CN106675646A - Weight lightening system and method for whole fraction of coal tar - Google Patents
Weight lightening system and method for whole fraction of coal tar Download PDFInfo
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- CN106675646A CN106675646A CN201611118045.4A CN201611118045A CN106675646A CN 106675646 A CN106675646 A CN 106675646A CN 201611118045 A CN201611118045 A CN 201611118045A CN 106675646 A CN106675646 A CN 106675646A
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G67/00—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only
- C10G67/02—Treatment of hydrocarbon oils by at least one hydrotreatment process and at least one process for refining in the absence of hydrogen only plural serial stages only
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Abstract
The invention relates to a weight lightening system and a weight lightening method for whole fraction of coal tar. A fractionating device (2) in the system provided by the invention has a coal tar inlet, a raw material light component outlet and a raw material heavy component outlet; a fixed bed hydrorefining device has a raw material light component inlet and a generated oil inlet; the raw material light component inlet is connected with the raw material light component outlet; moreover, the fractionating device (2), the fixed bed hydrorefining device, a three-phase separating device, a fixed bed hydrocracking device, a gas-liquid separating device and a fractionating device (7) are connected in sequence; the fractionating device (7) has a gasoline fraction outlet, a diesel fraction outlet and a heavy-weight fraction oil outlet; a mixing device has a raw material heavy component inlet, a heavy-weight fraction oil inlet, a catalyst inlet, a vulcanizer inlet and an oil slurry outlet; the raw material heavy component inlet is connected with the raw material heavy component outlet; the heavy-weight fraction oil inlet is connected with the heavy-weight fraction oil outlet. By using the weight lightening system and the weight lightening method, the utilization rates of the whole friction of the coal tar can be increased; a technical process is simplified.
Description
Technical field
The present invention relates to coal chemical technology, more particularly to a kind of full fraction of coal tar lighting system and method.
Background technology
As economic develops rapidly, China increasingly increases the demand of fuel oil.Due to most of fuel oil still need to from
Obtain in petroleum resources, the crude oil demand amount of China and external dependence degree are also increasing year by year.By 2014, crude oil in China
External dependence degree has reached 59.6%.Therefore, in the face of the problem and the energy general layout of the few oil of China's richness coal of petroleum resources shortage,
Obtain clean fuel from coal resource to have important practical significance.
Coal tar is the by-product of the dry distillation of coal, according to pyrolysis temperature, coal tar can be divided into into high temperature coal-tar, middle temperature coal tar
Oily and middle coalite tar etc..Compared with high temperature coal-tar, middle coalite tar arene content is relatively low, saturated hydrocarbon content phase
To higher, closer to the composition of oil.Therefore, middle coalite tar is more suitable for producing cleaning combustion by hydrotreating techniques
Material oil product.
Due in middle coalite tar containing the solid impurity such as substantial amounts of coal dust, pyrolytic carbon, and colloid, asphalt content compared with
It is high.Therefore, using traditional fixed bed hydrogenation technique processing coal tar, there is a problem of that easy green coke, cycle of operation are shorter.Native land
The technique that coal tar light component hydrogenation or delayed coking and fixed bed hydrogenation are combined inside is developed, but the utilization rate of coal tar is not
It is high.Also, though the impurity such as N, S, the O in coal tar can be removed using hydrofining technology, its lighting degree is relatively low, gained
Light-weight fuel oil product yield it is relatively low, economy is not high.Therefore, tied using suspension bed/slurry bed system/slurry bed system and fixed bed
Conjunction, hydrofinishing and the group technology for being hydrocracked combination, by maximizing coal tar utilization rate is improved, and produces light-weight fuel oil,
Improve the economy of coal tar processing.
Prior art discloses a kind of method of coal tar suspension bed catalytic hydrogenation.The method steams coal tar by normal pressure
Evaporate and be separated into carbolic oil fraction, diesel oil distillate and heavy oil fraction.Dephenolize oil is obtained after carbolic oil distillate dephenolizing, heavy oil fraction is suspended
Bed hydroprocessing cracking, is carried out after solid-liquid separation to isocrackate, and distillation obtains product liquid, using bottom of towe tail oil as recycle oil
Mix with heavy oil fraction, after the diesel oil distillate mixing in lighter products and dephenolize oil, raw material upgrading unit is entered.But, tower
Bottom tail oil is recycled directly back to suspended-bed reactor, is not processed further, and reaction depth is relatively low, and utilization rate is low, and the method flow process
It is more complicated.
