CN104449836A - Trans-hydrocracking process of whole fractions of coal tar - Google Patents
Trans-hydrocracking process of whole fractions of coal tar Download PDFInfo
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- CN104449836A CN104449836A CN201410544912.5A CN201410544912A CN104449836A CN 104449836 A CN104449836 A CN 104449836A CN 201410544912 A CN201410544912 A CN 201410544912A CN 104449836 A CN104449836 A CN 104449836A
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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
-
- 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
-
- 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
- C10G2300/20—Characteristics of the feedstock or the products
- C10G2300/201—Impurities
- C10G2300/202—Heteroatoms content, i.e. S, N, O, P
-
- 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
- C10G2400/02—Gasoline
-
- 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
Abstract
The invention discloses a trans-hydrocracking process of whole fractions of coal tar. The trans-hydrocracking process comprises the following steps: pretreating whole fractions of coal tar, hydrofining and separating to obtain a cold high-fraction gas, a cold low-fraction gas, hot low-fraction oil and cold low-fraction oil, wherein the cold high-fraction gas is a hydrogen-rich gas which is used as a hydrogen source for a hydrogenation reaction together with new hydrogen after being recycled; fractionally distilling the cold low-fraction oil to obtain a fuel gas, a gasoline fraction, a diesel fraction and tail oil; mixing the tail oil with a part of hot low-fraction oil, hydrocracking, returning hydrocracking products to a hydrofining reactor, and carrying out a purification reaction on the hydrocracking products and the oil generated after pretreatment. The trans-hydrocracking process of the whole fractions of the coal tar, disclosed by the invention, is simple in technological process; hydrogenation equipment is good in operation stability; the utilization rate of the coal tar is high; the content of sulfur and nitrogen in gasoline and diesel oil obtained by hydrogenation is low and satisfies the quality standards of clean fuels.
Description
Technical field
The present invention relates to a kind of coal tar hydrogenation process, particularly a kind of is the processing method that raw material production cleans light-weight fuel oil with full fraction of coal tar, belongs to technical field of coal chemical industry.
Technical background
Along with the sustainable development of China's economy, the domestic demand to liquid fuel is growing, but China is the country of an oil starvation, weak breath, coal resources relative abundance, under existing situation, develop the method for producing available liquid fuel by solid fuels such as coals and there is positive realistic meaning.Coal tar is the by product that coal is formed in coking, gasification and retort process, current is raw material with coal tar, adopt suitable processing scheme, improve the stability of coal tar, reduce its foreign matter content, thus obtain low sulfur naphtha and the clean fuel oil of high added value, be a very effective approach preparing liquid fuel.
Because coal tar oil composition is extremely complicated, containing unsaturated hydro carbons and oxygen, sulphur, nitrogen compound and solid impurities such as a large amount of alkene, polycyclic aromatic hydrocarbonss, and colloid and asphalt content are also quite high, therefore in actual production process, the hydrotreating/hydrocracking method of usual employing realizes that the deoxidation of coal tar, desulfurization, denitrogenation and unsaturated hydrocarbons saturated etc. clean, lighting object, thus obtains petroleum naphtha and clean fuel oil.Such as, Chinese patent literature CN1676583A discloses hydrogenation of high temperature coal tar process in one, this technique comprises: middle coal-tar heavy oil is introduced process furnace and sends into hydrofining reactor after mixing with hydrogen, the generation oil of refining reaction device effluent after being separated enters separation column, isolate gasoline, diesel oil, lubricating oil and tail oil, tail oil then introduces cracking case, and it generates oil and enters separation column and generate together with oil with hydrofining and carry out fractionation.
Above-mentioned prior art is by adopting hydrofining-hydrocracking process, by further for hydrorefined tail oil cracking, although improve the utilization ratio of coal tar raw material to a certain extent, but still the defect existed is: prior art to carry out in the oil product that hydrofining-cracking process obtains, still containing more sulphur, making oil quality not up to standard to full fraction of coal tar.Therefore, how improving to overcome to the hydrogenation technique of coal tar the defect that prior art exists, is those skilled in the art's technical barriers urgently to be resolved hurrily.
Summary of the invention
The problem that exceeds standard of sulphur content in what the present invention solved is light ends that coal tar hydrogenation process of the prior art exists, and then provide that a kind of utilization ratio to coal tar is high, hydrogenation unit run stability is good and light ends meets the coal tar hydrogenation process of clean fuel standards.
The technical scheme that the present invention solves the problems of the technologies described above is:
The trans hydrocracking process of a kind of full fraction of coal tar, comprises the steps:
A (), under hydrogenation protecting agent existent condition, carries out weighted BMO spaces to full fraction of coal tar, obtain pre-treatment and generate oil;
B () generates oil to described pre-treatment and carries out hydrofining, obtain hydrotreated product;
C () is carried out thermal high separation to described hydrotreated product and is obtained thermal high gas phase and thermal high liquid phase; Again cold anticyclone separation is carried out to described thermal high gas phase and obtain cold high score gas and cold anticyclone liquid phase; Thermal low separation is carried out to described thermal high liquid phase and obtains thermal low gas phase and heat low point of oil; Carry out cold low to described thermal low gas phase and the mixture of described cold anticyclone liquid phase to be separated and to obtain cold low point of gas and cold low point of oil;
D () carries out fractionation to described cold low point of oil, cut out gasoline, tail oil and fuel gas that diesel oil, boiling point are greater than 370 DEG C;
E low for a described heat point of oily part and described tail oil are mixed to get mixing oil by (), hydrocracking reaction is carried out to described mixing oil, be cracking high score gas and cracking high score oil by the product separation of hydrocracking, together with after wherein said cracking high score oil and the described pre-treatment prepared in step (a) generate oily mixing, carry out hydrofining.
The part that low point of described heat is oily and described tail oil are made mixing oil and carry out hydrocracking reaction, and another part mixes with the described full fraction of coal tar in step (a) and carries out weighted BMO spaces.
The temperature of carrying out weighted BMO spaces in step (a) is 300 ~ 450 DEG C, and pressure is 18Mpa, and hydrogen to oil volume ratio is 800 ~ 1500: 1, and volume space velocity is 0.1 ~ 5.0h
-1.
The hydrogenation protecting agent used in step (a) is compound containing active metallic element or the aqueous solution, and described active metallic element is one or more in VB, VIB, group VIII metal element; In every gram of described hydrogenation protecting agent, the content of active metallic element is 50 ~ 200 μ g.
Carrying out hydrorefined temperature in step (b) is 330 ~ 390 DEG C, and pressure is 18Mpa, hydrogen to oil volume ratio 800 ~ 1500: 1, and volume space velocity is 0.5 ~ 5.0h
-1.
