CN110396427A - A kind of processing technology of full fraction coal tar - Google Patents
A kind of processing technology of full fraction coal tar Download PDFInfo
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- CN110396427A CN110396427A CN201810378810.9A CN201810378810A CN110396427A CN 110396427 A CN110396427 A CN 110396427A CN 201810378810 A CN201810378810 A CN 201810378810A CN 110396427 A CN110396427 A CN 110396427A
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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
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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
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/70—Catalyst aspects
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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
- C10G2400/00—Products obtained by processes covered by groups C10G9/00 - C10G69/14
- C10G2400/04—Diesel oil
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- Oil, Petroleum & Natural Gas (AREA)
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- General Chemical & Material Sciences (AREA)
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- Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
Abstract
The invention discloses a kind of processing technologys of full fraction coal tar.The processing technology is first fractionated full fraction coal tar, obtains coal tar at different levels；Then heavy coal tar is carried out adding hydrogen and separation, obtains light-end products and heavy product, light-end products separates again, collects gas and liquid；Light tar and gas are carried out to add hydrogen, collect hydrogenation products；Heavy product is fractionated, wax oil is collected；Centering matter coal tar, liquid, hydrogenation products and wax oil carry out plus hydrogen, collects hydrogenation products；Finally hydrogenation products are fractionated, find that this mode can effectively avoid light tar and light-end products overcracking for the first time, and by adding hydrogen that it is made sufficiently to be changed into light-end products, simultaneously deepen also heavy coal tar cracking degree, so that it is converted into light-end products, finally hydrogenation products are fractionated, the naphtha and diesel oil of high yield can be obtained, after tested, the total recovery of naphtha and diesel oil is greater than 90%.
Description
Technical field
The invention belongs to technical field of coal chemical industry, and in particular to a kind of processing technology of full fraction coal tar.
Background technique
Coal tar is coke oven byproduct, is a kind of complex mixture being made of hydrocarbon, wherein containing there are many tools
There is the rare type of recovery value, is the precious resources that petrochemical industry is difficult to obtain.But at the same time, wherein also containing a large amount of
Oxygenatedchemicals and sulphur, nitrogen and metal impurities and organic impurities etc., for example, 10 μm of sizes iron filings and oxide powder,
0.5 μm of partial size of high temperature pyrolytic polymer.These impurity undoubtedly increase the difficulty that coal tar processing utilizes.
For this purpose, the utilization technique of coal tar is studied extensively by researcher, to achieve the purpose that make full use of coal tar.
In numerous coal tar processings, 103215070 A of Chinese patent literature CN discloses a kind of by producing diesel by utilizing coal tar
Full fraction of coal tar is first sent into vacuum fractionation tower, is cut into light component coal tar and heavy constituent coal tar by method；
Enter paste state bed reactor after again mixing heavy constituent coal tar and hydrogen, is carried out under the action of slurry bed catalyst plus hydrogen is anti-
It answers；Then, solid bed reactor, In will be sent into after mixing with light component coal tar by gained effluent after paste state bed reactor reacts
Hydrogenation reaction occurs under the action of fixed bed catalyst；Finally, gained effluent passes through gas-liquid after fixed bed reactors are reacted
Separation, liquids flow into fractionating column and are further divided, and are cut into diesel oil distillate therein.
In above-mentioned technology, coal tar is successively once fractionated, slurry bed hydroprocessing, fixed bed hydrogenation, gas-liquid separation and
Secondary fractionation, obtained yield reach 55.12% diesel oil, and the processing for realizing coal tar recycles.But unluckily, skill
Wax oil yield reaches 34.23% in art, compares naphtha and diesel oil, and wax oil is using limited, and impurity is more, is not easy to apply.
Therefore how wax oil yield is reduced in coal tar processing, and improve naphtha and diesel yield is this field urgent need to resolve
A technical problem.
Summary of the invention
For this purpose, to be solved by this invention is that wax oil high income, naphtha and diesel oil are inclined in existing coal tar processing
Low defect, and then a kind of processing technology for the full fraction coal tar that wax oil yield is low, naphtha and diesel yield are high is provided.
In order to solve the above technical problems, The technical solution adopted by the invention is as follows:
The processing technology of full fraction coal tar provided by the invention, includes the following steps:
1) first time fractionation is carried out to full fraction coal tar, obtains light tar, middle matter coal tar and heavy coal tar；
2) the heavy coal tar is successively carried out for the first time plus hydrogen is separated with first time, obtained light-end products and heavy produces
Product, the light-end products carry out second and separate, and collect gas and liquid；
3) second plus hydrogen are carried out to the light tar and the gas, collects second of hydrogenation products；
4) second is carried out to the heavy product to be fractionated, collect wax oil；
5) third time plus hydrogen are carried out to the middle matter coal tar, liquid, second of hydrogenation products and wax oil, collects third time
Hydrogenation products；
6) third time fractionation is carried out to the third time hydrogenation products, collects naphtha and diesel oil.
