according to claim 3 is characterized in that:
2. be that steam uses with water liquid T1VW thermal conversion.
13. method according to claim 12 is characterized in that:
2. be that steam is used as the stripped vapor that dehydration tower T1 uses with water liquid T1VW thermal conversion.
14. method according to claim 12 is characterized in that:
2. with water liquid T1VW thermal conversion steam pumped vacuum systems power steam when being used as dehydration tower T1 decompression operation.
15. method according to claim 12 is characterized in that:
2. be that steam is used as the separating obtained residuum coking process of poor quality oil 1F steam with water liquid T1VW thermal conversion.
16., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. poor quality oil 1F is that conventional boiling point initial boiling point is higher than 100 ℃ coalite tar, hydrocarbon 2F is a 1F hydroconversion process HR gained low boiling hydrocarbon product at interval, hydrocarbon 2F joins dehydration tower T1 top continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, part fluid T1VL returns dehydration tower T1 and uses as trim the top of column, and a part of fluid T1VL leaves oily water separation part SP and recycles as the stock oil of 1F hydroconversion process HR.
17. method according to claim 16 is characterized in that:
1. at interval hydrocarbon 2F mainly is lower than the conventional liq hydrocarbon that 150 ℃ component is formed by conventional boiling point final boiling point.
18., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. poor quality oil 1F is that conventional boiling point initial boiling point is higher than 100 ℃ coalite tar distillate, hydrocarbon 2F is a 1F hydroconversion process HR gained low boiling hydrocarbon product at interval, hydrocarbon 2F joins dehydration tower T1 top continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, part fluid T1VL returns dehydration tower T1 and uses as trim the top of column, and a part of fluid T1VL leaves oily water separation part SP and recycles as the stock oil of 1F hydroconversion process HR.
19. method according to claim 18 is characterized in that:
1. at interval hydrocarbon 2F mainly is lower than the conventional liq hydrocarbon that 150 ℃ component is formed by conventional boiling point final boiling point.
20., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. poor quality oil 1F is that the conventional boiling point initial boiling point of coalite tar coking thermally splitting gained is higher than 100 ℃ coking generation oil, hydrocarbon 2F is a 1F hydroconversion process HR gained low boiling hydrocarbon product at interval, hydrocarbon 2F joins dehydration tower T1 top continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, part fluid T1VL returns dehydration tower T1 and uses as trim the top of column, and a part of fluid T1VL leaves oily water separation part SP and recycles as the stock oil of 1F hydroconversion process HR.
21. method according to claim 20 is characterized in that:
1. at interval hydrocarbon 2F mainly is lower than the conventional liq hydrocarbon that 150 ℃ component is formed by conventional boiling point final boiling point.
22., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. poor quality oil 1F is that conventional boiling point initial boiling point is higher than 100 ℃ coal-tar middle oil, hydrocarbon 2F is a 1F hydroconversion process HR gained low boiling hydrocarbon product at interval, hydrocarbon 2F joins dehydration tower T1 top continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, part fluid T1VL returns dehydration tower T1 and uses as trim the top of column, and a part of fluid T1VL leaves oily water separation part SP and recycles as the stock oil of 1F hydroconversion process HR.
23. method according to claim 22 is characterized in that:
1. at interval hydrocarbon 2F mainly is lower than the conventional liq hydrocarbon that 150 ℃ component is formed by conventional boiling point final boiling point.
24., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. poor quality oil 1F is that conventional boiling point initial boiling point is higher than 100 ℃ coal-tar middle oil distillate, hydrocarbon 2F is a 1F hydroconversion process HR gained low boiling hydrocarbon product at interval, hydrocarbon 2F joins dehydration tower T1 top continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, part fluid T1VL returns dehydration tower T1 and uses as trim the top of column, and a part of fluid T1VL leaves oily water separation part SP and recycles as the stock oil of 1F hydroconversion process HR.
25. method according to claim 24 is characterized in that:
1. at interval hydrocarbon 2F mainly is lower than the conventional liq hydrocarbon that 150 ℃ component is formed by conventional boiling point final boiling point.
26., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. poor quality oil 1F is that the conventional boiling point initial boiling point of coal-tar middle oil coking thermally splitting gained is higher than 100 ℃ coking and generates oily 1F, hydrocarbon 2F is a 1F hydroconversion process HR gained low boiling hydrocarbon product at interval, hydrocarbon 2F joins dehydration tower T1 top continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, part fluid T1VL returns dehydration tower T1 and uses as trim the top of column, and a part of fluid T1VL leaves oily water separation part SP and recycles as the stock oil of 1F hydroconversion process HR.
27. method according to claim 26 is characterized in that:
1. at interval hydrocarbon 2F mainly is lower than the conventional liq hydrocarbon that 150 ℃ component is formed by conventional boiling point final boiling point.
28., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. poor quality oil 1F is a coal-tar heavy oil carbolineum, hydrocarbon 2F is a 1F hydroconversion process HR gained low boiling hydrocarbon product at interval, hydrocarbon 2F joins dehydration tower T1 top continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, part fluid T1VL returns dehydration tower T1 and uses as trim the top of column, and a part of fluid T1VL leaves oily water separation part SP and recycles as the stock oil of 1F hydroconversion process HR.
29. method according to claim 28 is characterized in that:
1. at interval hydrocarbon 2F mainly is lower than the conventional liq hydrocarbon that 150 ℃ component is formed by conventional boiling point final boiling point.
30., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. poor quality oil 1F is the coal-tar heavy oil washing oil, hydrocarbon 2F is a 1F hydroconversion process HR gained low boiling hydrocarbon product at interval, hydrocarbon 2F joins dehydration tower T1 top continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, part fluid T1VL returns dehydration tower T1 and uses as trim the top of column, and a part of fluid T1VL leaves oily water separation part SP and recycles as the stock oil of 1F hydroconversion process HR.
31. method according to claim 30 is characterized in that:
1. at interval hydrocarbon 2F mainly is lower than the conventional liq hydrocarbon that 150 ℃ component is formed by conventional boiling point final boiling point.
32., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. poor quality oil 1F is that conventional boiling point initial boiling point is higher than 100 ℃ petroleum base hydrocarbon ils inferior, hydrocarbon 2F is a 1F hydroconversion process HR gained low boiling hydrocarbon product at interval, hydrocarbon 2F joins dehydration tower T1 top continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, part fluid T1VL returns dehydration tower T1 and uses as trim the top of column, and a part of fluid T1VL leaves oily water separation part SP and recycles as the stock oil of 1F hydroconversion process HR.
33. method according to claim 32 is characterized in that:
1. at interval hydrocarbon 2F mainly is lower than the conventional liq hydrocarbon that 150 ℃ component is formed by conventional boiling point final boiling point.
34., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. poor quality oil 1F is that conventional boiling point initial boiling point is higher than 100 ℃ shale oil base hydrocarbon ils inferior, hydrocarbon 2F is a 1F hydroconversion process HR gained low boiling hydrocarbon product at interval, hydrocarbon 2F joins dehydration tower T1 top continuously at interval, the hydro carbons of steam stream T1V all is made up of interval hydrocarbon component, part fluid T1VL returns dehydration tower T1 and uses as trim the top of column, and a part of fluid T1VL leaves oily water separation part SP and recycles as the stock oil of 1F hydroconversion process HR.
35. method according to claim 34 is characterized in that:
1. at interval hydrocarbon 2F mainly is lower than the conventional liq hydrocarbon that 150 ℃ component is formed by conventional boiling point final boiling point.
36., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. dehydration tower T1 operates under reduced pressure.
37. method according to claim 36 is characterized in that:
1. dehydration tower T1 cat head working pressure is lower than 0.06MPa (absolute pressure).
38., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. minimum low 30 ℃ of described interval hydrocarbon hydro carbons initial boiling points than poor quality oil hydro carbons initial boiling point.
39., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. minimum low 50 ℃ of described interval hydrocarbon hydro carbons initial boiling points than poor quality oil hydro carbons initial boiling point.
40., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
1. minimum low 70 ℃ of described interval hydrocarbon hydro carbons initial boiling points than poor quality oil hydro carbons initial boiling point.
41., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
3. interval hydrocarbon 2F joins the epimere of dehydration tower T1 continuously, and at least a portion fluid T1VL leaves oily water separation part SP and recycles as interval hydrocarbon 2F.
42., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
3. interval hydrocarbon 2F joins the epimere of dehydration tower T1 continuously, and hydrocarbon 2F opening for feed position is 1～15 apart from dehydration tower T1 cat head number of theoretical plate at interval, and hydrocarbon 2F opening for feed position is 1～15 apart from an adjacent high boiling liquid extraction mouth number of theoretical plate at interval.
43., it is characterized in that according to claim 1 or 2 or 3 or 4 or 5 or 6 or 7 or 8 or 9 or 10 or 11 or 12 or 13 or 14 or 15 described methods:
3. interval hydrocarbon 2F joins the epimere of dehydration tower T1 continuously, and hydrocarbon 2F opening for feed position is 5～10 apart from dehydration tower T1 cat head number of theoretical plate at interval, and hydrocarbon 2F opening for feed position is 5～10 apart from an adjacent high boiling liquid extraction mouth number of theoretical plate at interval.
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN108756857A (en) * | 2018-05-18 | 2018-11-06 | 中国海洋石油集团有限公司 | A kind of oil-sand pool foming period top gas distribution forecasting method |
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