The Hydrobon catalyst used of hydrofining described in step (b) comprises the molybdenum oxide of 5 ~ 25wt%, the nickel oxide of 1 ~ 10wt%, surplus is silica support or alumina supporter, and the pore volume of described catalyst for refining is 0.20 ~ 0.50mL/g, specific surface area is 100 ~ 200m
2/ g.
In step (c), the working pressure carrying out described thermal high separation is 17.3MPa, service temperature is 310 DEG C; The working pressure carrying out described cold anticyclone separation is 17.2MPa, service temperature is 48 DEG C; The working pressure carrying out described thermal low separation is 2.0MPa, service temperature is 310 DEG C; The working pressure carrying out described cold low separation is 2.0MPa, service temperature is 45 DEG C.
Be separated the described cracking high score gas obtained and described thermal low gas phase and the mixture of described cold anticyclone liquid phase in step (e) jointly to carry out cold low and be separated and obtain cold low point of gas and cold low point of oil.
The pressure carrying out described hydrocracking in step (e) is 17MPa, hydrogen to oil volume ratio is 800 ~ 3000: 1, temperature is 260 ~ 340 DEG C, volume space velocity is 0.1 ~ 4.0h
-1.
When carrying out hydrocracking reaction in step (e); described mixing oil flows through cracking protective material bed, cracking pretreating agent bed and cracking catalyst bed successively; wherein said cracking protective material, cracking pretreating agent and cracking catalyst all with any one or a few in Mo, W, Co or Ni for active ingredient, with aluminum oxide and/or molecular sieve for carrier.Cracking protective material of the present invention, cracking pretreating agent and cracking catalyst are preferably the Catalyst For Single-stage Hydrocrackings such as FC-28, FC-14, ZHC-01 of Fu Yan institute development, the hydrocracking catalysts such as DHC39, DHC-8 of Uop Inc.'s exploitation.
Described cold high score gas is mixed the hydrogen source being used as hydrofining and the middle hydrocracking of step (e) in weighted BMO spaces, step (b) in step (a) with hydrogen.
The trans hydrogenation system of a kind of full fraction of coal tar, comprising:
Connect the pre-hydrogenation guard reactor and hydrofining reactor that arrange; The outlet of described pre-hydrogenation guard reactor is connected with the entrance of described hydrofining reactor by the feed(raw material)inlet pipe of described hydrofining reactor;
High pressure hot separator, is connected with the outlet of described hydrofining reactor and arranges;
Cold high pressure separator, is connected with the gaseous phase outlet of described high pressure hot separator and arranges;
Thermal low-pressure separators, is connected with the liquid-phase outlet of described high pressure hot separator and arranges;
Cold low separator, is connected with the liquid-phase outlet of described cold high pressure separator and the gaseous phase outlet of described thermal low-pressure separators and arranges;
Separation column, is connected with the liquid-phase outlet of described cold low separator and arranges;
Hydrocracking reactor, simultaneously exports to be connected with the liquid-phase outlet of described thermal low-pressure separators and the tail oil of described separation column and arranges;
Cracking high-pressure separator, is arranged with the outlet of described hydrocracking reactor;
The liquid-phase outlet of described cracking high-pressure separator is communicated with the feed(raw material)inlet pipe of described hydrofining reactor and arranges.
The liquid-phase outlet of described thermal low-pressure separators is communicated with the feed(raw material)inlet pipe of described pre-hydrogenation guard reactor simultaneously and arranges, and carries out hydrofining together with after being suitable for that the generation of the liquid phase of described cracking high-pressure separator and described pre-hydrogenation guard reactor is oily and mixing.
The gaseous phase outlet of described cracking high-pressure separator is connected with described cold low separator and arranges.
Be connected with circulating hydrogen compressor with the gaseous phase outlet of described cold high pressure separator, the pressurized gas of described circulating hydrogen compressor exports to be communicated with the hydrogen inlet of hydrocracking reactor with described pre-hydrogenation guard reactor, hydrofining reactor respectively and arranges.
In step (a) of the present invention; weighted BMO spaces reaction is carried out in single beds fixed-bed reactor; the top of this reactor is provided with cold hydrogen inlet; to control the temperature of beds; this beds is filled with hydrogenation protecting agent; there is demetalization reaction and hydrogenation of olefins presaturation reaction, prevent the alkene at high temperature blocking catalyst bed because of polymerization coking, affect the normal operation of device.The top of the hydrofining reactor that the hydrofining reaction of step (b) adopts is provided with cold hydrogen inlet, by regulating cold hydrogen the controlling of injecting quantity reaction bed temperature, prevents bed temperature runaway.In addition, the cracking catalyst that the present invention uses with aluminum oxide and/or molecular sieve for carrier, with any one or a few in Mo, W, Co or Ni for active ingredient, its reason is for the aromatic hydrocarbons in coal tar, it is active that its lighting needs cracking catalyst to have good open loop, but be not the lytic activity center increasing merely cracking catalyst in mode, but B, L acid site will be balanced, coordinate B acid to realize open loop, the cracking of aromatic hydrocarbons better to make L acid to the anchorage effect of conjugated system molecule.
Compared with coal tar hydrogenation process of the prior art, the advantage of the trans hydrocracking process of full fraction of coal tar of the present invention is:
(1) the trans hydrocracking process of full fraction of coal tar of the present invention, carry out hydrofining using the full cut of coal tar as raw material, the tail oil that refined products obtains through fractionation carries out hydrocracking further, isocrackate is directly in addition fractionation, but hydrofining process is carried out together with weighted BMO spaces product, to remove the S-contained substance existed in isocrackate further, thus the sulphur content effectively avoiding the mercaptan that in prior art, hydrocracking stage produces to cause cracking to generate in oil because having little time hydrocracking exceeds standard, directly oil is generated to this cracking and carry out fractionation, the problem of each light ends quality dissatisfaction can be caused.That is, the sulphur in the gasoline adopting the trans hydrocracking process of full fraction of coal tar of the present invention to obtain and diesel oil, nitrogen content are lower, all meet the quality standard of clean fuel.
Because heavy constituent in coal tar (> 370 DEG C) the i.e. content of tail oil is generally 50-60%, the present invention will occupy the tail oil hydrocracking over half of coal tar gross weight, and then be converted into light-end products, improve the economic worth of coal tar largely, thus improve adaptability and the production chains of coal tar raw material.And before above-mentioned hydrofining, the present invention also carries out weighted BMO spaces to coal tar raw material, makes the olefins hydrogenation in coal tar, prevent the alkene at high temperature blocking catalyst bed because of polymerization coking, thus the normal operation of assurance device; Simultaneously the present invention diluted coal tar raw material with the hot low point of oil of part before above-mentioned weighted BMO spaces, and its reason is to reduce the density of coal tar raw material, carbon residue and hydrogenation difficulty, can also control the temperature rise of beds.