Further, in step 1), the pressure of the first time fractionation is normal pressure, and temperature is 250-380 DEG C.
Further, in step 2), the first time adds the reaction pressure of hydrogen to be 18-25Mpa, reaction temperature 380-
460℃。
Further, in step 2), the first time adds the air speed of hydrogen to be 0.1-0.5h-1, hydrogen to oil volume ratio is (800-
1500): 1；And/or
The first time adds hydrogen hydrogenation catalyst used therein to be suspension bed hydrogenation catalyst, with total matter of the heavy coal tar
Meter, the first time add the additive amount of hydrogen hydrogenation catalyst used therein to be 0.5wt%-2wt%.Preferably, the suspension bed adds
Hydrogen catalyst is amorphous FeOOH, magnetic iron oxide, Alpha-hydroxy iron oxide.
Further, in step 2), the state modulator of the first time separation are as follows: 370-440 DEG C of temperature, pressure 18-
24Mpa。
Further, in step 2), the state modulator of second of separation are as follows: 250-350 DEG C of temperature, pressure 18-
24Mpa。
Further, in step 3), the reaction pressure for adding hydrogen for the second time is 18-23Mpa, reaction temperature 250-
350℃。
Further, in step 3), the air speed for adding hydrogen for the second time is 0.5-1h-1, hydrogen to oil volume ratio is (500-
1500): 1；And/or
It is described that hydrogen hydrogenation catalyst used therein is added to be fixed bed hydrogenation catalyst for the second time.The fixed bed hydrogenation catalyst is
It is made of the active constituent of carrier and load thereon, the load capacity of the active constituent is 5-15wt%, and the carrier is activity
Charcoal, molecular sieve or aluminium oxide；The active constituent is at least one of nickel oxide, molybdenum oxide, tungsten oxide.
Further, in step 4), second of fractionation is vacuum distillation, and the pressure of second of fractionation is 1-
5kpa (a), temperature are 300-400 DEG C.The isolated solid slag product of vacuum distillation tower tower bottom.
Further, in step 5), the third time adds the reaction pressure of hydrogen to be 18-22Mpa, reaction temperature 360-
420℃。
Further, in step 5), the third time adds the air speed of hydrogen to be 0.5-1h-1, hydrogen to oil volume ratio is (500-
1500): 1；And/or
The third time adds hydrogen hydrogenation catalyst used therein to be the molecular sieve catalyst for loading tungsten nickel, load capacity 15-
28wt%.
Further, in step 5), the pressure of the third time fractionation is 0.8-1.2Mpa, and temperature is 300-350 DEG C.
The wax oil is unsaturated wax oil.
It further include that the third time hydrogenation products are carried out before the third time hydrogenation products carry out third time fractionation
Gas-liquid separation, and the step of gas being separated to and the heavy coal tar progress first time are added into hydrogen, it is isolated
Liquid carries out the third time fractionation.
Compared with prior art, the invention has the following beneficial effects:
1) processing technology of full fraction coal tar provided by the present invention first divide for the first time to full fraction coal tar
It evaporates, obtains light tar, middle matter coal tar and heavy coal tar；Then the heavy coal tar is successively carried out adding for the first time
Hydrogen and for the first time separation obtain light-end products and heavy product, and the light-end products carries out second and separates, and collect gas and liquid
Body；Second plus hydrogen are carried out to the light tar and the gas, collect second of hydrogenation products；To the heavy product
It carries out second to be fractionated, collects wax oil；Third time is carried out to the middle matter coal tar, liquid, second of hydrogenation products and wax oil
Add hydrogen, collects third time hydrogenation products；Third time fractionation finally is carried out to the third time hydrogenation products, collects naphtha and bavin
Oil finds that this mode can effectively avoid light tar and light-end products overcracking for the first time, and is made by second plus hydrogen
It is sufficiently changed into light-end products, while also deepens heavy coal tar cracking degree, farthest it is made to be converted into lightweight
Oil product finally carries out third time fractionation to the third time hydrogenation products, the naphtha and diesel oil of high yield can be obtained, through surveying
The total recovery of examination, naphtha and diesel oil is greater than 90%；
2) processing technology of full fraction coal tar provided by the present invention is combined using multistage technology and is carried out, and further
Limit each section process raw material, control parameter and catalyst etc., keep its reasonably combined, not only solve because of the high institute of coal tar solid content
Short problem of the caused device cycle of operation, and catalyst activity can be given full play to, improve light oil (such as naphtha and bavin
Oil) yield and guarantee product quality.