Prior art two discloses a kind of method of process full fraction of coal tar to produce fuel oil.The method is by coal tar
Heavy distillat is mixed homogeneously with catalyst and vulcanizing agent, and hydrocracking reaction, product point are carried out into paste state bed reactor after sulfuration
Gasoline, diesel oil and hydrogenation tail oil are obtained after evaporating, partial hydrogenation tail oil returns to paste state bed reactor as recycle oil, remaining hydrogenation tail
Fixed bed reactors are entered after oil removing solid particle with coal tar light fraction, product fractionation obtains gasoline, diesel oil and hydrogenation tail
Oil.But, full fraction of coal tar lighting effect is poor, and coal tar utilization rate is relatively low, and technological process is complicated.
Prior art three discloses a kind of method of producing diesel by utilizing coal tar.Full fraction of coal tar is separated into richness by the method
Asphalitine phase and lean asphalitine phase, rich asphalitine phase mixes anti-into fixed bed Jing after slurry bed system hydrogenation reaction with lean asphalitine
Device is answered, after hydrogenation products cutting diesel product is obtained, a portion hydrogenated diesel oil mixes as recycle oil with coal tar raw material.
But, diesel cycle amount is larger, and diesel product quantum of output is less, product lighting low degree.
The content of the invention
It is an object of the invention to solve the problems, such as that coal tar utilization rate is relatively low, there is provided a kind of floating bed hydrogenation and fixed bed
The method of hydrogenation joint processing, effectively converts full fraction of coal tar, maximizes the light ends such as output gasoline and diesel oil, improves coal
Tar utilization rate.
In view of above-mentioned purpose, the present invention proposes a kind of full fraction of coal tar lighting system, including fractionating device (2),
Fixed bed hydrogenation refining plant, three-phase separating device, fixed bed hydrogenation cracking unit, gas-liquid separation device, fractionating device (7),
Mixing arrangement,
The fractionating device (2) is with coal tar oil-in, raw material light fraction outlet, Raw material recombination sub-export；
The fixed bed hydrogenation refining plant has raw material light component entrance, generates oil-in, and the raw material light component enters
Mouth is connected with the raw material light fraction outlet of the fractionating device (2)；
Wherein, the fractionating device (2), fixed bed hydrogenation refining plant, three-phase separating device, fixed bed hydrogenation cracking dress
Put, gas-liquid separation device, fractionating device (7) are sequentially connected；
The fractionating device (7) exports with gasoline fraction, diesel oil distillate is exported, heavy end oil export；
The mixing arrangement have Raw material recombination subentry, heavy end oil-in, catalyst inlet, vulcanizing agent entrance,
Slurry oil is exported, and the Raw material recombination subentry is connected with the Raw material recombination sub-export of the fractionating device (2), the heavy end
Oil-in is connected with the heavy end oil export of the fractionating device (7).
In said system, floating bed hydrocracking device, segregation apparatuss are further included；
The floating bed hydrocracking device has slurry oil entrance, isocrackate outlet, the slurry oil entrance and institute
State the slurry oil outlet connection of mixing arrangement；
The segregation apparatuss have isocrackate entrance, generate oil export, solid impurity outlet, described to be hydrocracked
Product inlet is connected with the isocrackate outlet of the floating bed hydrocracking device, and the generation oil export is solid with described
The generation oil-in connection of fixed bed hydro-refining unit.
The invention allows for a kind of method that utilization said system carries out full fraction of coal tar lighting, including following step
Suddenly：
Step A, by coal tar fractional distillation is carried out, and cut point T Raw material recombination point derived above is obtained below cut point T
Raw material light component；
Step B, the raw material light component is sent in the fixed bed hydrogenation refining plant carries out hydrofining reaction, instead
Answer product to carry out three phase separation, obtain gas phase, oil phase, water phase, the oil phase is carried out in the fixed bed hydrogenation cracking unit
Hydrocracking reaction, product carries out successively gas-liquid separation, fractional distillation, obtains gasoline fraction, diesel oil distillate, heavy distillate,
The heavy distillate is sent in the mixing arrangement via the heavy end oil-in.