(2) the trans hydrocracking process of full fraction of coal tar of the present invention, described hydrotreated product is separated through four separators such as high pressure hot separator, cold high pressure separator, thermal low-pressure separators and cold low separators, the hydrogen-rich gas obtained reclaims and then mixes the hydrogen source as hydrogenation reaction with new hydrogen, so can reduce the new hydrogen supply in whole system, reduce production cost.
Accompanying drawing explanation
Fig. 1 is the schema of the trans hydrocracking process of full fraction of coal tar of the present invention;
Wherein, Reference numeral is as follows:
1-boosting pump; 2-interchanger; The pre-hydrogenation guard reactor of 3-; 4-hydrofining reactor; 5-high pressure hot separator; 6-cold high pressure separator; 7-thermal low-pressure separators; 8-cold low separator; 9-separation column; 10-cracked charge interchanger; 11-hydrocracking reactor; 12-cracking high-pressure separator; 13-circulating hydrogen compressor.
Embodiment
Below in conjunction with specific embodiment, the trans hydrocracking process of full fraction of coal tar provided by the invention is described in detail.
Embodiment 1
Realize the trans hydrogenation system of full fraction of coal tar of the trans hydrocracking process of full fraction of coal tar in the present embodiment, comprising:
Connect the pre-hydrogenation guard reactor 3 and hydrofining reactor 4 that arrange;
High pressure hot separator 5, is connected with the outlet of described hydrofining reactor 4 and arranges;
Cold high pressure separator 6, is connected with the gaseous phase outlet of described high pressure hot separator 5 and arranges;
Thermal low-pressure separators 7, is connected with the liquid-phase outlet of described high pressure hot separator 5 and arranges;
Cold low separator 8, is connected with the liquid-phase outlet of described cold high pressure separator 6 and the gaseous phase outlet of described thermal low-pressure separators 7 and arranges;
Separation column 9, is connected with the liquid-phase outlet of described cold low separator 8 and arranges;
Hydrocracking reactor 11, simultaneously exports to be connected with the liquid-phase outlet of described thermal low-pressure separators 7 and the tail oil of described separation column 9 and arranges;
Cracking high-pressure separator 12, is arranged with the outlet of described hydrocracking reactor 11; The liquid-phase outlet of described cracking high-pressure separator 12 is communicated with the feed(raw material)inlet pipe of described hydrofining reactor 4 and arranges.
The trans hydrocracking process of full fraction of coal tar described in the present embodiment, as shown in Figure 1, comprises the steps:
A (), in pre-hydrogenation guard reactor 3, pressure is 18MPa, hydrogen to oil volume ratio is 1500: 1, temperature is 300 DEG C, volume space velocity is 2.5h
-1condition under, use Vanadium Pentoxide in FLAKES as hydrogenation protecting agent, weighted BMO spaces is carried out to full fraction of coal tar, obtain pre-treatment generate oil, the consumption of this hydrogenation protecting agent counts 50 μ g/g with v element;
B described pre-treatment is generated oil feeding hydrofining reactor 4 and carries out hydrofining by (), obtain hydrotreated product; Described hydrorefined condition is: pressure 18MPa, hydrogen to oil volume ratio 800: 1, temperature 390 DEG C, volume space velocity 0.5h
-1; The molybdenum oxide that the Hydrobon catalyst that described hydrofining uses is 25wt%, the nickel oxide of 1wt%, surplus is silica support, and the pore volume of this catalyst for refining be 0.20mL/g, specific surface area is 200m
2/ g;
C () utilizes high pressure hot separator 5 to carry out thermal high separation to described hydrotreated product and obtains thermal high gas phase and thermal high liquid phase; Recycling cold high pressure separator 6 carries out cold anticyclone separation to described thermal high gas phase and obtains cold high score gas and cold anticyclone liquid phase, utilizes thermal low-pressure separators 7 to carry out thermal low separation to described thermal high liquid phase and obtains thermal low gas phase and heat low point of oil; Utilize cold low separator 8 to carry out cold low to described thermal low gas phase and the mixture of described cold anticyclone liquid phase to be separated and to obtain cold low point of gas and cold low point of oil; Wherein, the working pressure that described thermal high is separated is 17.3MPa, service temperature is 310 DEG C; The working pressure carrying out described cold anticyclone separation is 17.2MPa, service temperature is 48 DEG C; The working pressure carrying out described thermal low separation is 2.0MPa, service temperature is 310 DEG C; The working pressure carrying out described cold low separation is 2.0MPa, service temperature is 45 DEG C;
D described cold low point of oil is sent into separation column 9 by (), carry out fractionation to described cold low point of oil, and cutting out gasoline, boiling point that boiling point is less than 150 DEG C is tail oil and the fuel gas that diesel oil, the boiling point of 150 ~ 370 DEG C is greater than 370 DEG C;
E low for a described heat point of oily part and described tail oil are made mixing oil and are sent into hydrocracking reactor 11 and carry out hydrocracking reaction by (), the condition of described hydrocracking is: pressure 17MPa, hydrogen to oil volume ratio 3000: 1, temperature 300 DEG C, volume space velocity 0.25h
-1, the DHC39 hydrocracking catalyst that the cracking catalyst that described hydrocracking uses is developed for Uop Inc.; Utilize cracking high-pressure separator 12 to be cracking high score gas and cracking high score oil by the product separation of hydrocracking, send into hydrofining reactor 4 again together with after wherein said cracking high score oil and the described pre-treatment prepared in step (a) generate oily mixing and carry out hydrofining.
Described in the present embodiment, the character of full fraction of coal tar is as shown in table 1, and the reaction conditions of the trans hydrocracking process of described full fraction of coal tar is as shown in table 2, the gasoline that fractionation obtains and bavin oil properties as shown in table 3.