Detailed description of the invention
It, below will be to specific in order to illustrate more clearly of the specific embodiment of the invention or technical solution in the prior art
Embodiment or attached drawing needed to be used in the description of the prior art be briefly described, it should be apparent that, it is described below
Attached drawing is some embodiments of the present invention, for those of ordinary skill in the art, before not making the creative labor
It puts, is also possible to obtain other drawings based on these drawings.
Fig. 1 is the used device flow chart of the processing technology of full fraction coal tar in the embodiment of the present invention；
Appended drawing reference is as follows:
The full fraction coal tar fractional distillation tower of 1-；2- floating bed hydrogenation reactor；3- product separator；4- gas-liquid separation dress
It sets；5- fixed bed hydrogenation reactor；6- vacuum distillation tower；7- hydrocracking reactor；8- gas-liquid separation device；The fractionation of 9- product
Tower；10- recycle gas compressor.
Specific embodiment
Technical solution of the present invention is clearly and completely described below, it is clear that described embodiment is the present invention
A part of the embodiment, instead of all the embodiments.Based on the embodiments of the present invention, those of ordinary skill in the art are not having
Every other embodiment obtained under the premise of creative work is made, shall fall within the protection scope of the present invention.
Embodiment 1
The processing technology for present embodiments providing a kind of full fraction coal tar, as shown in Figure 1, including the following steps:
1) full fraction coal tar is passed through in full fraction coal tar fractional distillation tower 1, and to full fraction coal at normal pressure, 265 DEG C
Tar carries out first time fractionation, obtains the middle matter coal tar that the light tar, boiling range that boiling range is 60-180 DEG C are 180-230 DEG C
The heavy coal tar for being 230-800 DEG C with boiling range；
2) the heavy coal tar is passed through in floating bed hydrogenation reactor 2, and in the reaction pressure of 20Mpa, 410 DEG C
Reaction temperature, 0.3h-1Air speed and 1300:1 hydrogen to oil volume ratio under, the heavy coal tar is successively carried out for the first time plus
Hydrogen, hydrogenation catalyst are powdered amorphous FeOOH, additive amount 1.5wt%；And the product after hydrogen will be added to be passed through production
It is separated in object separator 3, separation parameter is as follows: 410 DEG C of temperature, pressure 20MPa, obtaining light-end products and heavy produces
Product, the light-end products are sent into knockout drum 4 after being cooled to 220 DEG C, are carried out second and are separated, the parameter of second of separation
Control are as follows: 300 DEG C of temperature, pressure 22Mpa, collect the gas and liquid for being rich in hydrogen；
3) light tar and the gas rich in hydrogen are passed through in fixed bed hydrogenation reactor 5, and in
The reaction pressure of 20Mpa, 260 DEG C of reaction temperature, 0.7h-1Air speed and 700:1 hydrogen to oil volume ratio under, second is carried out to it
Secondary plus hydrogen, hydrogenation catalyst are the nickel oxide being carried on molecular sieve, and load capacity 10wt%, is collected second plus hydrogen produces
Object；
4) heavy product to be sent into vacuum distillation tower 6 and is separated, temperature is 320 DEG C, and pressure is 3kpa (a),
Obtain side line unsaturation wax oil product and tower bottom solid slag product；
5) enter after mixing the middle matter coal tar, liquid, unsaturated wax oil product and second of hydrogenation products and add
In hydrogen cracker 7, and in the reaction pressure of 20Mpa, 380 DEG C of reaction temperature, 0.7h-1Air speed and 800:1 hydrogen oil
Under volume ratio, third time plus hydrogen are carried out to it, hydrogenation catalyst is the molecular sieve catalyst for loading tungsten nickel, and load capacity is
21wt% collects third time hydrogenation products；
6) the third time hydrogenation products are passed through in gas-liquid separation device 8, isolated gas and liquid, gas is through following
10 reuse of ring air compressor is carried out into floating bed hydrogenation reactor 2 for the first time plus hydrogen, liquid enter in product fractionating column 9, and
Third time fractionation is carried out at 1.0Mpa, 320 DEG C, collects naphtha and diesel oil.