The above-mentioned method for carrying out full fraction of coal tar lighting, also including step：The Raw material recombination that step A is obtained
Divide, catalyst, vulcanizing agent are also fed in the mixing arrangement, are mixed to get slurry oil, the slurry oil splits in the floating bed hydrogenation
Makeup carries out hydrocracking reaction in putting, product obtains generating oil, solid impurity after segregation apparatuss process, described
Generate oil to send in the fixed bed hydrogenation refining plant via the generation oil-in.
In the above-mentioned method for carrying out full fraction of coal tar lighting, the T is 350~370 DEG C.
In the above-mentioned method for carrying out full fraction of coal tar lighting, what the hydrofining reaction in step B was adopted adds
Hydrogen catalyst for refining is consisted of：1wt%~5wt% nickel oxide, 15wt%~30wt% tungsten oxides, 0.5wt%~3wt% oxygen
Change phosphorus, 62wt%~83.5wt% γ-Al2O3。
In the above-mentioned method for carrying out full fraction of coal tar lighting, the reaction temperature of the hydrofining reaction in step B
Spend for 340~370 DEG C, hydrogen partial pressure is 10~16MPa.
In the above-mentioned method for carrying out full fraction of coal tar lighting, what the hydrocracking reaction in step B was adopted adds
Hydrogen Cracking catalyst is consisted of：1wt%~5wt% nickel oxide, 10wt%~20wt% molybdenum oxides, 0.5wt%~5wt% oxygen
Change phosphorus, 70wt%~88.5wt% carriers；
The carrier is Y type molecular sieve and γ-Al2O3Mixture, wherein, the Y type molecular sieve accounts for the hundred of the carrier
Divide than being 10wt%~25wt%.
In the above-mentioned method for carrying out full fraction of coal tar lighting, the reaction temperature of the hydrocracking reaction in step B
Spend for 370~410 DEG C, hydrogen partial pressure is 10~16MPa.
In the above-mentioned method for carrying out full fraction of coal tar lighting, the catalyst be microspheroidal loaded catalyst, institute
Microspheroidal loaded catalyst particle diameter is stated for 100~300 μm；
The reaction temperature of the hydrocracking reaction is 400~440 DEG C, and hydrogen partial pressure is 10~16MPa.
In the present invention, after restructuring lease making floating bed hydrocracking device in coal tar is processed, be conducive to mechanical admixture and
The deposition of metal, converts the resin and asphalt of easy green coke in heavy constituent, is conducive to heavy constituent to occur in fixed bed device instead
Should, and carbon deposit therein is reduced, extend cycle of operation.
In the present invention, floating bed hydrocracking generates oil and is directly entered in fixed bed hydrogenation refining plant, carries out further
Lighting, while being further added by heavy constituent utilization rate, moreover it is possible to simplification of flowsheet.And the heavy that will be hydrocracked in generation oil evaporates
Divide oil circulation, floating bed hydrocracking device is entered after mixing with Raw material recombination point, be conducive to the further anti-of heavy distillate
Should, while diluting Raw material recombination point, the viscosity of reduction charging improves the mass transfer of reactant, reduces isocrackate and separates admittedly
The difficulty of body.Additionally, containing substantial amounts of fractional saturation aromatic hydrocarbons in heavy distillate, can promote in Raw material recombination point as hydrogen supply agent
The conversion of resin and asphalt.
Description of the drawings
Fig. 1 is full fraction of coal tar lighting system schematic in the present invention.
Fig. 2 is full fraction of coal tar lightening method schematic flow sheet in the present invention.
Reference in accompanying drawing is as follows：
1st, raw material preprocessing device；2nd, fractionating device；3rd, fixed bed hydrogenation refining plant；4th, three-phase separating device；5th, it is solid
Fixed bed hydrocracking unit；6th, gas-liquid separation device；7th, fractionating device；8th, mixing arrangement；9th, floating bed hydrocracking device,
10th, segregation apparatuss.
Specific embodiment
Below in conjunction with drawings and Examples, the specific embodiment of the present invention is described in more details, so as to energy
Enough more fully understand the solution of the present invention and the advantage of its various aspects.However, specific embodiments described below and reality
It is only descriptive purpose to apply example, rather than limitation of the present invention.