Embodiment 2
Realize the trans hydrogenation system of full fraction of coal tar of the trans hydrocracking process of full fraction of coal tar in the present embodiment, comprising:
Be communicated with the boosting pump 1 and interchanger 2 that arrange;
Connect the pre-hydrogenation guard reactor 3 and hydrofining reactor 4 that arrange, the feed(raw material)inlet of described pre-hydrogenation guard reactor 3 is connected with the material outlet of described interchanger 2;
High pressure hot separator 5, is connected with the outlet of described hydrofining reactor 4 and arranges;
Cold high pressure separator 6, be connected with the gaseous phase outlet of described high pressure hot separator 5 and arrange, the gaseous phase outlet of described cold high pressure separator 6 is connected with circulating hydrogen compressor 13, and the pressurized gas of described circulating hydrogen compressor 13 exports to be communicated with the hydrogen inlet of hydrocracking reactor 11 with described pre-hydrogenation guard reactor 3, hydrofining reactor 4 respectively and arranges;
Thermal low-pressure separators 7, is connected with the liquid-phase outlet of described high pressure hot separator 5 and arranges, and the liquid-phase outlet of described thermal low-pressure separators 7 is communicated with the feed(raw material)inlet pipe of described pre-hydrogenation guard reactor 3 and arranges;
Cold low separator 8, is connected with the liquid-phase outlet of described cold high pressure separator 6 and the gaseous phase outlet of described thermal low-pressure separators 7 and arranges;
Separation column 9, is connected with the liquid-phase outlet of described cold low separator 8 and arranges;
Hydrocracking reactor 11, simultaneously exports to be connected with the liquid-phase outlet of described thermal low-pressure separators 7 and the tail oil of described separation column 9 and arranges;
Cracking high-pressure separator 12, is arranged with the outlet of described hydrocracking reactor 11; The liquid-phase outlet of described cracking high-pressure separator 12 is communicated with the feed(raw material)inlet pipe of described hydrofining reactor 4 and arranges; The gaseous phase outlet of described cracking high-pressure separator 12 is connected with described cold low separator 8 and arranges.
The trans hydrocracking process of full fraction of coal tar described in the present embodiment, as shown in Figure 1, comprises the steps:
(a) full fraction of coal tar through boosting pump 1 and interchanger 2 pressurize heat up after send into pre-hydrogenation guard reactor 3, pressure be 18MPa, hydrogen to oil volume ratio is 1150: 1, temperature is 450 DEG C, volume space velocity is 0.1h
-1condition under, use ammonium molybdate aqueous solution as hydrogenation protecting agent to through pressurization heat up after full fraction of coal tar carry out weighted BMO spaces, obtain pre-treatment generate oil, the consumption of this hydrogenation protecting agent counts 200 μ g/g with molybdenum element;
B described pre-treatment is generated oil feeding hydrofining reactor 4 and carries out hydrofining by (), obtain hydrotreated product; Described hydrorefined condition is: pressure 18MPa, hydrogen to oil volume ratio 1500: 1, temperature 360 DEG C, volume space velocity 5h
-1; The molybdenum oxide that the Hydrobon catalyst that described hydrofining uses is 5wt%, the nickel oxide of 5wt%, surplus is alumina supporter, and the pore volume of this catalyst for refining be 0.35mL/g, specific surface area is 150m
2/ g;
C () utilizes high pressure hot separator 5 to carry out thermal high separation to described hydrotreated product and obtains thermal high gas phase and thermal high liquid phase; Recycling cold high pressure separator 6 carries out cold anticyclone separation to described thermal high gas phase and obtains cold high score gas and cold anticyclone liquid phase, utilize thermal low-pressure separators 7 to carry out thermal low separation to described thermal high liquid phase and obtain thermal low gas phase and heat low point of oil, after wherein said cold high score gas mixes with hydrogen, can be used as the hydrogen source of hydrofining and the middle hydrocracking of step (e) in weighted BMO spaces, step (b) in step (a); Utilize cold low separator 8 to carry out cold low to described thermal low gas phase and the mixture of described cold anticyclone liquid phase to be separated and to obtain cold low point of gas and cold low point of oil; Wherein, the working pressure that described thermal high is separated is 17.3MPa, service temperature is 310 DEG C; The working pressure carrying out described cold anticyclone separation is 17.2MPa, service temperature is 48 DEG C; The working pressure carrying out described thermal low separation is 2.0MPa, service temperature is 310 DEG C; The working pressure carrying out described cold low separation is 2.0MPa, service temperature is 45 DEG C;
D described cold low point of oil is sent into separation column 9 and is carried out fractionation by (), cutting out gasoline, boiling point that boiling point is less than 150 DEG C is tail oil and the fuel gas that diesel oil, the boiling point of 150 ~ 370 DEG C is greater than 370 DEG C;
E low for a described heat point of oily part and described tail oil are made mixing oil and are sent into hydrocracking reactor 11 and carry out hydrocracking by (), in described hydrocracking reactor 11, described mixing oil flows through cracking protective material bed successively, cracking pretreating agent bed and cracking catalyst bed carry out hydrocracking reaction, wherein said cracking protective material is the FC-28 Catalyst For Single-stage Hydrocracking that Fu Yan institute develops, described cracking pretreating agent and cracking catalyst are respectively the DHC39 of Uop Inc.'s exploitation, DHC-8 hydrocracking catalyst, the condition of described hydrocracking is: pressure 17MPa, hydrogen to oil volume ratio 3000: 1, temperature 300 DEG C, volume space velocity 0.25h
-1, the product separation of hydrocracking is cracking high score gas and cracking high score oil by cracking high-pressure separator 12, wherein said cracking high score gas jointly carries out cold low with described thermal low gas phase with the mixture of described cold anticyclone liquid phase and is separated, and enters hydrofining reactor 4 and carry out hydrofining together with after described cracking high score oil and the described pre-treatment prepared in step (a) generate oily mixing, and the oily another part of low point of described heat mixes with the described full fraction of coal tar in step (a) and carries out weighted BMO spaces.
Described in the present embodiment, the character of full fraction of coal tar is as shown in table 1, and the reaction conditions of the trans hydrocracking process of described full fraction of coal tar is as shown in table 2, the gasoline that fractionation obtains and bavin oil properties as shown in table 3.
Embodiment 3
Realize the trans hydrogenation system of full fraction of coal tar of the trans hydrocracking process of full fraction of coal tar in the present embodiment, comprising:
Connect the pre-hydrogenation guard reactor 3 and hydrofining reactor 4 that arrange;
High pressure hot separator 5, is connected with the outlet of described hydrofining reactor 4 and arranges;
Cold high pressure separator 6, is connected with the gaseous phase outlet of described high pressure hot separator 5 and arranges;
Thermal low-pressure separators 7, is connected with the liquid-phase outlet of described high pressure hot separator 5 and arranges, and the liquid-phase outlet of described thermal low-pressure separators 7 is communicated with the feed(raw material)inlet pipe of described pre-hydrogenation guard reactor 3 and arranges;
Cold low separator 8, is connected with the liquid-phase outlet of described cold high pressure separator 6 and the gaseous phase outlet of described thermal low-pressure separators 7 and arranges;
Separation column 9, is connected with the liquid-phase outlet of described cold low separator 8 and arranges;
Hydrocracking reactor 11, simultaneously exports to be connected with the liquid-phase outlet of described thermal low-pressure separators 7 and the tail oil of described separation column 9 and arranges;
Cracking high-pressure separator 12, is arranged with the outlet of described hydrocracking reactor 11; The liquid-phase outlet of described cracking high-pressure separator 12 is communicated with the feed(raw material)inlet pipe of described hydrofining reactor 4 and arranges; The gaseous phase outlet of described cracking high-pressure separator 12 is connected with described cold low separator 8 and arranges.