Embodiment 2
The processing technology for present embodiments providing a kind of full fraction coal tar, includes the following steps:
1) full fraction coal tar is passed through in full fraction coal tar fractional distillation tower 1, and to full fraction coal at normal pressure, 250 DEG C
Tar carries out first time fractionation, obtains the middle matter coal tar that the light tar, boiling range that boiling range is 60-180 DEG C are 180-230 DEG C
The heavy coal tar for being 230-800 DEG C with boiling range；
2) the heavy coal tar is passed through in floating bed hydrogenation reactor 2, and in the reaction pressure of 18Mpa, 450 DEG C
Reaction temperature, 0.1h-1Air speed and 1500:1 hydrogen to oil volume ratio under, the heavy coal tar is successively carried out for the first time plus
Hydrogen, hydrogenation catalyst are Magnetic powder iron oxide, additive amount 2wt%；And the product after hydrogen will be added to be passed through product separation dress
Set in 3 and separated, separation parameter is as follows: 370 DEG C of temperature, pressure 22Mpa obtains light-end products and heavy product；It is described light
Matter product is sent into knockout drum 4 after being cooled to 200 DEG C, is carried out second and is separated, the state modulator of second of separation are as follows: temperature
350 DEG C, pressure 18Mpa of degree collects the gas and liquid for being rich in hydrogen；
3) light tar and the gas rich in hydrogen are passed through in fixed bed hydrogenation reactor 5, and in
The reaction pressure of 18Mpa, 280 DEG C of reaction temperature, 0.5h-1Air speed and 1000:1 hydrogen to oil volume ratio under, is carried out to it
Secondary plus hydrogen, hydrogenation catalyst are the nickel oxide and molybdenum oxide being carried on active carbon, and load capacity 5wt% collects second
Secondary hydrogenation products；
4) heavy product to be sent into vacuum distillation tower 6 and is separated, temperature is 300 DEG C, and pressure is 5kpa (a),
Obtain side line unsaturation wax oil product and tower bottom solid slag product；
5) enter after mixing the middle matter coal tar, liquid, unsaturated wax oil product and second of hydrogenation products and add
In hydrogen cracker 7, and in the reaction pressure of 22Mpa, 360 DEG C of reaction temperature, 1h-1Air speed and 500:1 hydrogen oil body
Under product ratio, third time plus hydrogen are carried out to it, hydrogenation catalyst is the molecular sieve catalyst for loading tungsten nickel, and load capacity is
28wt% collects third time hydrogenation products；
6) the third time hydrogenation products are passed through in product fractionation tower 6, and carry out third time at 0.8Mpa, 350 DEG C
Naphtha and diesel oil are collected in fractionation.
Embodiment 3
The processing technology for present embodiments providing a kind of full fraction coal tar, includes the following steps:
1) full fraction coal tar is passed through in full fraction coal tar fractional distillation tower 1, and to full fraction coal at normal pressure, 280 DEG C
Tar carries out first time fractionation, obtains the middle matter coal tar that the light tar, boiling range that boiling range is 60-180 DEG C are 180-230 DEG C
The heavy coal tar for being 230-800 DEG C with boiling range；
2) the heavy coal tar is passed through in floating bed hydrogenation reactor 2, and in the reaction pressure of 22Mpa, 380 DEG C
Reaction temperature, 0.5h-1Air speed and 1000:1 hydrogen to oil volume ratio under, the heavy coal tar is successively carried out for the first time plus
Hydrogen, hydrogenation catalyst are powdered Alpha-hydroxy iron oxide, additive amount 0.5wt%；And the product after hydrogen will be added to be passed through product point
From being separated in device 3, separation parameter is as follows: 440 DEG C of temperature, pressure 18Mpa obtains light-end products and heavy product；Institute
It states and is sent into knockout drum 4 after light-end products is cooled to 240 DEG C, carry out second and separate, the state modulator of second of separation
Are as follows: 250 DEG C of temperature, pressure 24Mpa, collect the gas and liquid for being rich in hydrogen；
3) light tar and the gas rich in hydrogen are passed through in fixed bed hydrogenation reactor 5, and in
The reaction pressure of 22Mpa, 250 DEG C of reaction temperature, 1h-1Air speed and 500:1 hydrogen to oil volume ratio under, second is carried out to it
Add hydrogen, hydrogenation catalyst is the nickel oxide and tungsten oxide being carried on active carbon, and load capacity 15wt% collects second and adds
Hydrogen product；
4) heavy product to be sent into vacuum distillation tower 6 and is separated, temperature is 350 DEG C, and pressure is 1kpa (a),
Obtain side line unsaturation wax oil product and tower bottom solid slag product；
5) enter after mixing the middle matter coal tar, liquid, unsaturated wax oil product and second of hydrogenation products and add
In hydrogen cracker 7, and in the reaction pressure of 18Mpa, 390 DEG C of reaction temperature, 0.5h-1Air speed and 1000:1 hydrogen oil
Under volume ratio, third time plus hydrogen are carried out to it, hydrogenation catalyst is the molecular sieve catalyst for loading tungsten nickel, and load capacity is
15wt% collects third time hydrogenation products；
6) the third time hydrogenation products are passed through in product fractionation tower 6, and carry out to it at 1.2Mpa, 300 DEG C
It is fractionated three times, collects naphtha and diesel oil.