As shown in figure 1, being full fraction of coal tar lighting system schematic in the present invention.The system bag of the embodiment of the present invention
Include raw material preprocessing device 1, fractionating device 2, fixed bed hydrogenation refining plant 3, three-phase separating device 4, fixed bed hydrogenation cracking
Device 5, gas-liquid separation device 6, fractionating device 7, mixing arrangement 8, floating bed hydrocracking device 9, segregation apparatuss 10.
As seen from Figure 1, in system of the invention, the annexation of each device is as follows：
Raw material preprocessing device 1 is used to carry out pretreatment to coal tar raw material, and it has feed(raw material)inlet, material outlet.
Fractionating device 2 is used to carry out fractional distillation to coal tar, and it has coal tar oil-in, raw material light fraction outlet, raw material weight
Component is exported.It is defeated by material outlet for receiving also, coal tar oil-in is connected with the material outlet of raw material preprocessing device 1
The pretreated coal tar sent.
Fixed bed hydrogenation refining plant 3 carries out hydrofining reaction for raw material light component, and there is raw material light component to enter for it
Mouth, generation oil-in, hydrotreated product outlet.Also, the raw material light fraction outlet of raw material light component entrance and fractionating device 2
Connection.
Three-phase separating device 4 is used to separate hydrotreated product, and there is hydrotreated product entrance, gas phase to go out for it
Mouth, oil phase outlet, water are mutually exported.Also, the hydrotreated product entrance is produced with the hydrofinishing of fixed bed hydrogenation refining plant 3
Thing outlet connection.
Fixed bed hydrogenation cracking unit 5 is used for the hydrocracking reaction of gained oil phase after separation, and it has oil phase entrance, adds
Hydrogen crackate is exported.Also, the oil phase entrance is connected with the oil phase outlet of three-phase separating device 4.
Gas-liquid separation device 6 is used to separate isocrackate, and there is isocrackate entrance, hydrogenation to split for it
Change liquid product outlet.Also, the isocrackate entrance is exported with the isocrackate of fixed bed hydrogenation cracking unit 5
Connection.
Fractionating device 7 is used to carry out fractional distillation to being hydrocracked liquid product, and it has and is hydrocracked liquid product entrance, vapour
Oil distillate outlet, diesel oil distillate outlet, heavy end oil export.Also, this is hydrocracked liquid product entrance and gas-liquid separation
The liquid product entrance that is hydrocracked of device 6 connects.
Mixing arrangement 8 is used for mixing of the Raw material recombination point with heavy distillate etc., and it has heavy end oil-in, raw material
Restructuring subentry, catalyst inlet, vulcanizing agent entrance, slurry oil outlet.Also, the Raw material recombination subentry and fractionating device 2
Raw material recombination sub-export connects, and heavy end oil-in is connected with the heavy end oil export of fractionating device 7.
Floating bed hydrocracking device 9 is used for the hydrocracking reaction of slurry oil, and it has slurry oil entrance, isocrackate
Outlet.Also, the slurry oil entrance is connected with the slurry oil outlet of mixing arrangement 8.
Segregation apparatuss 10 are used to separate isocrackate, and it has isocrackate entrance, generates oil export, solid
Impurities outlet.Also, the isocrackate entrance is connected with the isocrackate outlet of floating bed hydrocracking device 9,
The generation oil-in is connected with the generation oil-in of fixed bed hydrogenation refining plant 3.It includes gas-liquid separation device, centrifugal device
And defecator.
To sum up, the system of the embodiment of the present invention includes following two technology paths：
1. raw material preprocessing device 1, fractionating device 2, fixed bed hydrogenation refining plant 3, three-phase separating device 4, fixed bed
Hydrocracking unit 5, gas-liquid separation device 6, fractionating device 7, mixing arrangement 8 are sequentially connected.
2. raw material preprocessing device 1, fractionating device 2, mixing arrangement 8, floating bed hydrocracking device 9, segregation apparatuss 10,
Fixed bed hydrogenation refining plant 3 is sequentially connected.
I.e. in the embodiment of the present invention, while there is light component treatment technology route 1. with heavy constituent treatment technology route 2.,
Also, this two technology paths form the technology path of two mutual circulations again.