The trans hydrocracking process of full fraction of coal tar described in the present embodiment, as shown in Figure 1, comprises the steps:
A full fraction of coal tar is sent into pre-hydrogenation guard reactor 3 by (), pressure be 18MPa, hydrogen to oil volume ratio is 800: 1, temperature is 375 DEG C, volume space velocity is 5h
-1condition under, use nickelous nitrate and Cobaltous diacetate jointly to carry out weighted BMO spaces as hydrogenation protecting agent to full fraction of coal tar, obtain pre-treatment and generate oil, the consumption of this hydrogenation protecting agent is counted 60 μ g/g with nickel element, is counted 40 μ g/g with cobalt element;
B described pre-treatment is generated oil feeding hydrofining reactor 4 and carries out hydrofining by (), obtain hydrotreated product; Described hydrorefined condition is: pressure 18MPa, hydrogen to oil volume ratio 1150: 1, temperature 330 DEG C, volume space velocity 2.75h
-1, described hydrofining Hydrobon catalyst used is the molybdenum oxide of 15wt%, the nickel oxide of 10wt%, and surplus is silica support, and the pore volume of this Hydrobon catalyst be 0.5mL/g, specific surface area is 100m
2/ g;
C () utilizes high pressure hot separator 5 to carry out thermal high separation to described hydrotreated product and obtains thermal high gas phase and thermal high liquid phase; Recycling cold high pressure separator 6 carries out cold anticyclone separation to described thermal high gas phase and obtains cold high score gas and cold anticyclone liquid phase, utilizes thermal low-pressure separators 7 to carry out thermal low separation to described thermal high liquid phase and obtains thermal low gas phase and heat low point of oil; Utilize cold low separator 8 to carry out cold low to described thermal low gas phase and the mixture of described cold anticyclone liquid phase to be separated and to obtain cold low point of gas and cold low point of oil; Wherein, the working pressure that described thermal high is separated is 17.3MPa, service temperature is 310 DEG C; The working pressure carrying out described cold anticyclone separation is 17.2MPa, service temperature is 48 DEG C; The working pressure carrying out described thermal low separation is 2.0MPa, service temperature is 310 DEG C; The working pressure carrying out described cold low separation is 2.0MPa, service temperature is 45 DEG C.
D described cold low point of oil is sent into separation column 9 by (), carry out fractionation to described cold low point of oil, and cutting out gasoline, boiling point that boiling point is less than 150 DEG C is tail oil and the fuel gas that diesel oil, the boiling point of 150 ~ 370 DEG C is greater than 370 DEG C;
E low for a described heat point of oily part and described tail oil are made mixing oil by (), described mixing oil is sent into hydrocracking reactor 11, in described hydrocracking reactor 11, mixing oil flows through cracking protective material bed successively, cracking pretreating agent bed and cracking catalyst bed carry out hydrocracking reaction, wherein said cracking protective material is the DHC-8 hydrocracking catalyst of Uop Inc.'s exploitation, described cracking pretreating agent is the ZHC-01 Catalyst For Single-stage Hydrocracking that Fu Yan institute develops, described cracking catalyst is the FC-14 Catalyst For Single-stage Hydrocracking that Fu Yan institute develops, the condition of described hydrocracking is: pressure 17MPa, hydrogen to oil volume ratio 1900: 1, temperature 340 DEG C, volume space velocity 4h
-1, cracking high-pressure separator 12 is utilized to be cracking high score gas and cracking high score oil by the product separation of hydrocracking, wherein said cracking high score gas jointly carries out cold low with described thermal low gas phase with the mixture of described cold anticyclone liquid phase and is separated, and enters hydrofining reactor 4 and carry out hydrofining together with after described cracking high score oil and the described pre-treatment prepared in step (a) generate oily mixing, and the oily another part of low point of described heat enters pre-add hydrogen guard reactor 3 after mixing with the described full fraction of coal tar in step (a) carries out weighted BMO spaces.
Described in the present embodiment, the character of full fraction of coal tar is as shown in table 1, and the reaction conditions of the trans hydrocracking process of described full fraction of coal tar is as shown in table 2, the gasoline that fractionation obtains and bavin oil properties as shown in table 3.
Embodiment 4
Realize the trans hydrogenation system of full fraction of coal tar of the trans hydrocracking process of full fraction of coal tar in the present embodiment, comprising:
Connect the pre-hydrogenation guard reactor 3 and hydrofining reactor 4 that arrange;
High pressure hot separator 5, is connected with the outlet of described hydrofining reactor 4 and arranges;
Cold high pressure separator 6, be connected with the gaseous phase outlet of described high pressure hot separator 5 and arrange, the gaseous phase outlet of described cold high pressure separator 6 is connected with circulating hydrogen compressor 13, and the pressurized gas of described circulating hydrogen compressor 13 exports to be communicated with the hydrogen inlet of hydrocracking reactor 11 with described pre-hydrogenation guard reactor 3, hydrofining reactor 4 respectively and arranges;
Thermal low-pressure separators 7, is connected with the liquid-phase outlet of described high pressure hot separator 5 and arranges, and the liquid-phase outlet of described thermal low-pressure separators 7 is communicated with the feed(raw material)inlet pipe of described pre-hydrogenation guard reactor 3 and arranges;
Cold low separator 8, is connected with the liquid-phase outlet of described cold high pressure separator 6 and the gaseous phase outlet of described thermal low-pressure separators 7 and arranges;
Separation column 9, is connected with the liquid-phase outlet of described cold low separator 8 and arranges;
Hydrocracking reactor 11, simultaneously exports to be connected with the liquid-phase outlet of described thermal low-pressure separators 7 and the tail oil of described separation column 9 and arranges;
Cracking high-pressure separator 12, is arranged with the outlet of described hydrocracking reactor 11; The liquid-phase outlet of described cracking high-pressure separator 12 is communicated with the feed(raw material)inlet pipe of described hydrofining reactor 4 and arranges; The gaseous phase outlet of described cracking high-pressure separator 12 is connected with described cold low separator 8 and arranges.