Embodiment 4
The processing technology for present embodiments providing a kind of full fraction coal tar, includes the following steps:
1) full fraction coal tar is passed through in full fraction coal tar fractional distillation tower 1, and to full fraction coal at normal pressure, 255 DEG C
Tar carries out first time fractionation, obtains the middle matter coal tar that the light tar, boiling range that boiling range is 60-180 DEG C are 180-230 DEG C
The heavy coal tar for being 230-800 DEG C with boiling range；
2) the heavy coal tar is passed through in floating bed hydrogenation reactor 2, and in the reaction pressure of 19Mpa, 400 DEG C
Reaction temperature, 0.2h-1Air speed and 1000:1 hydrogen to oil volume ratio under, the heavy coal tar is successively carried out for the first time plus
Hydrogen, hydrogenation catalyst are powdered amorphous FeOOH, additive amount 1.8wt%；And the product after hydrogen will be added to be passed through production
It is separated in object separator 3, separation parameter is as follows: 380 DEG C of temperature, pressure 21MPa, obtaining light-end products and heavy produces
Product；
The light-end products is sent into knockout drum 4 after being cooled to 210 DEG C, is carried out second and is separated, described to separate for the second time
State modulator are as follows: 210 DEG C of temperature, pressure 21Mpa, collect be rich in hydrogen gas and liquid；
3) light tar and the gas rich in hydrogen are passed through in fixed bed hydrogenation reactor 5, and in
The reaction pressure of 21Mpa, 260 DEG C of reaction temperature, 0.6h-1Air speed and 900:1 hydrogen to oil volume ratio under, second is carried out to it
Secondary plus hydrogen, hydrogenation catalyst are the tungsten oxide being carried on molecular sieve, and load capacity 8wt% collects second of hydrogenation products；
4) heavy product to be sent into vacuum distillation tower 6 and is separated, temperature is 340 DEG C, and pressure is 2kpa (a),
Obtain side line unsaturation wax oil product and tower bottom solid slag product；
5) enter after mixing the middle matter coal tar, liquid, unsaturated wax oil product and second of hydrogenation products and add
In hydrogen cracker 7, and in the reaction pressure of 19Mpa, 380 DEG C of reaction temperature, 0.6h-1Air speed and 900:1 hydrogen oil
Under volume ratio, third time plus hydrogen are carried out to it, hydrogenation catalyst is the molecular sieve catalyst for loading tungsten nickel, and load capacity is
18wt% collects third time hydrogenation products；
6) the third time hydrogenation products are passed through in product fractionation tower 6, and carry out to it at 1.1Mpa, 330 DEG C
It is fractionated three times, collects naphtha and diesel oil.
Embodiment 5
The processing technology for present embodiments providing a kind of full fraction coal tar, includes the following steps:
1) full fraction coal tar is passed through in full fraction coal tar fractional distillation tower 1, and to full fraction coal at normal pressure, 270 DEG C
Tar carries out first time fractionation, obtains the middle matter coal tar that the light tar, boiling range that boiling range is 60-180 DEG C are 180-230 DEG C
The heavy coal tar for being 230-800 DEG C with boiling range；
2) the heavy coal tar is passed through in floating bed hydrogenation reactor 2, and in the reaction pressure of 21Mpa, 390 DEG C
Reaction temperature, 0.4h-1Air speed and 1100:1 hydrogen to oil volume ratio under, the heavy coal tar is successively carried out for the first time plus
Hydrogen, hydrogenation catalyst are Magnetic powder iron oxide, additive amount 0.9wt%；And the product after hydrogen will be added to be passed through product separation
Separated in device 3, separation parameter is as follows: 430 DEG C of temperature, pressure 19MPa obtains light-end products and heavy product；
The light-end products is sent into knockout drum 4 after being cooled to 230 DEG C, is carried out second and is separated, described to separate for the second time
State modulator are as follows: 270 DEG C of temperature, pressure 19Mpa, collect be rich in hydrogen gas and liquid；
3) light tar and the gas rich in hydrogen are passed through in fixed bed hydrogenation reactor 5, and in
The reaction pressure of 19Mpa, 270 DEG C of reaction temperature, 0.7h-1Air speed and 800:1 hydrogen to oil volume ratio under, second is carried out to it
Secondary plus hydrogen, hydrogenation catalyst are the molybdenum oxide being carried on aluminium oxide, and load capacity 12wt%, is collected second plus hydrogen produces
Object；
4) heavy product to be sent into vacuum distillation tower 6 and is separated, temperature is 340 DEG C, and pressure is 2kpa (a),
Obtain side line unsaturation wax oil product and tower bottom solid slag product；
5) enter after mixing the middle matter coal tar, liquid, unsaturated wax oil product and second of hydrogenation products and add
In hydrogen cracker 7, and in the reaction pressure of 21Mpa, 370 DEG C of reaction temperature, 0.8h-1Air speed and 700:1 hydrogen oil
Under volume ratio, third time plus hydrogen are carried out to it, hydrogenation catalyst is the molecular sieve catalyst for loading tungsten nickel, and load capacity is
23wt% collects third time hydrogenation products；
6) the third time hydrogenation products are passed through in product fractionation tower 6, and carry out to it at 0.9Mpa, 320 DEG C
It is fractionated three times, collects naphtha and diesel oil.