As shown in Fig. 2 being full fraction of coal tar lightening method schematic flow sheet in the present invention.The side of the embodiment of the present invention
Method comprises the steps：
Step A：In raw material preprocessing device 1 after pretreatment, send in fractionating device 2 carries out fractional distillation to coal tar, point
Temperature T Raw material recombination point derived above is evaporated, raw material light component is obtained below cut point T.
Wherein, the coal tar in the present embodiment is middle coalite tar.Preprocessing process mainly includes being dehydrated and removing machine
Tool impurity.Dehydration employs conventional method in the art, in the present embodiment, selects and adds breakdown of emulsion in coal tar
Agent.Also, using the method removing mechanical admixture for filtering.
Cut point T is 350~370 DEG C.
Step B：The raw material light component that step A is obtained is sent in fixed bed hydrogenation refining plant 3, carries out hydrofinishing anti-
Should, the hydrotreated product for obtaining is sent in three-phase separating device 4 and is separated, and obtains gas phase, oil phase, water phase.Then, by oil
Mutually sending in fixed bed hydrogenation cracking unit 5 carries out hydrocracking reaction, and the isocrackate for obtaining is in gas-liquid separation device 6
Send in fractionating device 7 after middle separation, obtain gasoline fraction, diesel oil distillate, heavy distillate.
The step realizes the lighting of coal tar raw material light component fraction, obtains gasoline and diesel oil.
Resulting heavy distillate is sent in mixing arrangement 8 via heavy end oil-in, and it includes fraction oil distillate
And heavy oil fraction.
After hydrotreated product is separated in three-phase separating device 4, the gas phase for obtaining is after purification as circulation
Hydrogen is used for hydrogenation reaction, the water phase for obtaining outer row Jing after alkali cleaning.
In the step, hydrofining reaction has also used Hydrobon catalyst.The Hydrobon catalyst is support type
Catalyst, and major catalyst be Herba Trifolii Pratentis strip, a diameter of 2 ㎜.Carried metal is nickel tungsten system, and phosphorus is as auxiliary agent, carrier
γ-Al2O3.The Hydrobon catalyst is consisted of：1wt%~5wt% nickel oxide, 15wt%~30wt% tungsten oxides,
0.5wt%~3wt% phosphorous oxide, 62wt%~83.5wt% γ-Al2O3 (wt% is mass percent).On major catalyst
Portion load protective agent, the protective agent is the Raschig ring by made by inert material, for depositing oil product in remain metal and machinery
Impurity etc..
The reaction temperature of hydrofining reaction is 340~370 DEG C, and hydrogen partial pressure is 10~16MPa, and hydrogen to oil volume ratio is
800~1400, reaction velocity is 0.3~1.2h-1.Through hydrofining reaction, most of nitrogenous, oxygen, sulfur are stripped of in raw material
Compound, so as to meet the feed needs of follow-up hydrogenation cracking reaction.And the polycyclic aromatic hydrocarbon saturation in raw material is caused, favorably
Further there is hydrocracking reaction in it, promote the conversion of polycyclic aromatic hydrocarbon.
In the step, hydrocracking reaction has also used hydrocracking catalyst.The hydrocracking catalyst is difunctional
Loaded catalyst, catalyst be Herba Trifolii Pratentis strip, a diameter of 1.5 ㎜.Carried metal is nickel molybdenum system, and phosphorus is used as auxiliary agent.Carry
Body is γ-Al2O3With the mixture of Y type molecular sieve, wherein, Y type molecular sieve account for carrier percentage ratio be 10wt%~25wt%.
The hydrocracking catalyst consist of 1wt%~5wt% nickel oxide, 10wt%~20wt% molybdenum oxides, 0.5wt%~
5wt% phosphorous oxide, 70wt%~88.5wt% carriers.
The reaction temperature of hydrocracking reaction is 370~410 DEG C, and hydrogen partial pressure is 10~16MPa, and hydrogen to oil volume ratio is
800~1400, reaction velocity is 0.5~1.5h-1.Through hydrocracking reaction, the significantly lighting of coal tar is capable of achieving, is utilized
Rate is substantially improved, and the yield of gasoline and diesel oil is higher, remarkable in economical benefits.