The trans hydrocracking process of full fraction of coal tar described in the present embodiment, as shown in Figure 1, comprises the steps:
A full fraction of coal tar is sent into pre-hydrogenation guard reactor 3 by (), pressure be 18MPa, hydrogen to oil volume ratio is 1200: 1, average reaction temperature is 350 DEG C, volume space velocity is 2.5h
-1condition under, use potassium dichromate aqueous solution as hydrogenation protecting agent, weighted BMO spaces is carried out to full fraction of coal tar, obtain pre-treatment generate oil, the consumption of this hydrogenation protecting agent counts 80 μ g/g with chromium element;
B described pre-treatment is generated oil feeding hydrofining reactor 4 and carries out hydrofining by (), obtain hydrotreated product; Described hydrorefined condition is: pressure 18MPa, hydrogen to oil volume ratio 1200: 1, temperature 350 DEG C, volume space velocity 2.5h
-1; The molybdenum oxide that the Hydrobon catalyst that described hydrofining uses is 22wt%, the nickel oxide of 8wt%, surplus is alumina supporter, and the pore volume of this catalyst for refining be 0.4mL/g, specific surface area is 190m
2/ g;
C () utilizes high pressure hot separator 5 to carry out thermal high separation to described hydrotreated product and obtains thermal high gas phase and thermal high liquid phase; Recycling cold high pressure separator 6 carries out cold anticyclone separation to described thermal high gas phase and obtains cold high score gas and cold anticyclone liquid phase, utilize thermal low-pressure separators 7 to carry out thermal low separation to described thermal high liquid phase and obtain thermal low gas phase and heat low point of oil, after wherein said cold high score gas mixes with hydrogen, can be used as the hydrogen source of hydrofining and the middle hydrocracking of step (e) in weighted BMO spaces, step (b) in step (a); Utilize cold low separator 8 to carry out cold low to described thermal low gas phase and the mixture of described cold anticyclone liquid phase to be separated and to obtain cold low point of gas and cold low point of oil; Wherein, the working pressure that described thermal high is separated is 17.3MPa, service temperature is 310 DEG C; The working pressure carrying out described cold anticyclone separation is 17.2MPa, service temperature is 48 DEG C; The working pressure carrying out described thermal low separation is 2.0MPa, service temperature is 310 DEG C; The working pressure carrying out described cold low separation is 2.0MPa, service temperature is 45 DEG C;
D described cold low point of oil is sent into separation column 9 and is carried out fractionation by (), cutting out gasoline, boiling point that boiling point is less than 150 DEG C is tail oil and the fuel gas that diesel oil, the boiling point of 150 ~ 370 DEG C is greater than 370 DEG C;
E low for a described heat point of oily part and described tail oil are made mixing oil by (), described mixing oil is sent into hydrocracking reactor 11, described mixing oil flows through cracking protective material bed successively in described hydrocracking reactor 11, cracking pretreating agent bed and cracking catalyst bed carry out hydrocracking reaction, wherein said cracking protective material and cracking pretreating agent are respectively the FC-14 that Fu Yan institute develops, ZHC-01 Catalyst For Single-stage Hydrocracking, described cracking catalyst is the DHC39 hydrocracking catalyst of Uop Inc.'s exploitation, the condition of described hydrocracking is: pressure 17MPa, hydrogen to oil volume ratio 2000: 1, temperature 340 DEG C, volume space velocity 4h
-1, be cracking high score gas and cracking high score oil by the product separation of hydrocracking, wherein said cracking high score gas jointly carries out cold low with described thermal low gas phase with the mixture of described cold anticyclone liquid phase and is separated, and carries out hydrofining together with after described cracking high score oil and the described pre-treatment prepared in step (a) generate oily mixing, and the oily another part of low point of described heat mixes with the described full fraction of coal tar in step (a) and carries out weighted BMO spaces.
Described in the present embodiment, the character of full fraction of coal tar is as shown in table 1, and the reaction conditions of the trans hydrocracking process of described full fraction of coal tar is as shown in table 2, the gasoline that fractionation obtains and bavin oil properties as shown in table 3.
Comparative example
The trans hydrocracking process of full fraction of coal tar described in this comparative example, comprises the steps:
A full fraction of coal tar is sent into pre-hydrogenation guard reactor 3 by (), pressure be 18MPa, hydrogen to oil volume ratio is 1200: 1, average reaction temperature is 350 DEG C, volume space velocity is 2.5h
-1condition under, use potassium dichromate aqueous solution as hydrogenation protecting agent, weighted BMO spaces is carried out to full fraction of coal tar, obtain pre-treatment generate oil, the consumption of this hydrogenation protecting agent counts 80 μ g/g with chromium element;
B described pre-treatment is generated oil feeding hydrofining reactor 4 and carries out hydrofining by (), obtain hydrotreated product; Described hydrorefined condition is: pressure 18MPa, hydrogen to oil volume ratio 1200: 1, temperature 350 DEG C, volume space velocity 2.5h
-1; The molybdenum oxide that the Hydrobon catalyst that described hydrofining uses is 22wt%, the nickel oxide of 8wt%, surplus is alumina supporter, and the pore volume of this catalyst for refining be 0.4mL/g, specific surface area is 190m
2/ g;
C () utilizes high pressure hot separator 5 to carry out thermal high separation to described hydrotreated product and obtains thermal high gas phase and thermal high liquid phase; Recycling cold high pressure separator 6 carries out cold anticyclone separation to described thermal high gas phase and obtains cold high score gas and cold anticyclone liquid phase, utilize thermal low-pressure separators 7 to carry out thermal low separation to described thermal high liquid phase and obtain thermal low gas phase and heat low point of oil, after wherein said cold high score gas mixes with hydrogen, can be used as the hydrogen source of hydrofining and the middle hydrocracking of step (e) in weighted BMO spaces, step (b) in step (a); Utilize cold low separator 8 to carry out cold low to described thermal low gas phase and the mixture of described cold anticyclone liquid phase to be separated and to obtain cold low point of gas and cold low point of oil; Wherein, the working pressure that described thermal high is separated is 17.3MPa, service temperature is 310 DEG C; The working pressure carrying out described cold anticyclone separation is 17.2MPa, service temperature is 48 DEG C; The working pressure carrying out described thermal low separation is 2.0MPa, service temperature is 310 DEG C; The working pressure carrying out described cold low separation is 2.0MPa, service temperature is 45 DEG C;
D described cold low point of oil is sent into separation column 9 and is carried out fractionation by (), cutting out gasoline, boiling point that boiling point is less than 150 DEG C is tail oil and the fuel gas that diesel oil, the boiling point of 150 ~ 370 DEG C is greater than 370 DEG C;
E low for a described heat point of oily part and described tail oil are made mixing oil by (), described mixing oil is sent into hydrocracking reactor 11, described mixing oil flows through cracking protective material bed successively in described hydrocracking reactor 11, cracking pretreating agent bed and cracking catalyst bed carry out hydrocracking reaction, wherein said cracking protective material and cracking pretreating agent are respectively the FC-14 that Fu Yan institute develops, ZHC-01 Catalyst For Single-stage Hydrocracking, described cracking catalyst is the DHC39 hydrocracking catalyst of Uop Inc.'s exploitation, the condition of described hydrocracking is: pressure 17MPa, hydrogen to oil volume ratio 2000: 1, temperature 340 DEG C, volume space velocity 4h
-1, be cracking high score gas and cracking high score oil by the product separation of hydrocracking, wherein said cracking high score gas jointly carries out cold low with described thermal low gas phase with the mixture of described cold anticyclone liquid phase and is separated, and described cracking high score oil directly enters separation column 9 and carries out fractionation, and the oily another part of low point of described heat mixes with the described full fraction of coal tar in step (a) and carries out weighted BMO spaces.