Embodiment 6
The processing technology for present embodiments providing a kind of full fraction coal tar, as shown in Figure 1, including the following steps:
1) full fraction coal tar is passed through in full fraction coal tar fractional distillation tower 1, and to full fraction coal at normal pressure, 380 DEG C
Tar carries out first time fractionation, obtains the middle matter coal tar that the light tar, boiling range that boiling range is 60-180 DEG C are 180-230 DEG C
The heavy coal tar for being 230-800 DEG C with boiling range；
2) the heavy coal tar is passed through in floating bed hydrogenation reactor 2, and in the reaction pressure of 25Mpa, 460 DEG C
Reaction temperature, 0.3h-1Air speed and 800:1 hydrogen to oil volume ratio under, the heavy coal tar is successively carried out for the first time plus hydrogen,
Hydrogenation catalyst is powdered amorphous FeOOH, additive amount 1.5wt%；And the product after hydrogen will be added to be passed through product point
From being separated in device 3, separation parameter is as follows: 410 DEG C of temperature, pressure 24MPa obtains light-end products and heavy product, institute
It states and is sent into knockout drum 4 after light-end products is cooled to 220 DEG C, carry out second and separate, the state modulator of second of separation
Are as follows: 250 DEG C of temperature, pressure 24Mpa, collect the gas and liquid for being rich in hydrogen；
3) light tar and the gas rich in hydrogen are passed through in fixed bed hydrogenation reactor 5, and in
The reaction pressure of 23Mpa, 350 DEG C of reaction temperature, 0.7h-1Air speed and 1500:1 hydrogen to oil volume ratio under, is carried out to it
Secondary plus hydrogen, hydrogenation catalyst are the nickel oxide being carried on molecular sieve, and load capacity 10wt%, is collected second plus hydrogen produces
Object；
4) heavy product to be sent into vacuum distillation tower 6 and is separated, temperature is 400 DEG C, and pressure is 3kpa (a),
Obtain side line unsaturation wax oil product and tower bottom solid slag product；
5) enter after mixing the middle matter coal tar, liquid, unsaturated wax oil product and second of hydrogenation products and add
In hydrogen cracker 7, and in the reaction pressure of 20Mpa, 420 DEG C of reaction temperature, 0.7h-1Air speed and 1500:1 hydrogen oil
Under volume ratio, third time plus hydrogen are carried out to it, hydrogenation catalyst is the molecular sieve catalyst for loading tungsten nickel, and load capacity is
21wt% collects third time hydrogenation products；
6) the third time hydrogenation products are passed through in gas-liquid separation device 8, isolated gas and liquid, gas is through following
10 reuse of ring air compressor is carried out into floating bed hydrogenation reactor 2 for the first time plus hydrogen, liquid enter in product fractionating column 9, and
Third time fractionation is carried out at 1.0Mpa, 320 DEG C, collects naphtha and diesel oil.
Comparative example 1
This comparative example provides a kind of processing technology of full fraction coal tar, includes the following steps:
1) full fraction coal tar is passed through in full fraction coal tar fractional distillation tower, and to full fraction coal tar at normal pressure, 265 DEG C
Oil carries out first time fractionation, obtain middle matter coal tar that the light tar, boiling range that boiling range is 60-180 DEG C are 180-230 DEG C and
The heavy coal tar that boiling range is 230-800 DEG C；
2) the heavy coal tar is passed through in floating bed hydrogenation reactor 2, and in the reaction pressure of 20Mpa, 410 DEG C
Reaction temperature, 0.3h-1Air speed and 1300:1 hydrogen to oil volume ratio under, the heavy coal tar is successively carried out for the first time plus
Hydrogen, hydrogenation catalyst are powdered amorphous FeOOH, additive amount 1.5wt%；And the product after hydrogen will be added to be passed through production
It is separated in object separator 3, separation parameter is as follows: 410 DEG C of temperature, pressure 20MPa, obtaining light-end products and heavy produces
Product, the light-end products are sent into knockout drum 4 after being cooled to 220 DEG C, are carried out second and are separated, the parameter of second of separation
Control are as follows: 300 DEG C of temperature, pressure 22Mpa, collect the gas and liquid for being rich in hydrogen；
3) light tar and the gas rich in hydrogen are passed through in fixed bed hydrogenation reactor 5, and in
The reaction pressure of 20Mpa, 260 DEG C of reaction temperature, 0.7h-1Air speed and 700:1 hydrogen to oil volume ratio under, second is carried out to it
Secondary plus hydrogen, hydrogenation catalyst are the nickel oxide being carried on molecular sieve, and load capacity 10wt%, is collected second plus hydrogen produces
Object；
4) enter in hydrocracking reactor 7 after mixing the middle matter coal tar, liquid and second of hydrogenation products,
And in the reaction pressure of 20Mpa, 380 DEG C of reaction temperature, 0.7h-1Air speed and 800:1 hydrogen to oil volume ratio under, it is carried out
Third time plus hydrogen, hydrogenation catalyst are the molecular sieve catalyst for loading tungsten nickel, and load capacity 21wt% collects third time plus hydrogen
Product；
5) the third time hydrogenation products are passed through in product fractionation tower 6, and carry out third time at 1.0Mpa, 320 DEG C
Naphtha and diesel oil are collected in fractionation.