Step C：Heavy distillate, Raw material recombination are distributed in mixing arrangement 8, while catalyst and vulcanizing agent are added,
Carry out being mixed to get slurry oil.Then, slurry oil is sent in floating bed hydrocracking device 9 carries out hydrocracking reaction, and hydrogenation splits
Change product after the process of segregation apparatuss 10, obtain generating oil, solid impurity.And it is solid via oil-in feeding is generated to generate oil
In fixed bed hydro-refining unit 3, with raw material light component hydrofining reaction is carried out.
Wherein, solid impurity is sent into into recovery system.The removal process includes：Solid impurity is sent into into pyrolytic reaction device
In carry out heat scission reaction, the oil phase for obtaining can mix with coal tar raw material after process, solid impurity burn after as catalyst
Recycle.
Catalyst in the step is microspheroidal loaded catalyst, and particle diameter is 100~300 μm, and carried metal is molybdenum, is carried
Body adopts amorphous aluminum silicate.Wherein, molybdenum oxide account for catalyst percentage ratio be 0.5wt%~2wt%, balance of amorphous silicon
Sour aluminum.
Amorphous silicic acid alumina supporter has stronger acidity, can promote the carrying out of hydrocracking reaction, and with preferable
Heat stability, can continually regenerate, and be conducive to catalyst to recycle.
The reaction temperature of slurry-bed hydrocracking be 400~440 DEG C, hydrogen partial pressure be 10~16MPa, hydrogen oil volume
Than for 600~1400, reaction velocity is 0.5~1.5h-1.Through slurry-bed hydrocracking, it is stripped of substantially in raw material
Easily green coke material, can completely convert the heavy constituent in raw material, substantially meet the requirement of fixed bed charging, realize the preliminary of raw material
Lighting, and tentatively remove sulfur, nitrogen, oxygen, metal impurities in raw material.
Embodiment
Coalite tar is raw material during embodiment 1 is selected, and according to step A pretreatment is carried out, and then analyzes raw material coal tar
Property, analysis result is as shown in table 1.
The property analysis result of the raw material coal tar of table 1
The coal tar after device is processed will be fractionated into and be separated into the raw material light component less than 370 DEG C and the original more than 370 DEG C
Material heavy constituent.
By Raw material recombination point, the mixing of heavy distillate, catalyst, vulcanizing agent, stir under the conditions of 80 DEG C.It is used to urge
Agent is 100~300 μm of catalyst with base of molybdenum, and molybdenum oxide percentage ratio is 2wt%, and catalyst is with the mass ratio of Raw material recombination point
3:1000.Vulcanizing agent used is Carbon bisulfide, and it is 2wt% that Carbon bisulfide accounts for the percentage ratio of Raw material recombination point.The slurry oil for obtaining send
Enter and carry out in floating bed hydrocracking device hydrocracking reaction, reaction hydrogen partial pressure is 16MPa, reaction temperature is 440 DEG C, hydrogen
Oil volume ratio is 1200, and reaction velocity is 1.5h-1, by centrifugation, filtration treatment after product gas-liquid separation, removing wherein institute
The particle diameter for containing is more than 25 μm of solid impurity, obtains generating oil.
Oil and the mixing of raw material light component will be generated, into fixed bed hydrogenation refining plant, Hydrobon catalyst is consisted of
Nickel oxide 1wt%, tungsten oxide 15wt%, phosphorous oxide 0.5wt%, balance of γ-Al2O3, reaction hydrogen partial pressure is 16MPa, is reacted
Temperature is 350 DEG C, and hydrogen to oil volume ratio is 1400, and reaction velocity is 0.5h-1.Hydrotreated product enters solid after three phase separation
Fixed bed hydrocracking unit, hydrocracking catalyst consists of nickel oxide 5wt%, molybdenum oxide 20wt%, phosphorous oxide 3wt%, remaining
Measure as carrier, molecular sieve content is 10wt% in carrier, reaction hydrogen partial pressure is 10MPa, and reaction temperature is 370 DEG C, hydrogen oil body
Than being 800, reaction velocity is 1.5h to product-1.Isocrackate obtains gasoline fraction, diesel oil and evaporates after gas-liquid separation, fractional distillation
Divide and heavy distillate.
The yield of gasoline obtained in the present embodiment 1 is 31%, and diesel yield is 53%, and heavy end oil yield is 16%,
Coal tar lighting effect is more apparent.