Described in this comparative example, the character of full fraction of coal tar is as shown in table 1, and the reaction conditions of the trans hydrocracking process of described full fraction of coal tar is as shown in table 2, the gasoline that fractionation obtains and bavin oil properties as shown in table 3.
The character of full fraction of coal tar described in table 1 embodiment 1-4 and comparative example
| Project | Full fraction of coal tar |
| Density (20 DEG C), g/cm 3 | 1.0981 |
| Carbon residue, wt% | 5.11 |
| Ultimate analysis, wt% | |
| C | 81.31 |
| H | 9.82 |
| S | 0.23 |
| N | 0.76 |
| O | 7.83 |
| Metallic element, μ g/g | |
| Fe | 66.28 |
| Na | 0.63 |
| Ni | 0.0483 |
| V | 0.0282 |
| Colloid, wt% | 37.4 |
| Water, wt% | 5.4 |
| > 360 DEG C of tail oils, wt% | 51.5 |
The reaction conditions of the trans hydrocracking process of full fraction of coal tar described in table 2 embodiment 1-4 and comparative example
Gasoline, bavin oil properties that in table 3 embodiment 1-4 and comparative example, fractionation obtains
As can be seen from Table 2, the trans hydrocracking process of full fraction of coal tar of the present invention is adopted to carry out hydrotreatment to full fraction of coal tar, the total amount of the fuel gas that fractionation obtains, gasoline, diesel oil accounts for more than the 88.6wt% of coal tar consumption, the total amount of the fuel gas obtained with comparative example fractionation, gasoline, diesel oil accounts for compared with the 79.6wt% of coal tar consumption, and hydrocracking process of the present invention significantly improves the utilization ratio of coal tar raw material.As shown in Table 3, adopt the trans hydrocracking process of full fraction of coal tar of the present invention to carry out hydrotreatment to coal tar, the sulfur content in gasoline that fractionation obtains is not higher than 8.5 μ gg
-1, nitrogen content is not higher than 1.2 μ gg
-1, in the diesel oil simultaneously obtained, sulphur content is not higher than 9.2 μ gg
-1, nitrogen content is not higher than 2.2 μ gg
-1, therefore the two all meets the quality standard of clean fuel.
Obviously, above-described embodiment is only for clearly example being described, and the restriction not to embodiment.For those of ordinary skill in the field, can also make other changes in different forms on the basis of the above description.Here exhaustive without the need to also giving all embodiments.And thus the apparent change of extending out or variation be still among the protection domain of the invention.
Claims (15)
1. the trans hydrocracking process of full fraction of coal tar, comprises the steps:
A (), under hydrogenation protecting agent existent condition, carries out weighted BMO spaces to full fraction of coal tar, obtain pre-treatment and generate oil;
B () generates oil to described pre-treatment and carries out hydrofining, obtain hydrotreated product;
C () is carried out thermal high separation to described hydrotreated product and is obtained thermal high gas phase and thermal high liquid phase; Again cold anticyclone separation is carried out to described thermal high gas phase and obtain cold high score gas and cold anticyclone liquid phase; Thermal low separation is carried out to described thermal high liquid phase and obtains thermal low gas phase and heat low point of oil; Carry out cold low to described thermal low gas phase and the mixture of described cold anticyclone liquid phase to be separated and to obtain cold low point of gas and cold low point of oil;
D () carries out fractionation to described cold low point of oil, cut out gasoline, tail oil and fuel gas that diesel oil, boiling point are greater than 370 DEG C;
E low for a described heat point of oily part and described tail oil are mixed to get mixing oil by (), hydrocracking reaction is carried out to described mixing oil, be cracking high score gas and cracking high score oil by the product separation of hydrocracking, together with after wherein said cracking high score oil and the described pre-treatment prepared in step (a) generate oily mixing, carry out hydrofining.
2. the trans hydrocracking process of full fraction of coal tar according to claim 1, it is characterized in that, the part that low point of described heat is oily and described tail oil are made mixing oil and carry out hydrocracking reaction, and another part mixes with the described full fraction of coal tar in step (a) and carries out weighted BMO spaces.
3. the trans hydrocracking process of full fraction of coal tar according to claim 1 and 2, it is characterized in that, the temperature of carrying out weighted BMO spaces in step (a) is 300 ~ 450 DEG C, and pressure is 18MPa, hydrogen to oil volume ratio is 800 ~ 1500: 1, and volume space velocity is 0.1 ~ 5.0h
-1.
4. according to the arbitrary described trans hydrocracking process of full fraction of coal tar of claim 1-3, it is characterized in that, the hydrogenation protecting agent used in step (a) is compound containing active metallic element or the aqueous solution, and described active metallic element is one or more in VB, VIB, group VIII metal element; In every gram of described hydrogenation protecting agent, the content of active metallic element is 50 ~ 200 μ g.
5. according to the arbitrary described trans hydrocracking process of full fraction of coal tar of claim 1-4, it is characterized in that, carrying out hydrorefined temperature in step (b) is 330 ~ 390 DEG C, and pressure is 18MPa, hydrogen to oil volume ratio 800 ~ 1500: 1, volume space velocity is 0.5 ~ 5.0h
-1.