Comparative example 2
This comparative example provides a kind of processing technology of full fraction coal tar, includes the following steps:
1) full fraction coal tar is passed through in floating bed hydrogenation reactor 2, and in the reaction pressure of 18Mpa, 450 DEG C anti-
Answer temperature, 0.1h-1Air speed and 1500:1 hydrogen to oil volume ratio under, the heavy coal tar is successively carried out for the first time plus hydrogen,
Hydrogenation catalyst is Magnetic powder iron oxide, additive amount 2wt%；And the product after hydrogen will be added to be passed through product separator 3
In separated, separation parameter is as follows: 370 DEG C of temperature, pressure 22Mpa obtains light-end products and heavy product；The lightweight produces
Product are sent into knockout drum 4 after being cooled to 200 DEG C, are carried out second and are separated, the state modulator of second of separation are as follows: temperature
350 DEG C, pressure 18Mpa, collect the gas and liquid for being rich in hydrogen；
2) gas rich in hydrogen is passed through in fixed bed hydrogenation reactor 5, and in the reaction pressure of 18Mpa, 280
DEG C reaction temperature, 0.5h-1Air speed and 1000:1 hydrogen to oil volume ratio under, second plus hydrogen, hydrogenation catalyst are carried out to it
For the nickel oxide and molybdenum oxide being carried on active carbon, load capacity 5wt% collects second of hydrogenation products；
3) heavy product to be sent into vacuum distillation tower 6 and is separated, temperature is 300 DEG C, and pressure is 5kpa (a),
Obtain side line unsaturation wax oil product and tower bottom solid slag product；
4) enter hydrocracking reactor after mixing the liquid, unsaturated wax oil product and second of hydrogenation products
In 7, and in the reaction pressure of 22Mpa, 360 DEG C of reaction temperature, 1h-1Air speed and 500:1 hydrogen to oil volume ratio under, to its into
Row is for the third time plus hydrogen, hydrogenation catalyst are the molecular sieve catalyst for loading tungsten nickel, and load capacity 28wt% collects third time and adds
Hydrogen product；
5) the third time hydrogenation products are passed through in product fractionation tower 6, and carry out third time at 0.8Mpa, 350 DEG C
Naphtha and diesel oil are collected in fractionation.
Test example 1
Collected naphtha, diesel oil and wax oil yield after being fractionated for the third time in the various embodiments described above and comparative example are carried out
Measurement, corresponding measurement result are as shown in table 1 below:
Table 1, naphtha, diesel oil and wax oil yield
| Naphtha yield | Diesel yield | Wax oil yield | |
| Embodiment 1 | 26% | 69% | 0.8% |
| Embodiment 2 | 24% | 68% | 1.2% |
| Embodiment 3 | 25% | 67% | 1.3% |
| Embodiment 4 | 23% | 68.5% | 1.5% |
| Embodiment 5 | 23.8% | 67.5% | 1.4% |
| Embodiment 6 | 27% | 70% | 0.5% |
| Comparative example 1 | 10% | 40% | 25% |
| Comparative example 2 | 11% | 45% | 27% |
As known from Table 1: using the processing technology of full fraction coal tar of the invention, finally obtained naphtha and diesel oil are received
Rate is higher, and wax oil yield is lower, can effective processing and utilization coal tar.
Test example 2
The product index of naphtha collected by the embodiment of the present invention and diesel oil is tested, corresponding test result is such as
Shown in the following table 2 and 3:
The naphtha product index of table 2, the embodiment of the present invention
| Project | Unit | Quality index | Test method |
| Density | kg/m3(20℃) | 700~800 | GB/T1884 |
| Boiling range | ℃ | 45~205 | GB/T6536 |
| Sulfur content | mg/kg | ≤10 | SH/T0689 |
| Nitrogen content | mg/kg | ≤20 | SH/T0657 |
| Copper is rotten | ≤1 | GB/T5096 |
The product index of table 3, diesel oil of the embodiment of the present invention
It was found from table 2 and 3: the sulfur content of naphtha obtained by the present invention and diesel oil, nitrogen content and copper corruption are lower, product
Index is higher, and measures the naphtha arrived and diesel oil collected in comparative example 1 and comparative example 2, and sulfur content is all larger than 15, and nitrogen contains
Amount is all larger than 25, and copper corruption is all larger than 3.