Embodiment 2 adopts raw oil same as Example 1, cuts>350 DEG C of fractions are that Raw material recombination point enters suspension bed
Hydrocracking unit, used catalyst molybdenum oxide percentage ratio is 0.5wt%, and catalyst is 5 with the mass ratio of Raw material recombination point:
1000, reaction condition is hydrogen partial pressure 16MPa, 420 DEG C of temperature, hydrogen to oil volume ratio 1400, reaction velocity 0.5h-1.Fixed bed adds
Hydrogen catalyst for refining consists of nickel oxide 3wt%, tungsten oxide 25wt%, phosphorous oxide 2wt%, balance of γ-Al2O3, react hydrogen
Partial pressure is 14MPa, and reaction temperature is 370 DEG C, and hydrogen to oil volume ratio is 800, and reaction velocity is 1.2h-1.Fixed bed hydrogenation cracking is urged
Agent consists of nickel oxide 3wt%, molybdenum oxide 16wt%, phosphorous oxide 2wt%, balance of carrier, and molecular sieve content is in carrier
18wt%, reaction hydrogen partial pressure be 12MPa, 410 DEG C of reaction temperature, hydrogen to oil volume ratio is 1400, and reaction velocity is 1.0h-1。
The yield of gasoline obtained in the present embodiment 2 is 33%, and diesel yield is 51%, heavy end oil yield 16%, coal
Tar lighting effect is more apparent.
Embodiment 3 adopts raw oil same as Example 1, cuts>350 DEG C of fractions are that Raw material recombination point enters suspension bed
Hydrocracking unit, used catalyst molybdenum oxide percentage ratio is 1.5wt%, and catalyst is 3 with the mass ratio of Raw material recombination point:
1000, reaction condition is hydrogen partial pressure 10MPa, 400 DEG C of temperature, hydrogen to oil volume ratio 600, reaction velocity 1.0h-1.Fixed bed hydrogenation
Catalyst for refining consists of nickel oxide 5wt%, tungsten oxide 30wt%, phosphorous oxide 3wt%, balance of γ-Al2O3, reactive hydrogen edema caused by disorder of QI
Press as 10MPa, reaction temperature is 340 DEG C, and hydrogen to oil volume ratio is 1200, and reaction velocity is 1.0h-1.Fixed bed hydrogenation cracking catalysis
Agent consists of nickel oxide 1wt%, molybdenum oxide 10wt%, phosphorous oxide 0.5wt%, balance of carrier, and molecular sieve content is in carrier
25wt%, reaction hydrogen partial pressure be 14MPa, 380 DEG C of reaction temperature, hydrogen to oil volume ratio is 800, and reaction velocity is 0.5h-1。
The yield of gasoline obtained in the present embodiment 3 is 34%, and diesel yield is 54%, heavy end oil yield 12%, coal
Tar lighting effect is more apparent.
Comparative example 1 adopts coal tar raw material same as Example 3, catalyst and technological parameter.Wherein, heavy distillate
Outer row, in not being recycled to floating bed hydrocracking device, the yield of gasoline of gained is 33%, and diesel yield is 50%, and heavy evaporates
Oil yield is divided to be 17%.
That is, the lighting of the achievable full fraction of coal tar of the present invention.
Finally it should be noted that：Obviously, above-described embodiment is only intended to clearly illustrate example of the present invention, and and
The non-restriction to embodiment.For those of ordinary skill in the field, can also do on the basis of the above description
Go out the change or variation of other multi-forms.There is no need to be exhaustive to all of embodiment.And thus drawn
Obvious change that Shen goes out or among changing still in protection scope of the present invention.