6. according to the arbitrary described trans hydrocracking process of full fraction of coal tar of claim 1-5, it is characterized in that, the Hydrobon catalyst used of hydrofining described in step (b) comprises the molybdenum oxide of 5 ~ 25wt%, the nickel oxide of 1 ~ 10wt%, surplus is silica support or alumina supporter, and the pore volume of described catalyst for refining is 0.20 ~ 0.50mL/g, specific surface area is 100 ~ 200m
2/ g.
7., according to the arbitrary described trans hydrocracking process of full fraction of coal tar of claim 1-6, it is characterized in that, in step (c), the working pressure carrying out described thermal high separation is 17.3MPa, service temperature is 310 DEG C; The working pressure carrying out described cold anticyclone separation is 17.2MPa, service temperature is 48 DEG C; The working pressure carrying out described thermal low separation is 2.0MPa, service temperature is 310 DEG C; The working pressure carrying out described cold low separation is 2.0MPa, service temperature is 45 DEG C.
8. according to the arbitrary described trans hydrocracking process of full fraction of coal tar of claim 1-7, it is characterized in that, be separated the described cracking high score gas obtained and described thermal low gas phase and the mixture of described cold anticyclone liquid phase in step (e) and jointly carry out cold low and be separated and obtain cold low point of gas and cold low point of oil.
9. according to the arbitrary described trans hydrocracking process of full fraction of coal tar of claim 1-8, it is characterized in that, the pressure carrying out described hydrocracking in step (e) is 17MPa, hydrogen to oil volume ratio is 800 ~ 3000: 1, temperature is 260 ~ 340 DEG C, volume space velocity is 0.1 ~ 4.0h
-1.
10. according to the arbitrary described trans hydrocracking process of full fraction of coal tar of claim 1-9; it is characterized in that; when carrying out hydrocracking reaction in step (e); described mixing oil flows through cracking protective material bed, cracking pretreating agent bed and cracking catalyst bed successively; wherein said cracking protective material, cracking pretreating agent and cracking catalyst all with any one or a few in Mo, W, Co or Ni for active ingredient, with aluminum oxide and/or molecular sieve for carrier.
11. according to the arbitrary described trans hydrocracking process of full fraction of coal tar of claim 1-10, it is characterized in that, described cold high score gas is mixed the hydrogen source being used as hydrofining and the middle hydrocracking of step (e) in weighted BMO spaces, step (b) in step (a) with hydrogen.
12. 1 kinds of trans hydrogenation systems of full fraction of coal tar, comprising:
Connect the pre-hydrogenation guard reactor (3) and hydrofining reactor (4) that arrange; The outlet of described pre-hydrogenation guard reactor (3) is connected with the entrance of described hydrofining reactor (4) by the feed(raw material)inlet pipe of described hydrofining reactor (4);
High pressure hot separator (5), is connected with the outlet of described hydrofining reactor (4) and arranges;
Cold high pressure separator (6), is connected with the gaseous phase outlet of described high pressure hot separator (5) and arranges;
Thermal low-pressure separators (7), is connected with the liquid-phase outlet of described high pressure hot separator (5) and arranges;
Cold low separator (8), is connected with the liquid-phase outlet of described cold high pressure separator (6) and the gaseous phase outlet of described thermal low-pressure separators (7) and arranges;
Separation column (9), is connected with the liquid-phase outlet of described cold low separator (8) and arranges;
Hydrocracking reactor (11), simultaneously exports to be connected with the liquid-phase outlet of described thermal low-pressure separators (7) and the tail oil of described separation column (9) and arranges;
Cracking high-pressure separator (12), is arranged with the outlet of described hydrocracking reactor (11);
It is characterized in that; the liquid-phase outlet of described cracking high-pressure separator (12) is communicated with the feed(raw material)inlet pipe of described hydrofining reactor (4) and arranges, and carries out hydrofining together with after the generation oil of the liquid phase and described pre-hydrogenation guard reactor (3) that are suitable for described cracking high-pressure separator (12) mixes.
The trans hydrogenation system of 13. full fraction of coal tar according to claim 12, is characterized in that, the liquid-phase outlet of described thermal low-pressure separators (7) is communicated with the feed(raw material)inlet pipe of described pre-hydrogenation guard reactor (3) simultaneously and arranges.
14. trans hydrogenation systems of full fraction of coal tar according to claim 12 or 13, is characterized in that, the gaseous phase outlet of described cracking high-pressure separator (12) is connected with described cold low separator (8) and arranges.
15. according to the arbitrary described trans hydrogenation system of full fraction of coal tar of claim 12-14; it is characterized in that; be connected with circulating hydrogen compressor (13) with the gaseous phase outlet of described cold high pressure separator (6), the pressurized gas of described circulating hydrogen compressor (13) exports to be communicated with the hydrogen inlet of hydrocracking reactor (11) with described pre-hydrogenation guard reactor (3), hydrofining reactor (4) respectively and arranges.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN106854474A (en) * | 2016-12-30 | 2017-06-16 | 山东胜星化工有限公司 | A kind of new coal tar hydrogenating cracker and preparation method thereof |
| CN107987882A (en) * | 2016-10-27 | 2018-05-04 | 中国石油化工股份有限公司 | A kind of method for hydrogen cracking for mixing artificial coal tar |
| CN109536205A (en) * | 2019-01-23 | 2019-03-29 | 陕西东鑫垣化工有限责任公司 | A kind of light tar mixes refining wax oil processing unit (plant) and method |
| CN111073701A (en) * | 2018-10-19 | 2020-04-28 | 中国石油化工股份有限公司 | Processing system and method for high-viscosity poly α olefin synthetic oil |
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2014
- 2014-10-15 CN CN201410544912.5A patent/CN104449836B/en active Active
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN107987882A (en) * | 2016-10-27 | 2018-05-04 | 中国石油化工股份有限公司 | A kind of method for hydrogen cracking for mixing artificial coal tar |
| CN106854474A (en) * | 2016-12-30 | 2017-06-16 | 山东胜星化工有限公司 | A kind of new coal tar hydrogenating cracker and preparation method thereof |
| CN111073701A (en) * | 2018-10-19 | 2020-04-28 | 中国石油化工股份有限公司 | Processing system and method for high-viscosity poly α olefin synthetic oil |
| CN111073701B (en) * | 2018-10-19 | 2021-12-17 | 中国石油化工股份有限公司 | Processing system and method for high-viscosity poly-alpha-olefin synthetic oil |
| CN109536205A (en) * | 2019-01-23 | 2019-03-29 | 陕西东鑫垣化工有限责任公司 | A kind of light tar mixes refining wax oil processing unit (plant) and method |
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