Obviously, the above embodiments are merely examples for clarifying the description, and does not limit the embodiments.It is right
For those of ordinary skill in the art, can also make on the basis of the above description it is other it is various forms of variation or
It changes.There is no necessity and possibility to exhaust all the enbodiments.And it is extended from this it is obvious variation or
It changes still within the protection scope of the invention.
Claims (10)
1. a kind of processing technology of full fraction coal tar, includes the following steps:
1) first time fractionation is carried out to full fraction coal tar, obtains light tar, middle matter coal tar and heavy coal tar；
2) the heavy coal tar is successively carried out for the first time plus hydrogen is separated with first time, obtain light-end products and heavy product,
The light-end products carries out second and separates, and collects gas and liquid；
3) second plus hydrogen are carried out to the light tar and the gas, collects second of hydrogenation products；
4) second is carried out to the heavy product to be fractionated, collect wax oil；
5) third time plus hydrogen are carried out to the middle matter coal tar, liquid, second of hydrogenation products and wax oil, collects third time plus hydrogen
Product；
6) third time fractionation is carried out to the third time hydrogenation products, collects naphtha and diesel oil.
2. processing technology according to claim 1, which is characterized in that in step 1), the pressure of the first time fractionation is
Normal pressure, temperature are 250-380 DEG C.
3. processing technology according to claim 1 or 2, which is characterized in that in step 2), the first time adds the reaction of hydrogen
Pressure is 18-25Mpa, and reaction temperature is 380-460 DEG C.
4. processing technology according to any one of claim 1-3, which is characterized in that in step 2), the first time adds
The air speed of hydrogen is 0.1-0.5h-1, hydrogen to oil volume ratio is (800-1500): 1；And/or
The first time adds hydrogen hydrogenation catalyst used therein to be suspension bed hydrogenation catalyst, with the gross mass of the heavy coal tar
Meter, the first time add the additive amount of hydrogen hydrogenation catalyst used therein to be 0.5wt%-2wt%.
5. processing technology described in any one of -4 according to claim 1, which is characterized in that in step 2), the first time point
From state modulator are as follows: 370-440 DEG C of temperature, pressure 18-24Mpa；And/or
The state modulator of second of separation are as follows: 250-350 DEG C of temperature, pressure 18-24Mpa.
6. processing technology according to any one of claims 1-5, which is characterized in that described to add for the second time in step 3)
The reaction pressure of hydrogen is 18-23Mpa, and reaction temperature is 250-350 DEG C.
7. processing technology according to claim 1 to 6, which is characterized in that described to add for the second time in step 3)
The air speed of hydrogen is 0.5-1h-1, hydrogen to oil volume ratio is (500-1500): 1；And/or
It is described that hydrogen hydrogenation catalyst used therein is added to be fixed bed hydrogenation catalyst for the second time.
8. processing technology described in any one of -7 according to claim 1, which is characterized in that in step 4), described second point
The pressure evaporated is 1-5kpa, and temperature is 300-400 DEG C.
9. processing technology described in any one of -7 according to claim 1, which is characterized in that in step 5), the third time adds
The reaction pressure of hydrogen is 18-22Mpa, and reaction temperature is 360-420 DEG C；And/or
The third time adds the air speed of hydrogen to be 0.5-1h-1, hydrogen to oil volume ratio is (500-1500): 1；And/or
The third time adds hydrogen hydrogenation catalyst used therein to be the molecular sieve catalyst for loading tungsten nickel, load capacity 15-28wt%.
10. processing technology according to claim 1 to 9, which is characterized in that in step 5), the third time point
The pressure evaporated is 0.8-1.2Mpa, and temperature is 300-350 DEG C.
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| CN104004542A (en) * | 2014-06-13 | 2014-08-27 | 煤炭科学研究总院 | Method for preparing coal-based high aromatic potential content raw oil |
| CN104449837A (en) * | 2014-11-17 | 2015-03-25 | 华电重工股份有限公司 | Hydrogenation segregation treatment method of total fractions of coal tar |
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| CN101747925A (en) * | 2009-12-26 | 2010-06-23 | 何巨堂 | Method for coking heavy oil of coal tar |
| CN104004542A (en) * | 2014-06-13 | 2014-08-27 | 煤炭科学研究总院 | Method for preparing coal-based high aromatic potential content raw oil |
| CN104449837A (en) * | 2014-11-17 | 2015-03-25 | 华电重工股份有限公司 | Hydrogenation segregation treatment method of total fractions of coal tar |
| CN105018140A (en) * | 2015-07-14 | 2015-11-04 | 程志宇 | High-temperature coal tar washing oil fraction combination processing method |
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