Claims (10)
1. a kind of full fraction of coal tar lighting system, including fractionating device (2), fixed bed hydrogenation refining plant, three phase separation
Device, fixed bed hydrogenation cracking unit, gas-liquid separation device, fractionating device (7), mixing arrangement, it is characterised in that
The fractionating device (2) is with coal tar oil-in, raw material light fraction outlet, Raw material recombination sub-export；
The fixed bed hydrogenation refining plant have raw material light component entrance, generate oil-in, the raw material light component entrance with
The raw material light fraction outlet connection of the fractionating device (2)；
Wherein, the fractionating device (2), fixed bed hydrogenation refining plant, three-phase separating device, fixed bed hydrogenation cracking unit,
Gas-liquid separation device, fractionating device (7) are sequentially connected；
The fractionating device (7) exports with gasoline fraction, diesel oil distillate is exported, heavy end oil export；
The mixing arrangement has Raw material recombination subentry, heavy end oil-in, catalyst inlet, vulcanizing agent entrance, slurry oil
Outlet, the Raw material recombination subentry is connected with the Raw material recombination sub-export of the fractionating device (2), and the heavy distillate enters
Mouth is connected with the heavy end oil export of the fractionating device (7).
2. system according to claim 1, it is characterised in that the system also include floating bed hydrocracking device, point
From device；
The floating bed hydrocracking device has slurry oil entrance, isocrackate outlet, and the slurry oil entrance is mixed with described
Attach together the slurry oil outlet connection put；
The segregation apparatuss have isocrackate entrance, generate oil export, solid impurity outlet, the isocrackate
Entrance is connected with the isocrackate outlet of the floating bed hydrocracking device, described to generate oil export and the fixed bed
The generation oil-in connection of hydro-refining unit.
3. the method that the system described in a kind of one of utilization claim 1-2 carries out full fraction of coal tar lighting, its feature exists
In comprising the steps：
Step A, by coal tar fractional distillation is carried out, and cut point T Raw material recombination point derived above obtains raw material below cut point T
Light component；
Step B, the raw material light component is sent into and carry out in the fixed bed hydrogenation refining plant hydrofining reaction, and reaction is produced
Thing carries out three phase separation, obtains gas phase, oil phase, water phase, and the oil phase is hydrogenated with the fixed bed hydrogenation cracking unit
Cracking reaction, product carries out successively gas-liquid separation, fractional distillation, obtains gasoline fraction, diesel oil distillate, heavy distillate, described
Heavy distillate is sent in the mixing arrangement via the heavy end oil-in.
4. method according to claim 3, it is characterised in that also including step：The Raw material recombination that step A is obtained
Divide, catalyst, vulcanizing agent are also fed in the mixing arrangement, are mixed to get slurry oil, the slurry oil splits in the floating bed hydrogenation
Makeup carries out hydrocracking reaction in putting, product obtains generating oil, solid impurity after segregation apparatuss process, described
Generate oil to send in the fixed bed hydrogenation refining plant via the generation oil-in.
5. method according to claim 3, it is characterised in that the T is 350~370 DEG C.
6. method according to claim 3, it is characterised in that the hydrogenation that the hydrofining reaction in step B is adopted
Catalyst for refining is consisted of：1wt%~5wt% nickel oxide, 15wt%~30wt% tungsten oxides, 0.5wt%~3wt% oxidations
Phosphorus, 62wt%~83.5wt% γ-Al2O3。
7. method according to claim 3, it is characterised in that the reaction temperature of the hydrofining reaction in step B
For 340~370 DEG C, hydrogen partial pressure is 10~16MPa.
8. method according to claim 3, it is characterised in that the hydrogenation that the hydrocracking reaction in step B is adopted
Cracking catalyst is consisted of：1wt%~5wt% nickel oxide, 10wt%~20wt% molybdenum oxides, 0.5wt%~5wt% oxidations
Phosphorus, 70wt%~88.5wt% carriers；
The carrier is Y type molecular sieve and γ-Al2O3Mixture, wherein, the Y type molecular sieve accounts for the percentage ratio of the carrier
For 10wt%~25wt%.
9. method according to claim 3, it is characterised in that the reaction temperature of the hydrocracking reaction in step B
For 370~410 DEG C, hydrogen partial pressure is 10~16MPa.
10. method according to claim 4, it is characterised in that the catalyst is microspheroidal loaded catalyst, described
Microspheroidal loaded catalyst particle diameter is 100~300 μm；
The reaction temperature of the hydrocracking reaction is 400~440 DEG C, and hydrogen partial pressure is 10~16MPa.
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| EP3567090A1 (en) * | 2018-05-11 | 2019-11-13 | Inner Mongolia Shengyuan Technology Co., Ltd. | Combined hydrogenation process method for producing high-quality fuel by medium-low-temperature coal tar |
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